CN103803617A - Method for producing aluminum oxide from coal ash through acid process - Google Patents
Method for producing aluminum oxide from coal ash through acid process Download PDFInfo
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- CN103803617A CN103803617A CN201310746884.0A CN201310746884A CN103803617A CN 103803617 A CN103803617 A CN 103803617A CN 201310746884 A CN201310746884 A CN 201310746884A CN 103803617 A CN103803617 A CN 103803617A
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Abstract
The invention provides a method for producing aluminum oxide from coal ash through an acid process. The method comprises the steps: S1, mixing coal ash and a solvent to obtain primary slurry, carrying out magnetic separation on the primary slurry, and filtering to obtain a Fe-poor filter cake; S2, carrying out acid dissolution on the Fe-poor filter cake to obtain acid slurry; S3, carrying out residue-liquid separation on the acid slurry to obtain an aluminum chloride solution and residues; S4, carrying out resin adsorption on the aluminum chloride solution to remove impurities to obtain a refined aluminum chloride solution; S5, carrying out concentration and crystallization treatment on the refined aluminum chloride solution to obtain an aluminum chloride crystal and condensed water; S6, calcining the aluminum chloride crystal to obtain aluminum oxide. The solvent in the step S1 comprises at least part of the condensed water in the step S5. The condensed water generated in the step S5 is used for preparing the primary slurry, so that the condensed water is reutilized, the condensed water treating burden in the traditional process is relieved, and the water consumption and cost are reduced.
Description
Technical field
The present invention relates to flyash process field, produce the method for aluminum oxide in particular to a kind of flyash acid system.
Background technology
Rich coal resources in China, and using coal as the basic fuel of electrical production.Along with the fast development of energy industry, flyash quantity discharged sharply increases, and exerts heavy pressures on to the development of the national economy and ecotope.Owing to containing the valuable mineral resources such as oxidation aluminium plus gallium in flyash, therefore flyash being fully utilized, turned waste into wealth has become study hotspot content widely.
At present, flyash extracts in the method for aluminum oxide, and acid system extracts the advantages such as digesting efficiency of alumina is high, technique is simple, sour reusable edible because of it, be just day by day widely adopted.
CN1792802A discloses " a kind of method of extracting aluminum oxide from flyash ", the method is by the flyash after roasting and sulfuric acid reaction, filter, concentrate generation crystalline sulfuric acid aluminium, then the high-temperature calcination of crystalline sulfuric acid aluminium is decomposed and generated aluminum oxide and sulfur trioxide gas.CN101234774A discloses " a kind of method of being prepared aluminum oxide by coal series kaolin rock or coal gangue ", the method is calcining and activating after fragmentation, grinding by coal series kaolin rock or coal gangue, then generate liquor alumini chloridi with hydrochloric acid reaction, by salting-out process, crystal aluminum chloride is settled out and is separated again, crystal aluminum chloride calcining and decomposing generates aluminum oxide and hydrogen chloride gas.CN1065255A discloses a kind of " technique for production of alumina by chlorhydric acid-soda method ", in technique take hydrochloric acid as dissolution medium, ore Cheng Fenhou in small, broken bits, through high-temperature roasting, salt adding and hcl reaction in high pressure enamel reaction still, generate alkaline aluminium salt, through separating desiliconization.Alkaline aluminium salt evaporation concentration, Roasting Decomposition are made to γ shape aluminum oxide and hydrogen chloride gas.CN102205982A discloses " a kind of flyash acid system is produced the circulation utilization method of acid in alumina process ", the method reclaims hydrogen chloride gas, and utilize the hydrogen chloride gas reclaiming to be prepared into the hydrochloric acid that meets acid-soluble concentration requirement, and then for acid-soluble step.
But flyash acid system is produced in the system of aluminum oxide except sour usage quantity is more, the use of water and consumption are all more, do not take effective recycle, can cause the waste of water resources, a large amount of water of condensation that especially liquor alumini chloridi is evaporated through evaporation and crystallization system, owing to containing certain acid, if return to waterworks as neutral water, need to take pretreatment technology, increase the inputs such as medicine and equipment, complex process, cost are improved.
Summary of the invention
The present invention aims to provide a kind of method of flyash acid system production aluminum oxide, produces the serious problem of alumina technology water resource waste to solve flyash in prior art.
To achieve these goals, according to an aspect of the present invention, provide a kind of flyash acid system to produce the method for aluminum oxide, comprise: step S1, flyash and solvent are mixed to get to original slurry, and original slurry is carried out to magnetic separation, filtration, obtain poor iron filter cake; Step S2, carries out poor iron filter cake acid-soluble, obtains wintercherry liquid; Step S3, carries out the separation of slag liquid by wintercherry liquid, obtains liquor alumini chloridi and residue; Step S4, carries out resin absorption removal of impurities processing by liquor alumini chloridi, obtains refined crystalline aluminium chloride liquid; Step S5, carries out condensing crystal processing by refined crystalline aluminium chloride liquid, obtains crystal aluminum chloride and water of condensation; And step S6, crystal aluminum chloride is calcined, obtain aluminum oxide, the solvent in step S1 comprises the water of condensation at least part of step S5.
Further, above-mentioned steps S5 comprises: adopt four-effect evaporator system that refined crystalline aluminium chloride liquid is carried out to evaporative crystallization processing, obtain crystal aluminum chloride and water of condensation, water of condensation comprises live steam condensed water, an effect secondary steam water of condensation, two effect secondary steam water of condensation, triple effect secondary steam water of condensation, quadruple effect water of condensation.
Further, above-mentioned steps S1 comprises: step S11, flyash and solvent are mixed to get to original slurry, and the amount ratio of solvent and flyash is 2.5～3m
3/ t flyash, the solvent in step S11 comprises from the part one in step S5 imitates secondary steam water of condensation and/or at least part of two effect secondary steam water of condensation, and preferably the consumption of water of condensation is 0.6～1m
3/ t flyash, further preferably the consumption of an effect secondary steam water of condensation is 0～0.95m
3/ t flyash, the consumption of two effect secondary steam water of condensation is 0.05～0.65m
3/ t flyash; Step S12, carries out magnetic separation to original slurry, obtains rich iron mortar and poor iron mortar; Step S13, filters poor iron mortar, obtains poor iron filter cake and poor iron filtrate.
Further, the poor iron filtrate in above-mentioned steps S13 is returned to a part and the flyash as solvent in step S11 and is mixed to form new original slurry, and the amount of preferably returning to the poor iron filtrate of step S11 is 1.5～2.5m
3/ t flyash.
Further, above-mentioned steps S12 comprises: steps A, and in magnetic separation system, utilize wash-down water to rinse original slurry, obtain rich iron mortar and rinse disposed slurry; Step B, filters rich iron mortar, obtains rich iron filtrate and Fu Tie filter cake; Step C, makes rich iron filtrate return to steps A and rinse disposed slurry or original slurry together with wash-down water; Step D, repeating step A, B and C lower than 1.0wt%, obtain poor iron mortar to rinsing Indian red content in disposed slurry.
Further, the consumption of above-mentioned wash-down water is 0.3～0.7m
3/ t flyash.
Further, above-mentioned steps S2 comprises: step S21, poor iron filter cake is dissolved in acid solution, and obtain mixed solution; Step S22, adopts hot steam heating mixed solution, obtains hot mixed solution; Step S23, adopts refrigerant that hot mixed solution is cooled to 80～100 ℃, obtains wintercherry liquid, and refrigerant comprises partial oxidation aluminum solutions.
Further, the introducing of the hot steam in the above-mentioned steps S22 water yield is 0.1～0.15m
3/ t flyash, the consumption of refrigerant is 0.3～0.6m
3/ t flyash.
Further, the acid solution in above-mentioned steps S21 is hydrochloric acid soln, and in mixed solution, the concentration of hydrochloric acid is 20～30wt%, and in hydrochloric acid, in HCl and flyash, the mol ratio of aluminum oxide is 4:1～6:1.
Further, above-mentioned steps S3 comprises: step S31, wintercherry liquid is carried out to the separation of slag liquid, and obtain aluminum chloride initial soln and initial residue; Step S32, adopt the initial residue of detergent washing, obtain residue and elutriant, and elutriant is mixed with aluminum chloride initial soln, obtain liquor alumini chloridi, washing composition comprises the water of condensation of part from step S5, and preferably part comprises at least part of live steam condensed water and/or an at least part of effect secondary steam water of condensation from the water of condensation of step S5.
Further, the consumption of above-mentioned washing composition is 1.0～1.4m
3/ t flyash, the consumption of live steam condensed water is 0.45～0.65m
3/ t flyash, the consumption of an effect secondary steam water of condensation is 0.55～0.85m
3/ t flyash.
Further, above-mentioned steps S4 comprises: step S41, liquor alumini chloridi is carried out to resin absorption removal of impurities processing, and obtain refined crystalline aluminium chloride liquid and saturated resin; Step S42, use regenerated solvent to carry out wash-out to saturated resin, obtain regenerating resin, regenerated solvent comprises the water of condensation of part from step S5, and preferably part comprises part triple effect secondary steam water of condensation and at least part of quadruple effect water of condensation from the water of condensation of step S5.
Further, the consumption of above-mentioned regenerated solvent is 0.10～0.21m
3/ t flyash, the consumption of triple effect secondary steam water of condensation is 0～0.20m
3/ t flyash, the consumption of quadruple effect water of condensation is 0.05～0.15m
3/ t flyash.
Further, above-mentioned steps S6 comprises: step S61, crystal aluminum chloride is calcined, and obtain aluminum oxide and flue gas; Step S62, adopts water to absorb flue gas, and acid solution is absorbed; Step S63, makes to absorb acid solution and returns to step S2 and dissolve poor iron filter cake.
Further, in above-mentioned steps S62, the consumption of water used is 0.8～1.15m
3/ t flyash, and water comprises two effect secondary steam water of condensation, part quadruple effect water of condensation and/or at least part of triple effect secondary steam water of condensation of part from step S5.
Further, the consumption of above-mentioned two effect secondary steam water of condensation is 0～0.55m
3/ t flyash, the consumption of triple effect secondary steam water of condensation is 0.50～0.80m
3/ t flyash.
Apply technical scheme of the present invention, in the evaporation and crystal process of step S5, can produce a large amount of water of condensation, the application is the preparation for original slurry by this water of condensation, makes water of condensation obtain recycling on the one hand, has effectively alleviated the pressure of existing art breading water of condensation; On the other hand, replace and in prior art, dissolved flyash former water used with water of condensation, and then reduced water consumption and the cost of flyash acid system production aluminum oxide.
Except object described above, feature and advantage, the present invention also has other object, feature and advantage.Below with reference to embodiment, the present invention is further detailed explanation.
Accompanying drawing explanation
The Figure of description that forms the application's a part is used to provide a further understanding of the present invention, and schematic description and description of the present invention is used for explaining the present invention, does not form inappropriate limitation of the present invention.In the accompanying drawings:
The flyash acid system that Fig. 1 shows a kind of preferred embodiment of the application to be provided is produced the process flow diagram of the method for aluminum oxide.
Embodiment
It should be noted that, in the situation that not conflicting, the feature in embodiment and embodiment in the application can combine mutually.Describe below with reference to the accompanying drawings and in conjunction with the embodiments the present invention in detail.
In a kind of typical embodiment of the present invention, provide a kind of flyash acid system to produce the method for aluminum oxide, the method comprises: step S1, is mixed to get original slurry by flyash and solvent, and original slurry is carried out to magnetic separation, filtration, obtain poor iron filter cake; Step S2, carries out poor iron filter cake acid-soluble, obtains wintercherry liquid; Step S3, carries out the separation of slag liquid by wintercherry liquid, obtains liquor alumini chloridi and residue; Step S4, carries out resin absorption removal of impurities processing by liquor alumini chloridi, obtains refined crystalline aluminium chloride liquid; Step S5, carries out evaporative crystallization processing by refined crystalline aluminium chloride liquid, obtains crystal aluminum chloride and water of condensation; And step S6, crystal aluminum chloride is calcined, obtain aluminum oxide, wherein, the solvent in above-mentioned steps S1 comprises the water of condensation at least part of step S5.
Above-mentioned flyash acid system is produced the method for aluminum oxide and is improved for conventional technical process at present, wherein in the evaporation and crystal process of step S5, can produce a large amount of water of condensation, the application is the preparation for original slurry by this water of condensation, make water of condensation obtain recycling on the one hand, effectively alleviated the pressure of existing art breading water of condensation; On the other hand, replace and in prior art, dissolved flyash former water used with water of condensation, and then reduced water consumption and the cost of flyash acid system production aluminum oxide.
Well known to a person skilled in the art it is that liquor alumini chloridi is carried out when evaporative crystallization is processed heating liquor alumini chloridi, make liquid component volatilization wherein, and then produce a large amount of water of condensation.In a kind of preferred embodiment of the present invention, the step S5 of aforesaid method comprises: adopt four-effect evaporator system that refined crystalline aluminium chloride liquid is carried out to evaporative crystallization processing, obtain crystal aluminum chloride and water of condensation, water of condensation comprises live steam condensed water, an effect secondary steam water of condensation, two effect secondary steam water of condensation, triple effect secondary steam water of condensation, quadruple effect water of condensation.
In above-mentioned preferred embodiment, adopt four-effect evaporator system that the refined crystalline aluminium chloride liquid after removal of impurities is carried out in the process of evaporative crystallization processing, use the thermals source such as water vapor to heat the liquor alumini chloridi in four-effect evaporator system, water vapor is in the time that the refined crystalline aluminium chloride liquid in evaporator room heats, refined crystalline aluminium chloride liquid in the first evaporator room is subject to thermogenesis one to imitate secondary steam water of condensation, refined crystalline aluminium chloride liquid in the second evaporator room is subject to thermogenesis two to imitate secondary steam water of condensation, refined crystalline aluminium chloride liquid in the 3rd evaporator room is subject to thermogenesis triple effect secondary steam water of condensation, refined crystalline aluminium chloride liquid in the 4th evaporator room is subject to thermogenesis quadruple effect water of condensation, and reduce or form live steam condensed water after cooling as the water vapor of thermal source temperature after by four-effect evaporator system, above-mentioned various steam condensate has formed the overwhelming majority of the water of condensation of aforesaid method.Wherein, by being mixed with part acid vapour in the steam condensate evaporating in refined crystalline aluminium chloride liquid, make formed water of condensation be slightly acidic.
Adopt slightly difference of Acidity in the various steam condensates that above-mentioned four-effect evaporator system obtains, those skilled in the art can carry out recycle targetedly according to the acidity of its reality, the present invention has carried out preferably the recycle approach of water of condensation according to the applicant's actual process, such as according to the water of condensation of different steps, acid content is inconsistent, the higher certain applications of acidity are in resin regeneration, the part that acid content is low is washed for wash heat, the part that acid content is lower is used for configuring original slurry, residue absorbs for acid, below will preferably be elaborated to this, those skilled in the art should be clearly, preferably just the present invention is directed to below that specific technique makes, can not be used as the protection domain that limits invention claim, those skilled in the art can be take the present invention as reference pin produce the water of condensation producing in the technique of aluminum oxide and carry out recycle being different from the flyash acid system of invention.
In the another kind of preferred embodiment of the present invention, the step S1 of aforesaid method comprises: step S11, flyash and solvent are mixed to get to original slurry, and the amount ratio of above-mentioned solvent and flyash is 2.5～3m
3/ t flyash, the solvent in above-mentioned steps S11 comprises from the part one of step S5 imitates secondary steam water of condensation and/or at least part of two effect secondary steam water of condensation, and preferably the consumption of water of condensation is 0.6～1m
3/ t flyash, further preferably the consumption of an effect secondary steam water of condensation is 0～0.95m
3/ t flyash, the consumption of two effect secondary steam water of condensation is 0.05～0.65m
3/ t flyash; Step S12, carries out magnetic separation to original slurry, obtains rich iron mortar and poor iron mortar; And step S13, poor iron mortar is filtered, obtain poor iron filter cake and poor iron filtrate.
Adopt above-mentioned steps to prepare poor iron filter cake, wherein an applied effect secondary steam water of condensation and two effect secondary steam water of condensation have a small amount of acid ion, solvent can dissolve part soluble ion in flyash, make original slurry be weakly alkaline, and acid ion in an effect secondary steam water of condensation and two effect secondary steam water of condensation can in and alkali ion but original slurry keeps neutral, and can not affect the effect of magnetic separation, and realize the effect of Substitute For Partial fresh solvent.The enforcement of above-mentioned detailed process can be take magnetic separation process of the prior art as reference, such as by flyash through being crushed to below 100 orders, wherein the amount ratio of solvent and flyash is 2.5～3m
3/ t flyash forms original slurry, and those skilled in the art are noted that above-mentioned solvent is generally water, and the application has comprised water of condensation, and the consumption of the preferred water of condensation of the present invention is 0.6～1m
3/ t flyash, further preferably the consumption of an effect secondary steam water of condensation is 0～0.95m
3/ t flyash, the consumption of two effect secondary steam water of condensation is 0.05～0.65m
3/ t flyash; Then on magnetic separator, carry out magnetic separation, obtain rich iron mortar and poor iron mortar, magnetic separation field intensity can be set between 1.0～2.0 ten thousand GS, wherein rich iron mortar and poor iron mortar and those skilled in the art's understanding is identical is a relative concept, after magnetic separation, iron can progressively separate and enrichment from original slurry, form rich iron mortar and the relatively low poor iron mortar of iron level that iron level is higher, wherein in poor iron mortar, the content of aluminium is higher, and the prepared aluminum oxide of the application derives from poor iron mortar; Then prepared poor iron mortar is filtered, obtain poor iron filter cake and poor iron filtrate, the prepared aluminum oxide of the application derives from poor iron filter cake.
In order further to save the consumption of water of the present invention, preferably the poor iron filtrate in above-mentioned steps S13 is returned to a part and the flyash as solvent in step S11 and is mixed to form new original slurry, and the amount of preferably returning to the poor iron filtrate of step S11 is 1.5～2.5m
3/ t flyash.
In addition, contriver is also optimized the step S12 of above-described embodiment, further saves the usage quantity of water, and preferably above-mentioned steps S12 comprises: steps A, and in magnetic separation system, utilize wash-down water to rinse original slurry, obtain rich iron mortar and rinse disposed slurry; Step B, filters rich iron mortar, obtains rich iron filtrate and Fu Tie filter cake; Step C, makes rich iron filtrate return to steps A and rinse disposed slurry or original slurry together with wash-down water; And step D, repeating step A, B and C lower than 1.0wt%, obtain poor iron mortar to rinsing Indian red content in disposed slurry.In said process, wash-down water is not to adopt new water completely, but utilize the new water of rich iron filtrate Substitute For Partial of rich iron mortar, because iron level is lower in the rich iron filtrate obtaining after filtering, therefore while utilizing it to rinse rinsing disposed slurry or original slurry as wash-down water, the developing result that can not introduce too much iron and can realize ideal.On the basis of developing result of realizing ideal, save as far as possible the consumption of wash-down water, the consumption of preferred above-mentioned wash-down water is 0.3～0.7m
3/ t flyash.
In another preferred embodiment of the present invention, preferably above-mentioned steps S2 comprises: step S21, poor iron filter cake is dissolved in acid solution, and obtain mixed solution; Step S22, adopts hot steam heating mixed solution, obtains hot mixed solution; And step S23, adopt refrigerant that hot mixed solution is cooled to 80～100 ℃, obtain wintercherry liquid, refrigerant comprises partial oxidation aluminum solutions.In said process, poor iron filter cake is dissolved in to the mixed solution heating forming in acid solution, form in the process of hot mixed solution, promote reacting of acid solution and aluminum oxide in poor iron filter cake, made the alumina leaching in poor iron filter cake, then hot mixed solution has been lowered the temperature and obtained wintercherry liquid, wherein temperature-fall period adopts refrigerant, in prior art, conventional refrigerant is water, and the present invention utilizes the liquor alumini chloridi in step S3 to replace part water, and then the usage quantity of having saved water.
In above-mentioned steps S2, it is 0.1～0.15m that the hot steam in further preferred above-mentioned steps S22 is introduced the water yield
3/ t flyash, the consumption of refrigerant is 0.3～0.6m
3/ t flyash.
The present invention is in the time dissolving poor iron filter cake, the acid solution adopting is identical with conventional acid technological process, for the acid-soluble effect of realizing ideal, preferably the acid solution in above-mentioned steps S21 is hydrochloric acid soln, in mixed solution, the concentration of hydrochloric acid is 20～30wt%, and in hydrochloric acid, in HCl and flyash, the mol ratio of aluminum oxide is 4:1～6:1.
In another preferred embodiment of the present invention, preferably above-mentioned steps S3 comprises: step S31, wintercherry liquid is carried out to the separation of slag liquid, and obtain aluminum chloride initial soln and initial residue; And step S32, adopt the initial residue of detergent washing, obtain residue and elutriant, and elutriant is mixed with aluminum chloride initial soln, obtain liquor alumini chloridi, washing composition comprises the water of condensation of part from step S5, and preferred above-mentioned part comprises at least part of live steam condensed water and/or an at least part of effect secondary steam water of condensation from the water of condensation of step S5.
After completing acid-soluble formation wintercherry liquid, wintercherry liquid is carried out to solid-liquid separation, and in solid-liquid separation process, initial residue is washed, so that aluminum chloride is washed out as much as possible.At present, the washing composition that washing process adopts is also to adopt water, and the present invention, in order further to save the usage quantity of water, preferably sneaks into partial condensation water in water, and the water of condensation in system is utilized again; In order not increase the concentration of acid ion in washing process, preferred above-mentioned water of condensation comprises at least part of live steam condensed water and/or an at least part of effect secondary steam water of condensation.
In order to utilize as much as possible the water of condensation in system in the washing effect of realizing ideal, the usage quantity that water is saved on maximum ground, the consumption of preferred above-mentioned washing composition is 1.0～1.4m
3/ t flyash, the consumption of live steam condensed water is 0.45～0.65m
3/ t flyash, the consumption of an effect secondary steam water of condensation is 0.55～0.85m
3/ t flyash.
In another preferred embodiment of the present invention, preferably above-mentioned steps S4 comprises: step S41, liquor alumini chloridi is carried out to resin absorption removal of impurities processing, and obtain refined crystalline aluminium chloride liquid and saturated resin; And step S42, make spent regeneration solution carry out wash-out to saturated resin, obtain regenerating resin, this regenerated solvent comprises the water of condensation of part from step S5, and preferred above-mentioned part comprises part triple effect secondary steam water of condensation and at least part of quadruple effect water of condensation from the water of condensation of step S5.
The adsorption treatment process of above-mentioned steps S41 is similar to conventional adsorption treatment flow process, and liquor alumini chloridi is passed in the resin column that macroporous type resin cation (R.C.) is housed, and utilizes resin to carry out deironing to the adsorptive power of iron, obtains refined crystalline aluminium chloride liquid.When absorption, treatment temp is that room temperature～90 ℃, preferable range are 60～80 ℃, liquor alumini chloridi flow velocity be 1～4 times of resin volume/hour, preferable range be 2～3 times of resin volumes/hour.Resin column can adopt the mode of single-column or twin columns series winding, and resin is preferably D001,732,742,7020H, 7120H, JK008 or SPC-1 resin etc.In the time obtaining refined crystalline aluminium chloride liquid saturated resin and carry out wash-out, adopt water as regenerated solvent, in order further to save the consumption of the water in resin regeneration process, preferably adopt partial condensation water to substitute regenerated solvent, in regenerative process, the existence of acid ion is not obvious on the impact of regeneration effect, and therefore, preferred above-mentioned water of condensation adopts part triple effect secondary steam water of condensation and at least part of quadruple effect water of condensation.
In the regenerative process of above-mentioned steps S42, the consumption of preferred above-mentioned regenerated solvent is 0.10～0.21m
3/ t flyash, the consumption of triple effect secondary steam water of condensation is 0～0.20m
3/ t flyash, the consumption of quadruple effect water of condensation is 0.05～0.15m
3/ t flyash.
In another preferred embodiment of the present invention, preferably above-mentioned steps S6 comprises: step S61, crystal aluminum chloride is calcined, and obtain aluminum oxide and flue gas; Step S62, adopts water to absorb flue gas, and acid solution is absorbed; And step S63, make to absorb acid solution and return to step S2 and dissolve poor iron filter cake.After obtaining crystal aluminum chloride, need to calcine to form aluminum oxide to crystal aluminum chloride, the flue gas producing in calcination process comprises HCl, not only cause the loss of HCl also can cause environmental pollution if discharged into the atmosphere, therefore, above-described embodiment reclaims flue gas, and returns to reclaim the acid solution forming to step S2 for dissolving poor iron filter cake.
In the process of the recovered flue gas of above-described embodiment, need to consume water, the present invention is in order further to save the consumption of water, and preferably in above-mentioned steps S62, the consumption of water used is 0.8～1.15m
3/ t flyash, and above-mentioned water comprises two effect secondary steam water of condensation, part quadruple effect water of condensation and/or at least part of triple effect secondary steam water of condensation of part from step S5.Two effect secondary steam water of condensation are relative less with acid ion content in triple effect secondary steam water of condensation, therefore, replace part water can not affect the assimilation effect to flue gas, but also realized the recycle of water of condensation with it.Further preferably the consumption of above-mentioned two effect secondary steam water of condensation is 0～0.55m
3/ t flyash, the consumption of triple effect secondary steam water of condensation is 0.50～0.80m
3/ t flyash.
Be more than embodiment after the present invention preferably, might not limit in the above-described embodiments for the cycle applications of water of condensation, in addition, the present invention preferably application of each effect water of condensation follows following rule:
Live steam condensed water after heating is preferentially for the washing of the initial residue of step S3; One effect secondary steam water of condensation is preferentially for the washing of the initial residue of step S3, if there is residue to prepare original slurry for step S1; Two effect secondary steam water of condensation are preferentially prepared original slurry for step S1, if having residue for replenish step S6 smoke absorption water used; Triple effect secondary steam water of condensation is preferentially for step S6 smoke absorption water used, if there be the resin regeneration regenerated solvent of residue for step S4; Quadruple effect water of condensation preferentially, for the resin regeneration regenerated solvent of replenish step S4, remains for step S6 smoke absorption water used if having.Wherein Fig. 1 shows flyash acid system that the preferred embodiment of the present invention provides and produces the method flow schematic diagram of aluminum oxide.
Below with reference to embodiment and comparative example, further illustrate beneficial effect of the present invention.
Embodiment 1
To in flyash according to 2.5m
3the ratio of/t flyash adds water and prepares original slurry, enters magnetic separation system 0.3m
3the wash-down water of/t flyash rinses rich iron mortar get off, and rich iron mortar filters to obtain rich iron filter cake and Fu Tie filtrate, rich iron filtrate 0.3m wherein
3/ t flyash returns and continues to serve as wash-down water, also filters to obtain poor iron filter cake and poor iron filtrate through the poor iron mortar of magnetic separation, and poor iron filtrate is wherein with 1.5m
3the consumption of/t flyash returns joins original slip, and an effect secondary steam water of condensation is with 0.95m
3the consumption of/t flyash and two effect secondary steam water of condensation are respectively with 0.05m
3the consumption of/t flyash supplements the original slip of preparation.
Poor iron filter cake is placed in to acid-resistant reacting kettle, and adding hydrochloric acid formation mixed solution to make acid concentration in mixed solution is 20wt%, and in hydrochloric acid, in HCl and flyash, the mol ratio of aluminum oxide is 4:1, adopts hot steam heating mixed solution to form hot mixed solution, and hot steam is introduced water yield 0.1m
3/ t flyash, the slip after sufficient reacting is squeezed into acid-resistant reacting kettle, and adding consumption is 0.41m
3the liquor alumini chloridi that/t flyash postorder obtains makes reacted hot mixed solution be cooled to 100 ℃, obtains wintercherry liquid.
Wintercherry liquid is squeezed into filter plant and carry out slag liquid and separate and obtain aluminum chloride initial soln and initial residue, use live steam condensed water with 0.45m
3the consumption of/t flyash and an effect secondary steam water of condensation are with 0.55m
3the consumption of/t flyash washs initial residue.Aluminum chloride initial soln is carried out to adsorption-edulcoration by two post series connection ion exchange resin systems of D001 resin, adsorb saturated resin and adopt quadruple effect water of condensation 0.1m
3the regeneration of/t flyash, obtains refined crystalline aluminium chloride liquid.
Refined crystalline aluminium chloride liquid is carried out to evaporative crystallization by four-effect evaporator system, and wherein, thermograde is 120 ℃, 100 ℃, 80 ℃, 60 ℃, and pressure gradient is 0.095MPa, 0.045MPa ,-0.025MPa ,-0.072MPa.Form crystal aluminum chloride and live steam condensed water, an effect secondary steam water of condensation, two effect secondary steam water of condensation, triple effect secondary steam water of condensation and quadruple effect water of condensation.
The crystal aluminum chloride that evaporative crystallization is obtained is calcined 2.5h in 1000 ℃ of High Temperature Furnaces Heating Apparatuss, obtains aluminum oxide and flue gas, and flue gas is 0.55m by consumption
3two effect secondary steam water of condensation and the consumption of/t flyash are 0.57m
3the triple effect secondary steam water of condensation of/t flyash absorbs, and the acid solution that is absorbed is emitted the absorption acid solution in absorption tower and acid storage tank, the acid-soluble step of returning, and the hydrochloric acid that supplementary a small amount of concentration is 30wt%, regulating acid concentration in mixed solution is 20wt%.The yield that calculates the aluminum oxide of embodiment 1 is 65%.
Embodiment 2
To in flyash according to 2.83m
3the ratio of/t flyash adds water and prepares original slurry, enters magnetic separation system 0.5m
3the wash-down water of/t flyash rinses rich iron mortar get off, and rich iron mortar filters to obtain rich iron filter cake and Fu Tie filtrate, rich iron filtrate 0.5m wherein
3/ t flyash returns and continues to serve as wash-down water, also filters to obtain poor iron filter cake and poor iron filtrate through the poor iron mortar of magnetic separation, and poor iron filtrate is wherein with 2.16m
3the consumption of/t flyash returns joins original slip, and an effect secondary steam water of condensation is with 0.16m
3the consumption of/t flyash and two effect secondary steam water of condensation are respectively with 0.51m
3the consumption of/t flyash supplements the original slip of preparation.
Poor iron filter cake is placed in to acid-resistant reacting kettle, and adding hydrochloric acid formation mixed solution to make acid concentration in mixed solution is 25wt%, and in hydrochloric acid, in HCl and flyash, the mol ratio of aluminum oxide is 5:1, adopts hot steam heating mixed solution to form hot mixed solution, and hot steam is introduced water yield 0.13m
3/ t flyash, the slip after sufficient reacting is squeezed into acid-resistant reacting kettle, and adding consumption is 0.12m
3the liquor alumini chloridi that/t flyash postorder obtains makes reacted hot mixed solution be cooled to 90 ℃, obtains wintercherry liquid.
Wintercherry liquid is squeezed into filter plant and carry out slag liquid and separate and obtain aluminum chloride initial soln and initial residue, use live steam condensed water with 0.56m
3the consumption of/t flyash and an effect secondary steam water of condensation wash initial residue with the consumption of 0.84m3/t flyash.Aluminum chloride initial soln is carried out to adsorption-edulcoration by JK008 resin two post series connection ion exchange resin systems, and adsorbing saturated resin employing consumption is 0.05m
3the triple effect secondary steam water of condensation of/t flyash, consumption are 0.14m
3the regeneration of/t flyash quadruple effect water of condensation, obtains refined crystalline aluminium chloride liquid.
Refined crystalline aluminium chloride liquid is carried out to evaporative crystallization by four-effect evaporator system, and wherein, thermograde is 122 ℃, 105 ℃, 84 ℃, 67 ℃, and pressure gradient is 0.096MPa, 0.047MPa ,-0.024MPa ,-0.070MPa.Form crystal aluminum chloride and live steam condensed water, an effect secondary steam water of condensation, two effect secondary steam water of condensation, triple effect secondary steam water of condensation and quadruple effect water of condensation.
The crystal aluminum chloride that evaporative crystallization is obtained is calcined 2.0h in 1100 ℃ of High Temperature Furnaces Heating Apparatuss, obtains aluminum oxide and flue gas, and flue gas is 0.20m by consumption
3two effect secondary steam water of condensation and the consumption of/t flyash are 0.77m
3the triple effect secondary steam water of condensation of/t flyash absorbs, and the acid solution that is absorbed is emitted the absorption acid solution in absorption tower and acid storage tank, the acid-soluble step of returning, and the hydrochloric acid that supplementary a small amount of concentration is 30wt%, regulating acid concentration in mixed solution is 25wt%.The yield that calculates the aluminum oxide of embodiment 2 is 81%.
Embodiment 3
To in flyash according to 3.0m
3the ratio of/t flyash adds water and prepares original slurry, and entering magnetic separation system consumption is 0.7m
3the wash-down water of/t flyash rinses rich iron mortar get off, and rich iron mortar filters to obtain rich iron filter cake and Fu Tie filtrate, rich iron filtrate 0.7m wherein
3/ t flyash returns and continues to serve as wash-down water, also filters to obtain poor iron filter cake and poor iron filtrate through the poor iron mortar of magnetic separation, and poor iron filtrate is wherein with 2.36m
3the consumption of/t flyash returns joins original slip, and an effect secondary steam water of condensation is with 0.02m
3the consumption of/t flyash and two effect secondary steam water of condensation are respectively with 0.62m
3the consumption of/t flyash supplements the original slip of preparation.
Poor iron filter cake is placed in to acid-resistant reacting kettle, adding hydrochloric acid formation mixed solution to make acid concentration in mixed solution is 30wt%, in hydrochloric acid, in HCl and flyash, the mol ratio of aluminum oxide is 6:1, adopts hot steam heating mixed solution to form hot mixed solution, and it is 0.15m that hot steam is introduced the water yield
3/ t flyash, the slip after sufficient reacting is squeezed into acid-resistant reacting kettle, and adding consumption is 0.56m
3the liquor alumini chloridi that/t flyash postorder obtains makes reacted hot mixed solution be cooled to 80 ℃, obtains wintercherry liquid.
Wintercherry liquid is squeezed into filter plant and carry out slag liquid and separate and obtain aluminum chloride initial soln and initial residue, use live steam condensed water with 0.65m
3the consumption of/t flyash and an effect secondary steam water of condensation are with 0.61m
3the consumption of/t flyash washs initial residue.Aluminum chloride initial soln is carried out to adsorption-edulcoration by D001 resin two post series connection ion exchange resin systems, and adsorbing saturated resin employing consumption is 0.161m
3the triple effect secondary steam water of condensation of/t flyash, consumption are 0.05m
3the quadruple effect water of condensation regeneration of/t flyash, obtains refined crystalline aluminium chloride liquid.
Refined crystalline aluminium chloride liquid is carried out to evaporative crystallization by four-effect evaporator system, wherein, 121 ℃, 104 ℃, 83 ℃, 65 ℃ of thermogrades, pressure gradient 0.095MPa, 0.046MPa ,-0.025MPa ,-0.070MPa.Form crystal aluminum chloride and live steam condensed water, an effect secondary steam water of condensation, two effect secondary steam water of condensation, triple effect secondary steam water of condensation and quadruple effect water of condensation.
The crystal aluminum chloride that evaporative crystallization is obtained is calcined 4.0h in 900 ℃ of High Temperature Furnaces Heating Apparatuss, obtains aluminum oxide and flue gas, and flue gas is 0.32m by consumption
3two effect secondary steam water of condensation and the consumption of/t flyash are 0.51m
3the triple effect secondary steam water of condensation of/t flyash absorbs, and the acid solution that is absorbed is emitted the absorption acid solution in absorption tower and acid storage tank, the acid-soluble step of returning, and the hydrochloric acid that supplementary a small amount of concentration is 30wt%, regulating acid concentration in mixed solution is 30wt%.The yield that calculates the aluminum oxide of embodiment 3 is 90%.
Embodiment 4
To in flyash according to 3.5m
3the ratio of/t flyash adds water and prepares original slurry, and entering magnetic separation system consumption is 0.8m
3the wash-down water of/t flyash rinses rich iron mortar get off, and rich iron mortar filters to obtain rich iron filter cake and Fu Tie filtrate, rich iron filtrate 0.8m wherein
3/ t flyash returns and continues to serve as wash-down water, also filters to obtain poor iron filter cake and poor iron filtrate through the poor iron mortar of magnetic separation, and poor iron filtrate is wherein with 2.52m
3the consumption of/t flyash returns joins original slip, and an effect secondary steam water of condensation is with 0.96m
3the consumption of/t flyash and two effect secondary steam water of condensation are respectively with 0.02m
3the consumption of/t flyash supplements the original slip of preparation.
Poor iron filter cake is placed in to acid-resistant reacting kettle, adding hydrochloric acid formation mixed solution to make acid concentration in mixed solution is 30wt%, in hydrochloric acid, in HCl and flyash, the mol ratio of aluminum oxide is 6:1, adopts hot steam heating mixed solution to form hot mixed solution, and it is 0.09m that hot steam is introduced the water yield
3/ t flyash, the slip after sufficient reacting is squeezed into acid-resistant reacting kettle, and adding consumption is 0.63m
3the liquor alumini chloridi that/t flyash postorder obtains makes reacted hot mixed solution be cooled to 85 ℃, obtains wintercherry liquid.
Wintercherry liquid is squeezed into filter plant and carry out slag liquid and separate and obtain aluminum chloride initial soln and initial residue, use live steam condensed water with 0.31m
3the consumption of/t flyash and an effect secondary steam water of condensation are with 0.45m
3the consumption of/t flyash washs initial residue.Aluminum chloride initial soln is carried out to adsorption-edulcoration resin model by JK008 resin two post series connection ion exchange resin systems temporarily cannot be provided, and may relate to cooperation unit's secure content, and adsorbing saturated resin employing consumption is 0.22m
3the triple effect secondary steam water of condensation of/t flyash, consumption are 0.04m
3the quadruple effect water of condensation regeneration of/t flyash, obtains refined crystalline aluminium chloride liquid.
Refined crystalline aluminium chloride liquid is carried out to evaporative crystallization by four-effect evaporator system, and wherein, thermograde is 117 ℃, 98 ℃, 79 ℃, 58 ℃, and pressure gradient is 0.092MPa, 0.043MPa ,-0.028MPa ,-0.075MPa.Form crystal aluminum chloride and live steam condensed water, an effect secondary steam water of condensation, two effect secondary steam water of condensation, triple effect secondary steam water of condensation and quadruple effect water of condensation.
The crystal aluminum chloride that evaporative crystallization is obtained is calcined 4.0h in 900 ℃ of High Temperature Furnaces Heating Apparatuss, obtains aluminum oxide and flue gas, and flue gas is 0.57m by consumption
3two effect secondary steam water of condensation and the consumption of/t flyash are 0.45m
3the triple effect secondary steam water of condensation of/t flyash absorbs, and the acid solution that is absorbed is emitted the absorption acid solution in absorption tower and acid storage tank, the acid-soluble step of returning, and it is 30wt% that the hydrochloric acid that supplementary a small amount of concentration is 30wt% regulates acid concentration in mixed solution.The yield that calculates the aluminum oxide of embodiment 4 is 89%.
Comparative example 1
To in flyash according to 3.0m
3the ratio of/t flyash adds water and prepares original slurry, and entering magnetic separation system consumption is 0.4m
3the wash-down water of/t flyash rinses rich iron mortar get off, and rich iron mortar filters to obtain rich iron filter cake and Fu Tie filtrate, also filters to obtain poor iron filter cake and poor iron filtrate through the poor iron mortar of magnetic separation.
Poor iron filter cake is placed in to acid-resistant reacting kettle, adding hydrochloric acid formation mixed solution to make acid concentration in mixed solution is 30wt%, in hydrochloric acid, in HCl and flyash, the mol ratio of aluminum oxide is 6:1, adopts hot steam heating mixed solution to form hot mixed solution, and it is 0.15m that hot steam is introduced the water yield
3/ t flyash, the slip after sufficient reacting is squeezed into acid-resistant reacting kettle, adds water to make reacted hot mixed solution be cooled to 95 ℃, obtains wintercherry liquid.
Wintercherry liquid is squeezed into filter plant and carry out slag liquid and separate and obtain aluminum chloride initial soln and initial residue, use consumption is 1.2m
3the initial residue of water washing of/t flyash.Aluminum chloride initial soln is carried out to adsorption-edulcoration by JK008 resin two post series connection ion exchange resin systems, and adsorbing saturated resin employing consumption is 0.15m
3the water reuse of/t flyash, obtains refined crystalline aluminium chloride liquid.
Refined crystalline aluminium chloride liquid is carried out to evaporative crystallization by four-effect evaporator system, and wherein, thermograde is 119 ℃, 98 ℃, 80 ℃, 59 ℃, and pressure gradient is 0.094MPa, 0.044MPa ,-0.026MPa ,-0.072MPa.Form crystal aluminum chloride and live steam condensed water, an effect secondary steam water of condensation, two effect secondary steam water of condensation, triple effect secondary steam water of condensation and quadruple effect water of condensation.
The crystal aluminum chloride that evaporative crystallization is obtained is calcined 4.0h in 900 ℃ of High Temperature Furnaces Heating Apparatuss, obtains aluminum oxide and flue gas, and flue gas is 1.05m by consumption
3the water of/t flyash absorbs, and the acid solution that is absorbed is emitted the absorption acid solution in absorption tower and acid storage tank, the acid-soluble step of returning, and it is 30wt% that the hydrochloric acid that supplementary a small amount of concentration is 30wt% regulates acid concentration in mixed solution.The yield that calculates the aluminum oxide of comparative example 1 is 89%.
Comparative example 2
To in flyash according to 2.5m
3the ratio of/t flyash adds water and prepares original slurry, enters magnetic separation system 0.3m
3the wash-down water of/t flyash rinses rich iron mortar get off, and rich iron mortar filters to obtain rich iron filter cake and Fu Tie filtrate, also filters to obtain poor iron filter cake and poor iron filtrate through the poor iron mortar of magnetic separation.
Poor iron filter cake is placed in to acid-resistant reacting kettle, and adding hydrochloric acid formation mixed solution to make acid concentration in mixed solution is 20wt%, and in hydrochloric acid, in HCl and flyash, the mol ratio of aluminum oxide is 4:1, adopts hot steam heating mixed solution to form hot mixed solution, and hot steam is introduced water yield 0.1m
3/ t flyash, the slip after sufficient reacting is squeezed into acid-resistant reacting kettle, and adding consumption is 0.41m
3/ t water of coal ash makes reacted hot mixed solution be cooled to 100 ℃, obtains wintercherry liquid.
Wintercherry liquid is squeezed into filter plant and carry out slag liquid and separate and obtain aluminum chloride initial soln and initial residue, use 1.0m
3the water consumption of/t flyash washs initial residue.Aluminum chloride initial soln is carried out to adsorption-edulcoration by two post series connection ion exchange resin systems of D001 resin, and adsorbing saturated resin employing consumption is 0.1m
3the water reuse of/t flyash, obtains refined crystalline aluminium chloride liquid.
Refined crystalline aluminium chloride liquid is carried out to evaporative crystallization by four-effect evaporator system, and wherein, thermograde is 120 ℃, 100 ℃, 80 ℃, 60 ℃, and pressure gradient is 0.095MPa, 0.045MPa ,-0.025MPa ,-0.072MPa.Form crystal aluminum chloride and live steam condensed water, an effect secondary steam water of condensation, two effect secondary steam water of condensation, triple effect secondary steam water of condensation and quadruple effect water of condensation.
The crystal aluminum chloride that evaporative crystallization is obtained is calcined 2.5h in 1000 ℃ of High Temperature Furnaces Heating Apparatuss, obtains aluminum oxide and flue gas, and flue gas is 1.5m by consumption
3the water of/t flyash absorbs, and acid solution is absorbed.The yield that calculates the aluminum oxide of comparative example 2 is 65%.
As can be seen from the above description, the above embodiments of the present invention have realized following technique effect:
The water of condensation that evaporative crystallization is obtained is produced each flow process of aluminum oxide for flyash acid system, effectively solved in prior art acid technological process water resources usage quantity large, waste serious problem; And, contrast by embodiment 1 and comparative example 2, embodiment 4 and comparative example 1 can be found out, in the time that the mol ratio of HCl in hydrochloric acid and aluminum oxide in flyash is identical, adopt the application's method basic identical with the yield of the aluminum oxide that adopts the method for prior art to obtain, as can be seen here, the application's method can't affect the use of yield and the processing unit of aluminum oxide on the recycle of water.
The foregoing is only the preferred embodiments of the present invention, be not limited to the present invention, for a person skilled in the art, the present invention can have various modifications and variations.Within the spirit and principles in the present invention all, any modification of doing, be equal to replacement, improvement etc., within all should being included in protection scope of the present invention.
Claims (16)
1. flyash acid system is produced a method for aluminum oxide, comprising:
Step S1, is mixed to get original slurry by flyash and solvent, and described original slurry is carried out to magnetic separation, filtration, obtains poor iron filter cake;
Step S2, carries out described poor iron filter cake acid-soluble, obtains wintercherry liquid;
Step S3, carries out the separation of slag liquid by described wintercherry liquid, obtains liquor alumini chloridi and residue;
Step S4, carries out resin absorption removal of impurities processing by described liquor alumini chloridi, obtains refined crystalline aluminium chloride liquid;
Step S5, carries out condensing crystal processing by described refined crystalline aluminium chloride liquid, obtains crystal aluminum chloride and water of condensation; And
Step S6, calcines described crystal aluminum chloride, obtains described aluminum oxide,
It is characterized in that, the solvent in described step S1 comprises the described water of condensation at least part of described step S5.
2. method according to claim 1, is characterized in that, described step S5 comprises:
Adopt four-effect evaporator system that described refined crystalline aluminium chloride liquid is carried out to evaporative crystallization processing, obtain crystal aluminum chloride and water of condensation, described water of condensation comprises live steam condensed water, an effect secondary steam water of condensation, two effect secondary steam water of condensation, triple effect secondary steam water of condensation, quadruple effect water of condensation.
3. method according to claim 2, is characterized in that, described step S1 comprises:
Step S11, is mixed to get original slurry by described flyash and solvent, and the amount ratio of described solvent and described flyash is 2.5～3m
3/ t flyash, the solvent in described step S11 comprises from the part one in described step S5 imitates secondary steam water of condensation and/or at least part of two effect secondary steam water of condensation, and the consumption of preferred described water of condensation is 0.6～1m
3/ t flyash, further preferably the consumption of a described effect secondary steam water of condensation is 0～0.95m
3/ t flyash, the consumption of described two effect secondary steam water of condensation is 0.05～0.65m
3/ t flyash;
Step S12, carries out magnetic separation to described original slurry, obtains rich iron mortar and poor iron mortar;
Step S13, filters described poor iron mortar, obtains described poor iron filter cake and poor iron filtrate.
4. method according to claim 3, it is characterized in that, described poor iron filtrate in described step S13 is returned to a part and the described flyash as described solvent in described step S11 and is mixed to form new original slurry, and the amount of preferably returning to the described poor iron filtrate of described step S11 is 1.5～2.5m
3/ t flyash.
5. method according to claim 3, is characterized in that, described step S12 comprises:
Steps A utilizes wash-down water to rinse described original slurry in magnetic separation system, obtains rich iron mortar and rinses disposed slurry;
Step B, filters described rich iron mortar, obtains rich iron filtrate and Fu Tie filter cake;
Step C, makes described rich iron filtrate return to described steps A and rinse described flushing disposed slurry or described original slurry together with described wash-down water;
Step D, repeating said steps A, B and C lower than 1.0wt%, obtain described poor iron mortar to Indian red content in described flushing disposed slurry.
6. method according to claim 5, is characterized in that, the consumption of described wash-down water is 0.3～0.7m
3/ t flyash.
7. method according to claim 2, is characterized in that, described step S2 comprises:
Step S21, is dissolved in described poor iron filter cake in acid solution, obtains mixed solution;
Step S22, adopts hot steam to heat described mixed solution, obtains hot mixed solution;
Step S23, adopts refrigerant that described hot mixed solution is cooled to 80～100 ℃, obtains described wintercherry liquid, and described refrigerant comprises the described liquor alumini chloridi of part.
8. method according to claim 7, is characterized in that, it is 0.1～0.15m that the hot steam in described step S22 is introduced the water yield
3/ t flyash, the consumption of described refrigerant is 0.3～0.6m
3/ t flyash.
9. method according to claim 7, it is characterized in that, acid solution in described step S21 is hydrochloric acid soln, and the concentration of hydrochloric acid described in described mixed solution is 20～30wt%, and in described hydrochloric acid, in HCl and described flyash, the mol ratio of aluminum oxide is 4:1～6:1.
10. method according to claim 2, is characterized in that, described step S3 comprises:
Step S31, carries out the separation of slag liquid by described wintercherry liquid, obtains aluminum chloride initial soln and initial residue;
Step S32, initial residue described in employing detergent washing, obtain described residue and elutriant, and described elutriant is mixed with described aluminum chloride initial soln, obtain described liquor alumini chloridi, described washing composition comprises the described water of condensation of part from described step S5, and preferred described part comprises at least part of described live steam condensed water and/or described one imitates secondary steam water of condensation at least partly from the water of condensation of step S5.
11. methods according to claim 10, is characterized in that, the consumption of described washing composition is 1.0～1.4m
3/ t flyash, the consumption of described live steam condensed water is 0.45～0.65m
3/ t flyash, the consumption of a described effect secondary steam water of condensation is 0.55～0.85m
3/ t flyash.
12. methods according to claim 2, is characterized in that, described step S4 comprises:
Step S41, carries out resin absorption removal of impurities processing by described liquor alumini chloridi, obtains described refined crystalline aluminium chloride liquid and saturated resin;
Step S42, use regenerated solvent to carry out wash-out to described saturated resin, obtain regenerating resin, described regenerated solvent comprises the described water of condensation of part from described step S5, and preferred described part comprises part described triple effect secondary steam water of condensation and at least part of described quadruple effect water of condensation from the water of condensation of described step S5.
13. methods according to claim 12, is characterized in that, the consumption of described regenerated solvent is 0.10～0.21m
3/ t flyash, the consumption of described triple effect secondary steam water of condensation is 0～0.20m
3/ t flyash, the consumption of described quadruple effect water of condensation is 0.05～0.15m
3/ t flyash.
14. methods according to claim 2, is characterized in that, described step S6 comprises:
Step S61, calcines described crystal aluminum chloride, obtains aluminum oxide and flue gas;
Step S62, adopts water to absorb described flue gas, and acid solution is absorbed;
Step S63, makes described absorption acid solution return to described step S2 and dissolves described poor iron filter cake.
15. methods according to claim 14, is characterized in that, in described step S62, the consumption of water used is 0.8～1.15m
3/ t flyash, and described water comprises described two effect secondary steam water of condensation, part described quadruple effect water of condensation and/or at least part of described triple effect secondary steam water of condensation of part from described step S5.
16. methods according to claim 15, is characterized in that, the consumption of described two effect secondary steam water of condensation is 0～0.55m
3/ t flyash, the consumption of described triple effect secondary steam water of condensation is 0.50～0.80m
3/ t flyash.
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| CN115784278A (en) * | 2022-12-06 | 2023-03-14 | 神华准能资源综合开发有限公司 | Method for utilizing water in process of preparing aluminum oxide from aluminum chloride |
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