US1494029A - Process of separating the constituents of mineral silicates - Google Patents
Process of separating the constituents of mineral silicates Download PDFInfo
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- US1494029A US1494029A US561704A US56170422A US1494029A US 1494029 A US1494029 A US 1494029A US 561704 A US561704 A US 561704A US 56170422 A US56170422 A US 56170422A US 1494029 A US1494029 A US 1494029A
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- potassium
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- aluminum
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- 238000000034 method Methods 0.000 title description 14
- 239000000470 constituent Substances 0.000 title description 13
- 229910052500 inorganic mineral Inorganic materials 0.000 title description 11
- 239000011707 mineral Substances 0.000 title description 11
- 150000004760 silicates Chemical class 0.000 title description 10
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 41
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 36
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 18
- 229910052700 potassium Inorganic materials 0.000 description 18
- 239000011591 potassium Substances 0.000 description 18
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 17
- 239000000243 solution Substances 0.000 description 16
- 235000011118 potassium hydroxide Nutrition 0.000 description 13
- 239000002253 acid Substances 0.000 description 11
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 10
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 10
- 229940037003 alum Drugs 0.000 description 10
- 229910052782 aluminium Inorganic materials 0.000 description 10
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 10
- 235000010755 mineral Nutrition 0.000 description 10
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Substances [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 10
- 239000000047 product Substances 0.000 description 10
- 229910002092 carbon dioxide Inorganic materials 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 7
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 6
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 6
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 6
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 6
- 238000002419 base digestion Methods 0.000 description 6
- 239000000377 silicon dioxide Substances 0.000 description 6
- 239000001117 sulphuric acid Substances 0.000 description 6
- 235000011149 sulphuric acid Nutrition 0.000 description 6
- HLLSOEKIMZEGFV-UHFFFAOYSA-N 4-(dibutylsulfamoyl)benzoic acid Chemical compound CCCCN(CCCC)S(=O)(=O)C1=CC=C(C(O)=O)C=C1 HLLSOEKIMZEGFV-UHFFFAOYSA-N 0.000 description 5
- 239000004111 Potassium silicate Substances 0.000 description 5
- 239000001569 carbon dioxide Substances 0.000 description 5
- BUACSMWVFUNQET-UHFFFAOYSA-H dialuminum;trisulfate;hydrate Chemical compound O.[Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O BUACSMWVFUNQET-UHFFFAOYSA-H 0.000 description 5
- 230000029087 digestion Effects 0.000 description 5
- 238000001914 filtration Methods 0.000 description 5
- 239000007789 gas Substances 0.000 description 5
- 229910052742 iron Inorganic materials 0.000 description 5
- 229910052913 potassium silicate Inorganic materials 0.000 description 5
- NNHHDJVEYQHLHG-UHFFFAOYSA-N potassium silicate Chemical compound [K+].[K+].[O-][Si]([O-])=O NNHHDJVEYQHLHG-UHFFFAOYSA-N 0.000 description 5
- 235000019353 potassium silicate Nutrition 0.000 description 5
- 229940074415 potassium silicate Drugs 0.000 description 5
- KVOIJEARBNBHHP-UHFFFAOYSA-N potassium;oxido(oxo)alumane Chemical compound [K+].[O-][Al]=O KVOIJEARBNBHHP-UHFFFAOYSA-N 0.000 description 5
- 150000003839 salts Chemical class 0.000 description 5
- SXQXMCWCWVCFPC-UHFFFAOYSA-N aluminum;potassium;dioxido(oxo)silane Chemical compound [Al+3].[K+].[O-][Si]([O-])=O.[O-][Si]([O-])=O SXQXMCWCWVCFPC-UHFFFAOYSA-N 0.000 description 4
- 238000007865 diluting Methods 0.000 description 4
- 239000010433 feldspar Substances 0.000 description 4
- 229910000027 potassium carbonate Inorganic materials 0.000 description 4
- 235000011181 potassium carbonates Nutrition 0.000 description 4
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 3
- 150000004645 aluminates Chemical class 0.000 description 3
- 150000001875 compounds Chemical class 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- AZDRQVAHHNSJOQ-UHFFFAOYSA-N alumane Chemical class [AlH3] AZDRQVAHHNSJOQ-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000001354 calcination Methods 0.000 description 2
- 150000004649 carbonic acid derivatives Chemical class 0.000 description 2
- 239000003518 caustics Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical compound C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 2
- 229940072033 potash Drugs 0.000 description 2
- 235000015320 potassium carbonate Nutrition 0.000 description 2
- 229910052710 silicon Inorganic materials 0.000 description 2
- 239000010703 silicon Substances 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 239000004117 Lignosulphonate Substances 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- YKTSYUJCYHOUJP-UHFFFAOYSA-N [O--].[Al+3].[Al+3].[O-][Si]([O-])([O-])[O-] Chemical compound [O--].[Al+3].[Al+3].[O-][Si]([O-])([O-])[O-] YKTSYUJCYHOUJP-UHFFFAOYSA-N 0.000 description 1
- 238000000184 acid digestion Methods 0.000 description 1
- 238000010306 acid treatment Methods 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 229910052910 alkali metal silicate Inorganic materials 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000009993 causticizing Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- OYFJQPXVCSSHAI-QFPUQLAESA-N enalapril maleate Chemical compound OC(=O)\C=C/C(O)=O.C([C@@H](C(=O)OCC)N[C@@H](C)C(=O)N1[C@@H](CCC1)C(O)=O)CC1=CC=CC=C1 OYFJQPXVCSSHAI-QFPUQLAESA-N 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 239000011736 potassium bicarbonate Substances 0.000 description 1
- 235000015497 potassium bicarbonate Nutrition 0.000 description 1
- 229910000028 potassium bicarbonate Inorganic materials 0.000 description 1
- TYJJADVDDVDEDZ-UHFFFAOYSA-M potassium hydrogencarbonate Chemical compound [K+].OC([O-])=O TYJJADVDDVDEDZ-UHFFFAOYSA-M 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000009877 rendering Methods 0.000 description 1
- 239000012047 saturated solution Substances 0.000 description 1
- RMAQACBXLXPBSY-UHFFFAOYSA-N silicic acid Chemical compound O[Si](O)(O)O RMAQACBXLXPBSY-UHFFFAOYSA-N 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 230000002277 temperature effect Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D7/00—Carbonates of sodium, potassium or alkali metals in general
Definitions
- Our invention relates to processes for .separating the constituents of mineral silicates, and'particularly to processes for eX- tracting the potassium and other values from potash feldspar.
- This invention relates to improvements in a process of this general character disclosed in our pending application for U. S. Letters Patent, Serial No. 407,724.
- lVe dilute the alkali digestion products with from one (l) to four (4) times their volume of water and then carbonate themixture with carbon dioxide, maintaining a pressure of about 22 inches above atmospheric pressure, the temperature being maintained at substantially room temperature ,by f
- vWe convert only a part of the potassium ,carbonates thus obtained into sales products and the balance We causticize in order to obtain caustic potash for reuse in further digestion operations.
- the balance of the carbonate solution is concentrated to a 10 percent solution which is suitable for a causticizing operation withv lime to produce caustic potash for reuse andcalcium Acarbonate for sale.
- the acid digestion products are diluted with Water and then the saine repeatedly filtered in an acid proof ilter and Washed, the Wash Water utilized being about 2.2 gallons per lb. of ore digested.
- the aluminum salts in solution are l'ractionally crystallized, producing as a first. fraction practically pure alum containing only traces of iron, the successive fractions containing proportionately more iron and less alum and, of course, more aluminum sulphate.
- the alum is represented by the formula K2SO4A12(SO4)3.24H2O and the reason for its presence lies in the fact that there is Jformed in the autoclave a Water insoluble but acid decomposable silica containing KZO and the latter will not appear i'n the carbonate liquors, but in the residue of alumina and silica, there to be decomposed by the sulphuric acid treatment and thence to follow the aluminum.
- the silica is dried of its absorbed and adsorbed Water and then cleansed from impurities by treatment With hot concentrated sulphuric acid for one or two hours and then ⁇ filtered and Washed free of acid.
- the steps of recovering the potassium Value consisting in, first, converting the silicate into potassium sil-icate and aluminate by means of a solution of substantially ninety per cent (90%) caustic potash; and then recovering the potassium by passing carbonio acid gas, in the cold and under pressure additional to that normally incident to carbonation, through the potassium silicate and aluminate solution.
Description
May il@ is. w. SCOFIELD ET AL' PROCESSOF SEPARATING THE CONSTITUENTS OF MINERAL -SILICATES Filed May 1'7 5.5. 5.2.5.5 Gbs :E565 ...Eri
CAB
Patented May (i3, llQl.
' narran sraras SHERMAN W. SCOFIELD AND JOHN-2B. LA RUE, OFVCLEVELAND, OHO; SAID iA RUE parlar oratori.
ASSIGNOR TO SAID SCOFELD.
EROCESS 0F SEPRATING THE CONSTITUENTS MNERAL SILSCCATES.
Application filed May 17,
To all 'who/m t 'may concern.'
Be it known that we, SHERMAN W. SCO- rtELD and JOHN B. LA RUE, citizens of the United States, residents of Cleveland, county of Cuyahoga, and State of Chio, have invented new and useful .Improvements in Processes of Separating the Constituents of Mineral Silicates, of which the following is a specification, the principle of the invention being herein explained andthe best mode in which we have contemplated apply-- ing that principle, so as togdistinguish it from other' inventions.
Our invention relates to processes for .separating the constituents of mineral silicates, and'particularly to processes for eX- tracting the potassium and other values from potash feldspar. This invention relates to improvements in a process of this general character disclosed in our pending application for U. S. Letters Patent, Serial No. 407,724.
The annexed drawing and the following description set forth in detail certain steps` embodying. our invention, the disclosed steps, however, constituting but one o'f the.
various methods in which the principle ,ot the said invention may be carried out.
Thedrawing represents a flow diagram of our improved process. Y
` Wel first crush high grade crystalline potash-feldspar to about thirty-live mesh, in order that a subsequent calcining can be thoroughly and economically effected.v `We then calcine this crushed'V ore until the same is converted to an amorphous condition, in order vthat a subsequent digestion with caustic potash may be effected to convert the ore constituents into water soluble or acid soluble compounds. This calcining is eilected upon the bed of a furnace or in any other suitable manner by heating from one (l) to two (2) hours at from 800o to 10500 C. After the ore has -thus been reduced to an amorphous condition, we then further crush thesame to about two hundred (200) mesh after which the same is 'digested with the caustic potash. rlhe digestion of the ore with caustic potash is not carried to a point where all of the ore is converted into water soluble potassium silly cate and potassium z tluininate but there is also produced a water insoluble but an acid soluble potassium aluminum silicate. We'
1922, serial no. $61,704.
.use 90% caustic -potash for the allalicdigesvand also an equal amount of water, heating forfroni one (1) to two hours at a temperature from 275` to 325 C. The operation is effected in an autoclave at a pressure .of from 300 to 350 lbs. per square inch. )Ve then allow a further reaction period of about two (2) hours, resulting in a complete decomposition of the ore into the water or acid soluble compounds above-mentioned. During the digestion operation considerable hydrogen isiformed, after the temperature has reached substantially 200 C., due-to the tact that the iron walls ofthe autoclave are attacked by the strong caustic potash, the reaction being Fe-l-QKGHZFMOlQg--Hg. It may be that some impurity in the ore or even in the iron acts as a catalyst for this reaction. The iron `later appears as an impurity in the aluminum salts or possibly in the silica. In order that this envolved hydrogen may not form an explosive mixture witlr'the oxygen of the air-#which is in the autoclave at the start, we remove this air from the autoclave during the'tirst part 'of the' digestion operation by allowing the pressureto reach thirty (30) to forty (40) lbs. per square inch and then allowing the oxygen toxv escape from the autoclave. The alreadyl formed steam displaces the air which escapes and finally the interior of the auto clave contains nothing but steam, indicated by a current of pure quickly condensingr steam escaping from the autoclave valve.
lVe dilute the alkali digestion products with from one (l) to four (4) times their volume of water and then carbonate themixture with carbon dioxide, maintaining a pressure of about 22 inches above atmospheric pressure, the temperature being maintained at substantially room temperature ,by f
means of apositive removal of the generated heat. `We thus obtain the water soluble potash value in solution and precipitate aluini num hydroxide and ortho silicic acid The mass action resulting from the pressure above-mentioned and the Amaintenance et normal temperature effects the carbonating in about fortydive (45) minutes, the same taking place in two stages, the first stage resulting in a conversion of the potassium content to potassium carbonate and taking i mal carbonate.
only about tive minutes and the second stage convertin the potassium carbonate to bicarbonate and taking about forty (40) minutes. The reaction is based upon the action if the ionized acid (H2003) formed by the dissolving of C02 gas in Water. There is only incomplete precipitation of the silicon andaluminum during the first stage because the potassium carbonate being strongly Megane alkaline dissolves aluminum hydroxide `and lio ortho silicio acid and it is not'until this carbonate is very largely converted into bicaibonate, Which is almost neutral in reaction, that all of the aluminum and silicon separate out. The reactions are represented, at least in principle, by the following equations:
Of course, carbonation to formation of 100 per cent bicarbonate requires just twice the amount of C02 that is needed for the nor.-i The speed of carbonation can be greatly increased b distributing the gas uniformly over the W ole cross-section of the volume of liquid to obtain the most extensive Contact between the gas andliquor, and also .by vei strong agitation. To'the carbonation pro ucts We add about one-half of their volume of Water. We then repeatedly filter and Wash, the Wash Water re.- quirements being from tWo and onefquarter (2l) to 4 and one-half (4%) gallons of Water per lb. of feldspar digested. These steps, of course, result in the recovery of so much of the potassium from the feldspar as was converted into Water soluble compounds during the alkali digestion period.
, vWe convert only a part of the potassium ,carbonates thus obtained into sales products and the balance We causticize in order to obtain caustic potash for reuse in further digestion operations. In detail, We evaporate the carbonate solution in steps obtaining v each time a saturated solution from Which,
as the temperature is permitted to drop, crystalline masses of potassium carbonate and potassium bicarbonate are` obtained, preferably until from live to ten (10) per cent of the tot-al potassium content of the carbonate solution is removed. The potassium carbonatos thus obtained also contain the sodium carbonate that is present and thus prevent the building up of the sodium content during repeated reuses of the caus tic potash.v The balance of the carbonate solution is concentrated to a 10 percent solution Which is suitable for a causticizing operation withv lime to produce caustic potash for reuse andcalcium Acarbonate for sale.
To the alumina and silica residue produced by the carbonating We add enough' Water to make a slurry and then digest the same with from to 125 per cent excess of per cent sulphuric acid7 thus placing all the aluminum salts` in solution as alum and aluminum sulphate and rendering the freshly precipitated silica utterly insoluble as Si02, due to the dehydrating action of the sulphur'ic acid. l
The acid digestion products are diluted with Water and then the saine repeatedly filtered in an acid proof ilter and Washed, the Wash Water utilized being about 2.2 gallons per lb. of ore digested.
The aluminum salts in solution are l'ractionally crystallized, producing as a first. fraction practically pure alum containing only traces of iron, the successive fractions containing proportionately more iron and less alum and, of course, more aluminum sulphate. The alum is represented by the formula K2SO4A12(SO4)3.24H2O and the reason for its presence lies in the fact that there is Jformed in the autoclave a Water insoluble but acid decomposable silica containing KZO and the latter will not appear i'n the carbonate liquors, but in the residue of alumina and silica, there to be decomposed by the sulphuric acid treatment and thence to follow the aluminum.
The silica is dried of its absorbed and adsorbed Water and then cleansed from impurities by treatment With hot concentrated sulphuric acid for one or two hours and then `filtered and Washed free of acid.
What we claim is 1. In a process of separating the constituents of mineral silicates, the steps of recovering tlie potassium value consisting in,
first, converting the silicate into alkali-metal silicate and aluminate by means of a solution of caustic alkali; and then recovering the potassium by passing carbonio acid gas7 in the cold and under pressure additional to that normally incident to carbonation, through the silicate and aluminate solution.
2. ln the process of separating the constituents of mineral silicates, the steps of.. recovering the potassium value consisting in,
hrst, converting the silicate into alkali-metal" aaa-aow silicate and Valuminate by means of a so-lution of caustic alkali, and then recovering the potassium by passing carbonio acid 'gas throughthe silicate and aluminate solution, the heat generated by carbonation being positively removed and the carbonation being eiilected under va pressure of substantially 22 inches above atmospheric pressure.
3. In the process of separating'the' constituents of mineral silicates, the steps of recovering the potassium Value consisting in, first, converting the silicate into potassium sil-icate and aluminate by means of a solution of substantially ninety per cent (90%) caustic potash; and then recovering the potassium by passing carbonio acid gas, in the cold and under pressure additional to that normally incident to carbonation, through the potassium silicate and aluminate solution..
4. In a process of separating the constituents of mineral silicates, the steps which consist in converting the natural ore into an amorphous condition; digesting the same with substantially 90% caustic potash in amount from one and one quarter (19;) to two (2) times the Weight of the ore and ar. equal Weight of water, thus obtaining Water soluble potassium silicate and potassium aluminate and Water insoluble but acid solublepotassium aluminum silicate; diluting the alkali digestion products With Water and carbonating with carbon dioxide to remove the Water soluble potassium values; filtering and then digesting the alumina and silica residue with an excess of substantially 95% sulphuric acid to remove the aluminum as soluble salts; and filtering and fractionally crystallizing the aluminum solution, thus obtaining as a first fraction ractically `pure alum (K2SO4A12'(SO4)3.24 20) and successive fractions of alum containing increasing quantities of aluminum sulphate.
5. In a process of separating the constituents of mineral silicates, the steps Which consist in converting the natural ore into an amorphous condition; digesting the same with substantially 90% caustic potash in amount. substantially two (2) times the weight of the ore and an equal Weight of water, thus obtaining .Water soluble potassium silicate and potassium aluminate and water insoluble but acid soluble potassium aluminum silicate; diluting the alkali digestion products with an amount of Water at least equal in volume to said products,'and carbonating with carbon dioxide to substantially complete bicarbonation to remove the water soluble potassium values; filtering and thendigesting the alumina and silica residue With an excess of substantially 95% sulphuric acid to remove the aluminum as soluble salts; and se arating the resultant insoluble silica from't e solution of alumi` num Salts. v .f
6. In a process of separating the constituents of mineral silicates, the steps which consist in crushing the natural ore to substantially thirty-tive (35) mesh; converting the crushed ore to an amorphous condition; further crushing the amorphous ore to substantially two hundred (200) mesh; digesting the line ore With substantially 90% caustic potash in amount from one and one quarter (19g) to two (2) times the Weight of.
soluble but acid soluble potassium aluminum silicate; diluting the alkali digestion products with Water andcarbonating with carbon dioxide to remove the Water soluble potassium values; filtering and 'then digesting the alumina and silica residue With an excess of substantially 95% sulphuric acid to remove the aluminum as soluble salts; and iiltering and ractionally crystallizing the aluminum solution, thusobtaining as aiirst fraction practically pure alum (K2SO4A12 (SO4).24H2O) and successive fractions of alum containing increasing quantities 'of aluminum sulphate. A
7. In a process of separating the constituents of mineral silicates, the steps which consist in converting the natural ore into an amorphous condition digesting the same with substantially 90% caustic potash in amount substantially two (2) times the Weightofthe ore and an equal Weight of Water, thus obtaining Water soluble potassium silicate and potassium aluminate and Water insoluble but acid soluble potassium aluminum silicate; diluting the alkali digestion products With an amount of Water at least equal in volume to said products, and carbonating with carbon dioxide to remove the Water soluble potassium values; repeatedly filtering and Washing the carbonation products, the Wash Water requirements .being from 2.25 to 4.5 gallons of Water per pound of ore utilized; digesting the alumina and silica residue with from to 125% excessof substantially 95% sulphuric acid to remove the aluminum as soluble salts;` and ltering and fractionally crystallizing the aluminum solution, thus obtaining as a first fraction practically pure alum (K,SO4Al2(SO4)3.24H2O) and successive fractions of alum containing increasing quantities of aluminum sulphate.
Signed by me this lith day of May, 1922.
Y SHERMAN W. SCOFIELD.
4Signed by me' this 13th day of May, 1922.
JOHN B. LA RUE.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US561704A US1494029A (en) | 1922-05-17 | 1922-05-17 | Process of separating the constituents of mineral silicates |
| US691217A US1751663A (en) | 1922-05-17 | 1924-02-07 | Process of separating the constituents of mineral silicates |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US561704A US1494029A (en) | 1922-05-17 | 1922-05-17 | Process of separating the constituents of mineral silicates |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US1494029A true US1494029A (en) | 1924-05-13 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US561704A Expired - Lifetime US1494029A (en) | 1922-05-17 | 1922-05-17 | Process of separating the constituents of mineral silicates |
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| US (1) | US1494029A (en) |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4056363A (en) * | 1974-03-21 | 1977-11-01 | Georg Messner | Apparatus for the fabrication of pure alumina from Al2 O3 and silica containing raw materials by leaching with hydrochloric acid |
| US20040213705A1 (en) * | 2003-04-23 | 2004-10-28 | Blencoe James G. | Carbonation of metal silicates for long-term CO2 sequestration |
| US20110044869A1 (en) * | 2007-05-21 | 2011-02-24 | Richard Boudreault | Processes for extracting aluminum and iron from aluminous ores |
| US9023301B2 (en) | 2012-01-10 | 2015-05-05 | Orbite Aluminae Inc. | Processes for treating red mud |
| US9150428B2 (en) | 2011-06-03 | 2015-10-06 | Orbite Aluminae Inc. | Methods for separating iron ions from aluminum ions |
| US9181603B2 (en) | 2012-03-29 | 2015-11-10 | Orbite Technologies Inc. | Processes for treating fly ashes |
| US9260767B2 (en) | 2011-03-18 | 2016-02-16 | Orbite Technologies Inc. | Processes for recovering rare earth elements from aluminum-bearing materials |
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| US9353425B2 (en) | 2012-09-26 | 2016-05-31 | Orbite Technologies Inc. | Processes for preparing alumina and magnesium chloride by HCl leaching of various materials |
| US9382600B2 (en) | 2011-09-16 | 2016-07-05 | Orbite Technologies Inc. | Processes for preparing alumina and various other products |
| US9410227B2 (en) | 2011-05-04 | 2016-08-09 | Orbite Technologies Inc. | Processes for recovering rare earth elements from various ores |
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-
1922
- 1922-05-17 US US561704A patent/US1494029A/en not_active Expired - Lifetime
Cited By (22)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4056363A (en) * | 1974-03-21 | 1977-11-01 | Georg Messner | Apparatus for the fabrication of pure alumina from Al2 O3 and silica containing raw materials by leaching with hydrochloric acid |
| US20040213705A1 (en) * | 2003-04-23 | 2004-10-28 | Blencoe James G. | Carbonation of metal silicates for long-term CO2 sequestration |
| US8114374B2 (en) | 2003-04-23 | 2012-02-14 | U.T. Battelle, LLC. | Carbonation of metal silicates for long-term CO2 sequestration |
| US8673256B2 (en) | 2003-04-23 | 2014-03-18 | Ut-Battelle, Llc | Carbonation of metal silicates for long-term CO2 sequestration |
| US10632418B2 (en) | 2003-04-23 | 2020-04-28 | Ut-Battelle, Llc | Carbonation of metal silicates for long-term CO2 sequestration |
| US9718693B2 (en) | 2003-04-23 | 2017-08-01 | Ut-Battelle, Llc | Carbonation of metal silicates for long-term CO2 sequestration |
| US20110044869A1 (en) * | 2007-05-21 | 2011-02-24 | Richard Boudreault | Processes for extracting aluminum and iron from aluminous ores |
| US8241594B2 (en) | 2007-05-21 | 2012-08-14 | Orbite Aluminae Inc. | Processes for extracting aluminum and iron from aluminous ores |
| US8337789B2 (en) | 2007-05-21 | 2012-12-25 | Orsite Aluminae Inc. | Processes for extracting aluminum from aluminous ores |
| US8597600B2 (en) | 2007-05-21 | 2013-12-03 | Orbite Aluminae Inc. | Processes for extracting aluminum from aluminous ores |
| US9945009B2 (en) | 2011-03-18 | 2018-04-17 | Orbite Technologies Inc. | Processes for recovering rare earth elements from aluminum-bearing materials |
| US9260767B2 (en) | 2011-03-18 | 2016-02-16 | Orbite Technologies Inc. | Processes for recovering rare earth elements from aluminum-bearing materials |
| US9410227B2 (en) | 2011-05-04 | 2016-08-09 | Orbite Technologies Inc. | Processes for recovering rare earth elements from various ores |
| US9150428B2 (en) | 2011-06-03 | 2015-10-06 | Orbite Aluminae Inc. | Methods for separating iron ions from aluminum ions |
| US9382600B2 (en) | 2011-09-16 | 2016-07-05 | Orbite Technologies Inc. | Processes for preparing alumina and various other products |
| US10174402B2 (en) | 2011-09-16 | 2019-01-08 | Orbite Technologies Inc. | Processes for preparing alumina and various other products |
| US9556500B2 (en) | 2012-01-10 | 2017-01-31 | Orbite Technologies Inc. | Processes for treating red mud |
| US9023301B2 (en) | 2012-01-10 | 2015-05-05 | Orbite Aluminae Inc. | Processes for treating red mud |
| US9181603B2 (en) | 2012-03-29 | 2015-11-10 | Orbite Technologies Inc. | Processes for treating fly ashes |
| US9290828B2 (en) | 2012-07-12 | 2016-03-22 | Orbite Technologies Inc. | Processes for preparing titanium oxide and various other products |
| US9353425B2 (en) | 2012-09-26 | 2016-05-31 | Orbite Technologies Inc. | Processes for preparing alumina and magnesium chloride by HCl leaching of various materials |
| US9534274B2 (en) | 2012-11-14 | 2017-01-03 | Orbite Technologies Inc. | Methods for purifying aluminium ions |
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