GB2027618A - Creación de Inventos y Patentes con Inteligencia Artificial

GB2027618A – Process for the treatment of aluminium salt slags
– Google Patents

GB2027618A – Process for the treatment of aluminium salt slags
– Google Patents
Process for the treatment of aluminium salt slags

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Publication number
GB2027618A

GB2027618A
GB7924324A
GB7924324A
GB2027618A
GB 2027618 A
GB2027618 A
GB 2027618A
GB 7924324 A
GB7924324 A
GB 7924324A
GB 7924324 A
GB7924324 A
GB 7924324A
GB 2027618 A
GB2027618 A
GB 2027618A
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United Kingdom
Prior art keywords
flotation
aluminum
stage
collector
salt
Prior art date
1978-07-12
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1978-07-12
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1979-07-12
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1980-02-27

1979-07-12
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1980-02-27
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patent/GB2027618A/en

1982-09-29
Application granted
granted
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1982-09-29
Publication of GB2027618B
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patent/GB2027618B/en

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Classifications

B—PERFORMING OPERATIONS; TRANSPORTING

B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS

B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION

B03D1/00—Flotation

B03D1/001—Flotation agents

B03D1/004—Organic compounds

B03D1/01—Organic compounds containing nitrogen

B—PERFORMING OPERATIONS; TRANSPORTING

B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS

B03B9/00—General arrangement of separating plant, e.g. flow sheets

B03B9/04—General arrangement of separating plant, e.g. flow sheets specially adapted for furnace residues, smeltings, or foundry slags

B—PERFORMING OPERATIONS; TRANSPORTING

B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION

B03D1/00—Flotation

B03D1/001—Flotation agents

B03D1/002—Inorganic compounds

E—FIXED CONSTRUCTIONS

E04—BUILDING

E04H—BUILDINGS OR LIKE STRUCTURES FOR PARTICULAR PURPOSES; SWIMMING OR SPLASH BATHS OR POOLS; MASTS; FENCING; TENTS OR CANOPIES, IN GENERAL

E04H3/00—Buildings or groups of buildings for public or similar purposes; Institutions, e.g. infirmaries or prisons

E04H3/10—Buildings or groups of buildings for public or similar purposes; Institutions, e.g. infirmaries or prisons for meetings, entertainments, or sports

E04H3/12—Tribunes, grandstands or terraces for spectators

E04H3/126—Foldable, retractable or tiltable tribunes

B—PERFORMING OPERATIONS; TRANSPORTING

B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION

B03D2201/00—Specified effects produced by the flotation agents

B03D2201/02—Collectors

B—PERFORMING OPERATIONS; TRANSPORTING

B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION

B03D2203/00—Specified materials treated by the flotation agents; specified applications

B03D2203/02—Ores

B03D2203/04—Non-sulfide ores

Description

1 GB 2 027. 618 A 1
SPECIFICATION Process for the treatment of aluminum-salt slags
The present invention relates to a process for the treatment of aluminumsalt slags for the recovery of aluminum and a recyclable salt product.
In the production of aluminum bodies it is a common practice to utilize, as much as possible, aluminum scrap to reduce the qua i ntity of raw materials required. Such scrap normally is associated with a relatively high proportion of various impurities which must be removed before the scrap aluminum forms a useful melt. The scrap aluminum is treated in aluminum remelting plants, generally in a rotary furnace, to remove these impurities.
To assist in the removal of the impurities, the common practice is to add slag-forming salts to the10 scrap aluminum in the furnace.
One part of the salt mixture is added to two parts of the aluminum scrap in the smelting furnace. The salt mixture generally comprises 25 to 30% by weight potassium chloride, 65 to 70% by weight sodium chloride, 2% by weight calcium fluoride (CaF,) and traces of other chlorides, fluorides, sulfates 15 and bromides.
Aside from acting as slag formers, the additive also controls the rheology of the melt.
Because of the remelting of aluminum scrap, large quantities of salt slags are obtained which can be constituted of 4% to 8% by weight aluminum metal, 18% to 20% by weight potassium chloride, 45% to 50% by weight sodium chloride and 22% to 33% by weight of water- soluble components.
The disposal of these slags with other wastes creates serious ecological problems since it can 20 result in an increase in the salt concentration of ground water and, upon solubilization of the salts, an evolution of gases which are partially toxic and are noxious. The storage of these wastes in other ways, i.e. in subterranean conversion, has been found to be highly uneconomical. – Experiments have been carried out to treat aluminum salt slags to recover the aluminum and the salts.
For example, a solubilization process has been developed which involves high treatment cost and large energy expenditures. Other salt recovery processes, such as reverse osmosis, solubilization and freezing or chemical or thermal precipitation, have not proved to be practicable also because of their high energy costs and their environmental effects.
Efforts to carry out a separation by high voltage electrostatic precipitation techniques do not yield 30 the desired results.
The present invention seeks to provide an improved process for the recovery of aluminum and reusable salts from aluminum salt slags of the type produced in the remelting of aluminum scrap.
The present invention is based upon our discovery that aluminum salt slags contain a large number of mineral phases which, in large measure, are intergrown while the metallic aluminum is generally trapped somewhat less tightly in the mineral structure.
According to the invention, there is provided a process for the treatment of an aluminum-salt slag produced in the remelting of aluminum by the addition of salt to aluminum scrap, wherein the process comprises braking down the aluminum saft slag to an X., value of about 130 to 150 microns classifying the broken down product to recover therefrom a large-particle fraction consisting at least predominantly 40 of aluminum particles, and a fine-particle fraction; subjecting said fine- particle fraction to flotation in a flotation stage to which a cation active collector is added of the formula RO-(CH2)n -NH-(CH2)n -NH2 or RO-CH2)n -NH2 wherein R is a straight or branched chain saturated or unsaturated alkyl having 8 to 22 carbon atoms or mixtures thereof, and n is 1 to 5, or an organic or inorganic salt thereof, to recover an impurity-containing froth of low chloride level and a concentrate containing most of the 45 chlorides of the salts of the slag; Thus the metallic aluminum is converted into a form which facilitates its inorganic separation and which enables oxide, hydroxide, oxyhydrate and silicate components to be separated out from the slag collectively so that the sodium chloride and potassium chloride components of the slag can be recycled as slag-forming additives to the furnace.
More specifically, the slag may be initially comminuted by pressure and impact effect and rolled out to a thickness dl to 0.2 mm, the rolled product being then milled with pressure and impact milling to an X80 value of 130 to 150 microns.
This comminuted product is subjected to, for example, multi-stage particle-size separation or fractionation, i.e. classification, e.g. by sieving, air sifting or screening to recover a first fraction having a 55 particle size of eg 300 to 500 microns and consisting of coarse aluminum particles and a fine particle fraction with a particle size less than 300 to 200 microns (X,,6-value of 130 to 150 microns) which is subjected to foam flotation with cation-active coagulant or collecting agents which can be alkylether amines of the formula RO(CH2) -NH2 or alkylether polyalkylene diamine of the formula RO(CH2)n -NH-(CH,_)n -NH, and salts thereof with organic and inorganic acids, e.g. the acetate or 60 hydrochloride salts. R is a straight or branched chain saturated or unsaturated alkyl having 8 to 22 carbon atoms and mixtures thereof, while n can be 1 to 5, preferably 3. This collector may be used in an amount of 500 to 2500 grams per ton of flotation-feed solids, preferably 1000 to 1500 grams per ton.
Before this agent is added to the flotation stage, it is preferred to treat the flotation stage with a 2 GB 2 027 618 A 2 base, such as a metal hydroxide, preferably an alkaline-earth metal hydroxide such as C,,(OH)2 or Mg(OH)2, in an amount of 0.04 to 0.4 g per ton (of the fine fraction) to bring the pH to a value of 10 to 11. After separating the nonchloride component in the foam product from the cell residue, the pure potassium chloride/sodium chloride concentrate in the latter may be filtered and dried to form a salt concentrate which can be recycled to the flotation processor otherwise processed. The organic coagulating agent may be permitted to react with the flotation system for a period of 1 to 3 minutes.
An important aspect of the invention is the preparation of the slag to recover therefrom the largegrained aluminum particles with a particle size eg of 300 to 500 microns and a fine grained product with a particle size corresponding to an X., value of 130 to 150 microns in which the salt and the water soluble components are practically quantitatively present.
This may be achieved by the comminution process described previously, i.e. the passage of the pieces of slag through a roll mill with a gap width of say 0.5 mm and thereafter through a ball mill. The slag pieces may also be subjected to similar effects in a rod or pin mill, i.e. subjected to such a combination of pressure, fraction and impact, as to comminute the slag and simultaneously cause the aluminum particles to flatten and assume the large particle configuration which enables their recovery 15 in the manner described. Similar results may also be obtained with apug mill which subjects the slag pieces to a combination of pressure and shear forces.
The milling stages not only break up the complex slag particles and flatten the aluminum trapped in the slag, but also appear to mechanically induce a separation of these flattened aluminum particles from the grains of mineral matter produced by the comminution, these grains consisting predominantly 20 of the salts and watering soluble components of the slag.
The treatment converts the aluminum grain to platelets of 0.2 to 1.5 mm in thickness by the rolling and squeezing actions during the comminution so that these particles during air sifting, screening or sieving are easily recovered from the remainder of the particles.
The selective increase in the size of the aluminum components and transformation of the mineral matter to a fine particle component is thus an important feature since it can allow the simple mechanical separation steps of air sifting, sieving or screening to separate these two components.
It should be noted that during above comminution treatment of the brokenup slags by the fine roll mill, the oxides, hydroxides and silicates are formed into small platelets with the salts acting as binders, these platelets being more difficult to separate from the aluminum without the second comminution 30 step which is the milling operation, mentioned. previously and following the rolling.
The second milling step applies pressure, fraction and impact to the mass which have little effect upon the aluminum platelets but readily comminute the oxide, hydroxide and silicate platelets to the fine grain products mentioned previously.
The comminuted product, substantially freed from the aluminum platelets, can be subjected to 35 foam flotation in the described manner to recover 70 to 85% of the chlorides contained in the slag.
The removal of sodium chloride and potassium chloride is dependent upon the collector concentration which can be varied within a wide range.
The flotation process may be effected at the preferred pH range of 10 to 11, established as described above, and the impurities in the salt component, such as corundum (Al 20.) and spinels may 40 be removed in the froth product, i.e. the foam.
In the separation of the aluminum particles from the comminuted product by air sifting, we prefer to make use first of an air stream with a velocity of 0.4 to 0.8 meters per second and to then subject the separated coarse product by a second air sifting with an air velocity between 2 and 4.5 meters per second with a sifting-air loading of 1 to 2 kg of solids per cubic meter of air. The fines recovered in the 45 second sifting operation may be recycled to the comminution stage or to one of the comminution steps.
The coarse product obtained in the second air-sifting stage has an aluminum concentration of 94% by weight and represents a recovery of 50 to 70% of the aluminum of the slag.
The recovered aluminum in the large-size platelet form, can be smelted without further compaction.
The metallic aluminum may also be recovered by multistage sieving or screening. Since the aluminum salt slags from these continuous smelting processes differ in composition and mechanical characteristics (structure), the minerological composition of the particle sizes of the individual-minerals will differ materially with the slags of different furnace charges. With the multi-stage screening, an excellent aluminum separation can be obtained in spite of such variations.
The comminuted product may thus be passed through or onto sieves of different-size apertures, preferably ranging from 2 tp 0.3 mm.
The product retained on the 2 mm sieve generally is found to be 100% aluminum, the product retained on a 1 mm sieve being 90 to 05% pure aluminum, while the product retained on the 0.5 mm sieve is 50 to 90% pure aluminum. This last retained fraction can be recycled to the comminuting 60 process.
The sieve-sepa ration of aluminum will produce, depending upon the particle size of the aluminum, a product which may constitute 50 to 75% of the aluminum in the salt slag originally.
The fraction passing the 0.3 mm sieve can be subjected to flotation in the afore described manner.
When the foam flotation is carried out with a cation-active collector, a portion of the potassium 65 3 GB 2 027 618 A 3′ chloride is trapped therewith so that with increasing collector concentrations, there is a corresponding reduction in the I(C1 leve in the liquid phase.
To avoid this (since the highest level of the chlorides should be retained in the liquid which is separated from the foam in a one-stage process), the fines with a particle size smaller than 200 to 250 microns W,,,=1 30 to 150 microns) after the screening or air sifting may be subjected first to a direct M 5 flotation with a cation-active collector of the free fatty amine type or a salt with inorganic or organic acids of the formula R’-NI-12 or (R’-NH3)+.CH3 C05 or (R’ -NH3+.Cl- wherein RI is a straight or branched chain saturated or unsaturated alkyl of 8 to 22 carbon atoms or a mixture thereof. After separation of the foam product the liquor is recycled to the flotation process and 10 the cell residue is subjected to further flotation.
The use of this direct KCI flotation approach allows a combination of direct KCI flotation with indirect Na Cl flotation using two distinct collectors whose selectivities- can be appropriately chosen so that the cell residue of the first stage can be separated from the flotation liquor before the next stage.
With the combined flotation process, i.e. tle. the two stage flotation described above, 70 to 80% by 1.5 weight of the total salts contained in the slag can be recovered and the deposited wastes can contain 20% by weight or less water-soluble chlorides.
To minimize the requirement of fresh liquor in the flotation process it is advantageous if froth be separated from the flotation and if the cell residues may be filtered and the filtered liquor is recycled to the corresponding flotation stage.
In spite of this recycling, flotation operations continuously lose liquor so that in each flotation stage fresh water must be introduced. This can be utilized for further reduction in the cloricle content of the waste by treating the filtered substances from the first or second stage filtration to leach additional chlorides therefrom and by utilizing the chloride-containing water as the makeup water for the respective flotation stages. This addition step has been found to reduce the chloride content of the waste 25 significantly below 20% by weight.
The invention will now be described in greater detail, by way of example, with reference to the drawings, in which:
Figure 1 is a flow diagram of the process of the present invention using a single stage flotation; Figure 2 is a flow diagram representing the process with. a two stage flotation; Figure 3 is a diagram corresponding to the process of Figure 1 but providing details of a specific example of the invention; and Figure 4 represents the process detailed in Figure 2 but with the values obtained in the specific examples, corresponding to the tables of Figure 3.
Figures 1 and 2 show flow diagrams forthe treatment of aluminum salt slags according to the 35 present invention. In the detailed examples the aluminum salt slag is understood to be available in pieces having maximum size of 20 cm and consisting essentially of 45 to 50% by weight sodium chloride, 17 to 20% by weight potassium chloride, 4 to 8.5% by weight aluminum and 20 to 25% by weight other minerals as described above.
In both processes, the mass of slag pieces, represented as the aluminum salt slag at 10, is 40 subjected to multistage comminution and ultimate milling at 20, using jaw, impact or hammer mills for the initial comminution with the final or further comminution being effected in a roll mill followed by a ball ml1J_ or with the pin or rod mill or pug mill as described previously until the comminuted product at the end of stage 20 has an X80 value of 130 to 150 microns. The comminuted product thus contains the aluminum in the form of thin platelets while the salts and impure minerals, corundum, spinels, other oxides, hydroxides and silicates, are separable therefrom by air sifting or screening.
The milled product of the slag comminuted in this manner can have the sieve analysis given in Table 1 below in which the H20 insoluble residue corresponds to the sum of the impure minerals in the form of oxides, hydroxides, silicates and the like.
4 GB 2 027 618 A 4.
Table 1 (All % given by weight) Fraction Mass % NaCI% KCI% Aluminum % H20 Insoluble % + 250 gm 6.4.3 32.7 12.4 18.7 36.2 +200 gm 3.17 34.7 17.8 6.5 41.0 + 150 lim 7.24 42.4 20.0 6.0 32.6 + 100 tim 11.116 49.8 20.2 4.1 25.9 —100 gm 72.00 51.3 18.6 3.5 26.6 Approximate 48.8 18.5 4.8 28.11 Composition In the next stage 30 the aluminum is mechanically separated from the remainder of the slag. As described, this can be done by multistage sieving or multistage air sifting.
In the multistage sieving step, the pure aluminum with a particle size greater than 500 microns is pure aluminum and is obtained as the aluminum concentrate 40, not having passed a corresponding sieve. The slag fraction of a particle size of 500 to 200 microns is recycled at 31 to the milling stage. In the multistage air sifting, the first sifting is carried out with an air velocity of 0.4 to 0.8 m per second. The fine product is supplied at 32 to the foam flotation stage. The coarse product is subjected to air sifting in a second stage with air at a velocity of 2.5 to 0.5 m per second from the coarse fraction of which 96% of aluminum is obtained as the aluminum concentrate 40. Further purification of the aluminum can be carried out in after-sifting stages not shown. The fine component of the second air sifting stage is recycled to the comminution step 20 as represented at 3 1.
When the aluminium is not present in the slag with a particle size below 500 microns, at least 65% of the metallic aluminum can be recovered in this manner.
5;r FIGS. 1 and 3 show the process of the present invention utilizing a combined NaCI-KCI flotation, 15 i.e. a single stage flotation. To the flotation stage 50, a collector of the aforedescribed composition is added as represinted at 51 preferably in an amount of 1500 g per ton of the salt treated. This collector is added in two to five aliquots during the flotation stage with the residence time of the collector being 1 to 3 minutes for each addition. The pH of the flotation stage is adjusted by the addition of bases, preferably calcium hydroxide, as represented at 52, to a pH value of 10 to 11.
The resulting froth of foam contains the impure minerals which contaminate the salt and this foam product can be recovered at 53 and subjected to after cleaning at 60 with the recovered liquor at 61 being recycled to the flotation stage. The froth residue is subjected to dewatering and contact with fresh water at 70, the fresh water constituting the makeup water for the flotation process and leaching residual salt from the foam product by being cycled to the flotation stage at 71. The waste recovered at 25 80 is nontoxic and can be disposed of with household wastes.
The cell residue of the flotation stage is filtered off with the filtrate being recycled to the flotation stage 91, this filtration constituting the dewatering represented at 90 of the salt concentrate. The salt concentrate is supplied to a dryer 92 and the dry salt concentrate is recovered at 93 for reuse in the slag-forming process.
Table 2 below shows the composition of the waste and the salt concentrate derived from the flotation-separated product.
Flotat. % of NaCi Table 2 (All % by weight) KCI Alum.Metal H20 Insol.. Residue Product Total Content % of Content % of Cont. % of Cont. % of % Total % Total % Total % Total Waste 42.6 33.5 23.4 13.46 42.55 2.09 67.93 50.7 90.1, Salt Concentr. 57.4 81.6 76.6 13.50 57.45 0.73 32.07 4.2 9.9 100.0 61.1t 100.0 13.49 100.00 1.31 100.00 24.0 100.0 z GB 2 027 618 A 5 The foregoing flotation results show the metal balance of a single stage flotation process using an alkyl ether amino acetate MG-98A of Ashland Chemical Co., Mi, nneapolis, Minnesota, at a pH 10.4 in an amount of 1500 g per ton added in four aliquots, the pH having been adjusted with calcium hydroxide and the waste having not been after cleaned or treated with fresh water. The salt concentrate contained 95.1% by weight chloride.
In a single stage flotation process as thus described, the salt concentrate has a chloride content of above 95% with a recovery of 70% of the chlorides from the comminuted product from which the aluminium has_previously been separated, the waste containing up to 25% chloride, in extreme cases, 30% chloride after fresh water treatment.
Better flotation results are obtained when the collector is an alkyl ether diamine, especially Hoe F 10 2468 or Hoe F 2640 of Farbwerke Hoechst AG, Frankfurt, Germany. This collector is added after adjustment of the pH to 10.5 with calcium hydroxide in an amount of 1000 g per ton in four aliquots with two minutes between each addition.
Table 3 shows balance for the aluminum as well as the chlorides utilizing the process. The salt 15 concentrate contains about 99% by weight of the chlorides.
Table 3 (All % by weight) Product Amt. I Content 94.0 0.5 6.0 8.451 Aluminum % of Total 66.7 2.8 30.5 1100.0- Content 3.6 74.0 24.0′ 66.0, 47.9 NaCI % of Total 0.5 71.8 21.5 6.2 100.0, Content 1.5 25.0 12.0 34.0′ 18.4 KCl % of Total 0.5 63.2 28.0′ 8.3 100.0 H20 Insol.
Content 1.0 0.5 58.0 25.4 Residue % of Total Aluminum Concentrate Salt Concentrate Waste Recycled Liquor 6.0 46.5 43.0′ 4.5 -0.3 0.9 98.8 1 TV, 100,0, FIGS. 2 and 4 show an embodiment of the invention in which the fines of the first sifting stage (FIG. 4) or the product 32 passing the screen of the last screening stage (FIG. 2) are subjected first to a potassium chloride flotation at 50a. Abut 30 to 100 g per ton of the collector is added to this flotation stage at 5 1 a and is permitted to act for about two minutes. The foam flotation is carried out at practically neutral conditions with a pH of 6 to 8 and the froth is filtered off at 50b with the liquor being recycled to the KCI flotation as represented at 9 1 a.
This froth contains 70 to 80% by weight KCI, 15 to 20% NaCl, up to 1 % by weight aluminum and 4 to 14% impurities. This froth can be subjected to after cleaning and ultimately is dewatered at 90a to recover the potassium chloride concentrate at 90b.
The cell residue of this flotation stage is clewatered at 90c and,the liquor recycled at 90dto the flotation stage. The clewatered cell residue can be thermally treated in a dryer at 300″C to decompose the KCI collector before this product is introduced into the sodium chloride flotation stage 50d to ensure that the KCI collector and the NaCl collector will not interfere with one another or detrimentally affect each other’s selectivity. The cell residue of the KCI flotation with a second collector, used in an amount 30 of about 1500 g per ton, is subjected to the flotation subsequent stage having been set at a pH 10.5 with calcium hydroxide. This collector is added at four aliquots spaced apart by two minutes each. The foam product is filtered off at 90e with the liquor being recycled at 91 c to the flotation stage.
The flotation results of this two-stage process are represented in Table 4.
6 GB 2 027 618 A 6 Table 4
Flotat. Product KCl Concentrate NaCl Concentrate Waste % of Tota 1 19.2 38.5 42.3 100.0 Cont.
19.6 94.1 30.5 52.9 NaCl KCI Aluminum % of Total 7.2 68.4 24.4 Cont. 1 i1 72.1 4.0 6.6 18.11 % of Total 76.2 8.3 15.5 100.0 Cont.
0.9 0.4 7.6 3.0 % of Total 5.6 5.6 88.8 100.0 H20 Insol., Residue Cont. % of % Total 7.3 1.8 55.1 25.4 5.5 2.8 91.7 100.0 100.0 The foam product of the NaCI stage, which contains the impurities, can be aftercleaned as often as is desirable. the flotation results from a two- stage foam flotation with a simple one-stage aftercleaning are shown in Table 5.
Table 5
Flotat. Product KCl Concentrate NaCl Concentrate -Middle Product Waste % of Total NaC 1 KCI Cont. i %of Cont.! %of % Total % Total 19.6 7.2 72.11 76.2 94.11 68.4 4.0 8.3 62.9 13.2 22.2 13.8 18.9 11.2 1.0 1.7 52.9 100.0 18.1, 1 100.0 Cont.
0.9 0.9 1.7 9.6 3.6 H20 Aluminum Insol.! Residue % of Total % of Tota 1 5.6 5.6 5.6 83.2 100.0 Cont. % 7.3 1.8 13.2 69.9 25.4 With a single cleaning of the waste, i.e. the foam product of the NaCI flotation, there is a 19.2 38.5 11.1 31.2 5.5 2.8 5.9 85.8 loo.,0 reduction of the chloride content of more than 50% from the chloride level above 35% to a maximum of 20% chloride.
In these tests the 10 to 15% liquor loss during the filtration is made up by the addition of fresh water which is added to and then filtered from the waste, before being admixed to the sodium chloride 10 flotation stage. The chloride content in the waste can thus be lowered to 15 to 20%, usually 15 to 17%. For the tests of example 4, the KCI flotation stage were carried out at neutral pH with primary fatty amine hydrochlorides as marketed under the name Armeen HTD by the firm Armour Hess. This collector is added in an amount of 100 g per ton and removes the KCI. The aftercleaning of the KCI concentrate is not reflected in Table 4.
The KCI concentrate contains 91.7% chloride. The filtered cell residue of the KCI stage is dispersed in a fresh liquor and brought to a pH of 10.5 with calcium hydroxide. The collector is here the water soluble preparation Hoe F 2468, namely, Hoe F 2640, which is added in an amount of 1500 g per ton in four aliquots with two minutes between the additions. The sodium chloride concentrate contains 98.4% chloride. The chloride recovery of the two stages is on the average of 80%. In the case of Table 4 the 20 waste was not aftercleaned nor was it washed or treated with fresh water.
The concentrations and recoveries in the sa It concentrate are the same as those given in Table 4 but the chloride content of the waste can be reduced by the aftercleaning. 13% chloride can be recycled as an intermediate to the flotation stage or aftercleaned in further stages. The number of aftercleaning stages is, of course, unlimited.
7 GB 2 027 618 A 7 In the material balance represented by Tables 4 and 5, the afterwashing of the waste, namely, the froth of the sodium chloride flotation is not reflected. The cell residue of the sodium chloride flotation, rich in sodium chloride, is filtered off and the liquor recycled to the sodium chloride flotation.
The filter cake can be dried and mixed with dried potassium chloride concentrate at 93a. This mixture can serve as salt additive for the flux formation during the remelting of aluminum scrap.
FIGS. 3 and 4 show comparative results of the one- stage and two-stage processes (see also Table 5).
In the two-stage flotation of the above-described type, cationic active collectors of the free fatty amine class are used for the first stage so that the major part of the KCI is removed in the froth.
The subsequent treatment of the cell residue is effected in a manner similar or identical to the 10 flotation of the single stage process, i.e. after the addition of a base to bring the flotation system to a pH between 10 and 11 prior to the additon of the cation active collector for this stage. When this flotation is effected subsequent to a KCI flotation, i.e. is an indirect NaCl flotation, the preferred collector is an alkyl ether polyalkylene diamine.
Investigations have shown that a further simplification of the process can be achieved by treating 15 the fines resulting from screening or sifting and of a particle size with an X-80 value of 130 to 150 microns, initially by direct KCI flotation with a cation active collector of the alkyl ether polyalkylene monoamine type having the formula R-O-(CH2)n-NH or its salts with organic or inorganic acids such as its acetate salt [R-O(CH2) i–NH3]+.CH3COo- or its hydrochloride salt [R-O(CH2) d-NH3]+.Cl- at a concentration of 200 to 100 g of the collector per ton of solids. R is a straight or branched chain 20 saturated or unsaturated alkyl having 6 to 12 carbon atoms or a mixture thereof and n is 1 to 5, preferably 3. Preferably, prior to the addition of this collector to the direct KCI flotation stage, the latter is brought to a pH of 7 to 9, advantageously by the addition of a base such as calcium hydroxide.
The KCI is recovered in the froth, i.e. as a foam product and after separation and, if desired, one or more aftercleaning steps, the foam product, usually after thickening, is subjected to flotation at the pH 25 of 10 to 11 described earlier. The liquor decanted from the thickener is recycled to the KCI flotation stage.
This latter procedure can be carried out without the dewatering of the waste of the KCI flotation prior to the treatment of the cell residue byindirect NaCl flotation. This is because the alkyl ether polyalkylene monoamine does not interfere with the selectivity of the alkyl ether polyalkylene diamine in 30 the NaCl flotation stage. The elimination of the clewatering and drying of the KCI flotation cell residue results in a significant simplification and hence a major reduction in cost.

Claims (17)

1. A process for the treatment of an aluminum-salt slag produced in the remelting of aluminum by the addition of salt to aluminum scrap, wherein the process comprises braking down the aluminum salt 35 slag to an X80 value of about 130 to 150 microns classifying the broken down product to recover therefrom a large-particle fraction consisting at least predominantly of aluminum particles, and a fine particle fraction; subjecting said fine-particle fraction to flotation in a flotation stage to which a cation active collector is added of the formula RO-7(CH2)n -NH-(CH2)n -NH2 or RO- CHA, -NH2 wherein R is a straight or branched chain saturated or unsaturated alkyl having 8 to 22 carbon atoms or mixtures 40 thereof, and n is 1 to 5, or an organic or inorganic salt thereof, to recover an impurity-containing froth of low chloride level and a concentrate containing most of the chlorides of the salts of the slag.

2. A process as claimed in claim 1, wherein prior to the addition of the cation active collector, a base is added to the flotation stage to bring the pH of the flotation stage to a pH value between 10 and 11.

3. A process as claimed in claim 2, wherein the base is added in an amount between 0.04 to 0.4 g of base per ton of material subjected to flotation.

4. A process as claimed in any one of claims 1 to 3, wherein the braking down of the aluminum salt-slag is undertaken in two stages by first comminuting the slag with pressure and impact and rolling the comminuted product to a thickness of about 0.2 mm to about 1 mm and second milling the rolled 50 product to an X80 value of about 130 to 150 means.

5. A process as claimed in any one of claims 1 to 4 wherein the flotation liquor from the flotation stage is recirculated.

6. A process as claimed in any one of claims 1 to 5, wherein the concentrate from the flotation stage is thereafter dewatered.

7. A process as claimed in any one of claims 1 to 6, wherein the classification of the broken down product is carried out in a plurality of stages.

8. A process as claimed in claim 4 wherein the classification of the milled product is carried out by multistage screening on screens having opening sizes from 2 to 0.3 mm, the fine fraction passing the 0.3 mm screen, the aluminum being recovered from screens retaining a particle size upwards of 0.5 60 mm, and a fraction having a particle size range between 0.5 and 0.2 mm being recycled to the milling step.

9. A process as claimed in claim 4, wherein the classification of the milled product is carried out first in a zigzag air stream with a velocity of 0.5 to 0.8 m per second’to recover a coarse fraction,-said 8 GB 2 027 618 A 8 coarse fraction being subjected to a second air sifting with an air speed of 2 to 4.5 m per second with each air sifting being effected with a solids charge of 1 to 2 kg per cubic meter of air, fines from the second sifting being recycled to the milling step while fines from the first sifting form the fine fraction, a coarse component of the second sifting being recovered as an aluminum concentrate.

10. A process as claimed in any one of claims 1 to 9 wherein the fine particle fraction from the 5 classification is subjected between the classification and flotation steps’to direct KCI flotation with a cation active collector selected from the group which consists of RI-NH2 or a hydrochloride or acetate salt thereof, R’ being a straight or branched chain saturated or unsaturated alkyl having 8 to 22 carbon atoms or a mixture thereof, thereby producing a froth and a cell residue, the cell residue being thereafter 1c) processed in the following flotation instep.

11. A process as claimed in any one of claims 1 to 10 wherein the flotation yields a froth, and separation of the froth, forming a cell residue by filtration, thereby recovering a liquor, and recycling said liquor to the flotation from which is was derived is carried out.

12. A process as claimed in claim 11, wherein the froth is washed with fresh water and the water with which the froth was washed is fed to the respective flotation as makeup water for loss of liquor 15 therefrom.

13. A process as claimed in any one of claims 1 to 12, wherein the collector is added in an amount of 500 to 2500 g per ton of solids in the flotation stage.

14. A process as claimed in claim 10, wherein the collector added in the first flotation stage is present in an amount of substantially 50 to 100 g per ton of the solids therein while the collector in the 20 second flotation stage is added in an amount of 1000 to 1500 g per ton of the solids treated therein.

15. A process as claimed in claim 1, 2, or 3, wherein the fine particle fraction from the classification step is subjected, prior to the flotation step, to a direct KCI flotation with a cation active collector having the formula RII 0-(CH2n’ -NH2 or an acetate or hydrochloride thereof in a collector concentration of 200 to 1000 g of the collector per ton of solids in the KCI flotation stage, RII being a straight or branched chain saturated or unsaturated alkyl of 6 to 12 carbon atoms or mixtures thereof and n’ being 1 to 5, the KCI flotation system being brought to a pH of 7 to 9 prior to the addition of the collector thereto, thereby producing a froth containing KCI.

16. A process as claimed in claim 15 wherein the froth is separated from a cell residue which is’ subjected to the following flotation step.

17. A process for the treatment of aluminum salt slag substantially as described herein with reference to the drawings.
1 () Printed for Her Majesty’s Stationery Office by the Courier Press, Leamington Spa, 1980. Published by the Patent Office, 25 Southampton Buildings, London, WC2A 1 AY, from which copies may be obtained.

GB7924324A
1978-07-12
1979-07-12
Process for the treatment of aluminium salt slags

Expired

GB2027618B
(en)

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DE2830574C2
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1978-07-12
1978-07-12

Process for processing aluminum salt slag

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1980-02-27

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1978-07-12
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Process for the treatment of aluminium salt slags

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1978

1978-07-12
DE
DE2830574A
patent/DE2830574C2/en
not_active
Expired

1979

1979-07-02
US
US06/055,189
patent/US4275847A/en
not_active
Expired – Lifetime

1979-07-05
CH
CH6276/79A
patent/CH647262A5/en
not_active
IP Right Cessation

1979-07-10
LU
LU81483A
patent/LU81483A1/en
unknown

1979-07-11
IT
IT7924279A
patent/IT1122138B/en
active

1979-07-11
DK
DK291979A
patent/DK291979A/en
not_active
Application Discontinuation

1979-07-11
FR
FR7918517A
patent/FR2430981A1/en
active
Granted

1979-07-11
JP
JP8696079A
patent/JPS5524990A/en
active
Granted

1979-07-11
SE
SE7906048A
patent/SE436397B/en
not_active
IP Right Cessation

1979-07-11
ES
ES482427A
patent/ES482427A1/en
not_active
Expired

1979-07-11
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AT0483879A
patent/AT374378B/en
active

1979-07-11
NO
NO792305A
patent/NO152978C/en
unknown

1979-07-12
NL
NL7905466A
patent/NL7905466A/en
not_active
Application Discontinuation

1979-07-12
BE
BE2/57949A
patent/BE877646A/en
not_active
IP Right Cessation

1979-07-12
GB
GB7924324A
patent/GB2027618B/en
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IT1122138B
(en)

1986-04-23

ES482427A1
(en)

1980-04-01

FR2430981A1
(en)

1980-02-08

NL7905466A
(en)

1980-01-15

NO152978C
(en)

1985-12-27

JPS5524990A
(en)

1980-02-22

LU81483A1
(en)

1979-10-31

CH647262A5
(en)

1985-01-15

AT374378B
(en)

1984-04-10

FR2430981B1
(en)

1984-02-17

SE7906048L
(en)

1980-01-13

NO792305L
(en)

1980-01-15

IT7924279D0
(en)

1979-07-11

JPS6260450B2
(en)

1987-12-16

DE2830574C2
(en)

1982-05-19

GB2027618B
(en)

1982-09-29

DK291979A
(en)

1980-01-13

BE877646A
(en)

1979-11-05

ATA483879A
(en)

1983-09-15

CA1129656A
(en)

1982-08-17

SE436397B
(en)

1984-12-10

NO152978B
(en)

1985-09-16

DE2830574A1
(en)

1980-01-31

US4275847A
(en)

1981-06-30

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