CN100412012C - Method of treating red mud by extracting Bayer method mother liquid - Google Patents
Method of treating red mud by extracting Bayer method mother liquid Download PDFInfo
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- CN100412012C CN100412012C CNB2006101408583A CN200610140858A CN100412012C CN 100412012 C CN100412012 C CN 100412012C CN B2006101408583 A CNB2006101408583 A CN B2006101408583A CN 200610140858 A CN200610140858 A CN 200610140858A CN 100412012 C CN100412012 C CN 100412012C
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- 238000000034 method Methods 0.000 title claims abstract description 77
- 239000007788 liquid Substances 0.000 title claims abstract description 46
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 37
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims abstract description 17
- 235000011941 Tilia x europaea Nutrition 0.000 claims abstract description 17
- 239000004571 lime Substances 0.000 claims abstract description 17
- 238000001704 evaporation Methods 0.000 claims abstract description 11
- 229910052782 aluminium Inorganic materials 0.000 claims abstract description 9
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims abstract description 9
- 239000004411 aluminium Substances 0.000 claims abstract description 9
- 239000002893 slag Substances 0.000 claims abstract description 4
- 238000000605 extraction Methods 0.000 claims description 126
- 238000004131 Bayer process Methods 0.000 claims description 26
- 239000012452 mother liquor Substances 0.000 claims description 24
- 238000004090 dissolution Methods 0.000 claims description 23
- 239000003921 oil Substances 0.000 claims description 20
- 239000003795 chemical substances by application Substances 0.000 claims description 18
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 16
- 239000000243 solution Substances 0.000 claims description 16
- 150000002191 fatty alcohols Chemical class 0.000 claims description 14
- OSMSIOKMMFKNIL-UHFFFAOYSA-N calcium;silicon Chemical compound [Ca]=[Si] OSMSIOKMMFKNIL-UHFFFAOYSA-N 0.000 claims description 13
- 239000003518 caustics Substances 0.000 claims description 12
- 230000008020 evaporation Effects 0.000 claims description 10
- 239000012530 fluid Substances 0.000 claims description 9
- -1 hydrogen sodium oxide Chemical class 0.000 claims description 7
- 229910052799 carbon Inorganic materials 0.000 claims description 6
- 238000000354 decomposition reaction Methods 0.000 claims description 6
- 239000000203 mixture Substances 0.000 claims description 6
- 239000012670 alkaline solution Substances 0.000 claims description 5
- 229910001948 sodium oxide Inorganic materials 0.000 claims description 5
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Natural products OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims description 4
- 239000003350 kerosene Substances 0.000 claims description 4
- 229960003742 phenol Drugs 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 3
- 150000004996 alkyl benzenes Chemical group 0.000 claims description 3
- 125000000217 alkyl group Chemical group 0.000 claims description 3
- 229910052739 hydrogen Inorganic materials 0.000 claims description 3
- 239000001257 hydrogen Substances 0.000 claims description 3
- 238000000622 liquid--liquid extraction Methods 0.000 claims description 3
- 238000000638 solvent extraction Methods 0.000 claims description 3
- 239000002699 waste material Substances 0.000 claims description 3
- 125000000373 fatty alcohol group Chemical group 0.000 claims description 2
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 abstract description 29
- 238000011084 recovery Methods 0.000 description 23
- 239000012071 phase Substances 0.000 description 13
- 239000003513 alkali Substances 0.000 description 12
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 12
- 230000035484 reaction time Effects 0.000 description 12
- 239000000126 substance Substances 0.000 description 12
- 239000004615 ingredient Substances 0.000 description 10
- 239000011734 sodium Substances 0.000 description 8
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 description 6
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 6
- 229910001388 sodium aluminate Inorganic materials 0.000 description 6
- 229910001570 bauxite Inorganic materials 0.000 description 4
- KBPLFHHGFOOTCA-UHFFFAOYSA-N caprylic alcohol Natural products CCCCCCCCO KBPLFHHGFOOTCA-UHFFFAOYSA-N 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 3
- 238000005245 sintering Methods 0.000 description 3
- 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 2
- 229910004298 SiO 2 Inorganic materials 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 229910010413 TiO 2 Inorganic materials 0.000 description 2
- 150000004645 aluminates Chemical class 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 150000004677 hydrates Chemical class 0.000 description 2
- TVMXDCGIABBOFY-UHFFFAOYSA-N n-Octanol Natural products CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 2
- 229910052708 sodium Inorganic materials 0.000 description 2
- KKCBUQHMOMHUOY-UHFFFAOYSA-N sodium oxide Chemical compound [O-2].[Na+].[Na+] KKCBUQHMOMHUOY-UHFFFAOYSA-N 0.000 description 2
- 239000007790 solid phase Substances 0.000 description 2
- CSDREXVUYHZDNP-UHFFFAOYSA-N alumanylidynesilicon Chemical compound [Al].[Si] CSDREXVUYHZDNP-UHFFFAOYSA-N 0.000 description 1
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 1
- 229910021502 aluminium hydroxide Inorganic materials 0.000 description 1
- 239000000378 calcium silicate Substances 0.000 description 1
- 229910052918 calcium silicate Inorganic materials 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 229910001648 diaspore Inorganic materials 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- ZZUFCTLCJUWOSV-UHFFFAOYSA-N furosemide Chemical compound C1=C(Cl)C(S(=O)(=O)N)=CC(C(O)=O)=C1NCC1=CC=CO1 ZZUFCTLCJUWOSV-UHFFFAOYSA-N 0.000 description 1
- 238000009533 lab test Methods 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- NASFKTWZWDYFER-UHFFFAOYSA-N sodium;hydrate Chemical compound O.[Na] NASFKTWZWDYFER-UHFFFAOYSA-N 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Images
Abstract
The invention discloses a red mud disposal method through mother liquid of through Baeyer extracting method, which is characterized by the following: separating sodium hydroxide from Baeyer mother liquid (decomposed mother liquid, circulating mother liquid or evaporating mother liquid); making extracting phase reextract to obtain sodium hydroxide without aluminium through water; allocating lime to strip Baeyer red mud through adding the sodium hydroxide solution; draining the slag; returning the stripped liquid for Baeyer ore.
Description
Technical field
A kind of method for the treatment of red mud by extracting Bayer method mother liquid, relate to a kind of with Fatty Alcohol(C12-C14 and C12-C18) or alkylphenol as extraction agent bayer process modified by extraction mother liquor (comprising mother liquid evaporation), with the sodium hydroxide solution that obtains to contain hardly sodium aluminate after the pure water back extraction, handle Bayer process red mud to reclaim aluminum oxide and sodium oxide wherein with this sodium hydroxide solution, the solution behind the processing Bayer process red mud is used for the method for bayer process process in leaching batching.
Background technology
At present, worldwide, basic industry all faces worldwide energy shortage, and resource is dilution and scarcity day by day, and the protection of environment more and more is subjected to people's attention.With regard to aluminum oxide industry, these challenges are all the more sharp-pointed, can not be ignored.
In the explored bauxite resource of China, alumina silica ratio (A/S) is that 5～7 medium grade alumyte accounts for more than 80%.As everyone knows, when handling medium grade (A/S5～7) diaspore type bauxite with pure Bayer process, the alumina recovery rate is low, and the alkaline consumption height causes resource utilization low, and the economic and social benefits of aluminum oxide production process are had a strong impact on.In order to reduce alkaline consumption, improve the rate of recovery of aluminum oxide, the aluminum oxide industry of USSR (Union of Soviet Socialist Republics) and China is devoted to adopt the technical study of Bayer sintering integrated process for a long time, has obtained significant achievement.But facts have proved that the integrated process Production Flow Chart exists energy consumption height, Production Flow Chart complexity, the not high drawback of production efficiency to a certain extent, its crux is that mainly the energy consumption of sintering process system is difficult to have the change of essence.
People such as nineteen fifty-seven ripple Nuo Maliefu are to Na
2O-Al
2O3-CaO-SO
2-H
2O system and Na
2O-CaO-SO
2-H
2O system is studied.Found not contain Al
2O
3Calcium silicate hydrate sodium (Na
2O2CaO2SiO
2H
2O) can be in high temperature high causticity ratio solution stable existence, thereby established the aquation method basis of handling high silicon aluminum-containing raw material, after this states such as the U.S., Hungary, Australia have all carried out extensive studies to high pressure aquation method.China has just proposed to carry out the aquation method and has handled Bayer red mud in 1979, realize the suggestion of Bayer-aquation integrated process, and formally carries out the laboratory test that the aquation method is handled Bayer red mud in 1989, and has obtained bigger breakthrough.Through countries in the world scientist's unremitting effort, Bayer aquation combination producing method is greatly improved and develops.Technological Economy comparison shows that Bayer aquation method is compared with Bayer sintering mixed combining method, and energy consumption and product cost all can reduce significantly.
In traditional Bayer aquation method flow process, the sodium aluminate solution after the Bayer process red mud stripping need be evaporated to Na
2The concentration that the O500 grams per liter is above, to separate out aluminate hydrates sodium solid phase, after the liquid-solid separation, liquid phase is that more high causticity ratio's (greater than 30) solution is used for exsolution red mud as circulating mother liquor, aluminate hydrates sodium solid phase changes the sodium aluminate solution of low causticity ratio again into.This flow process complexity, and steam consumption is big in the evaporative process.
Therefore, the key issue of realization Bayer hydro chemical method is the circulating mother liquor that will obtain the high causticity ratio.
Summary of the invention
Purpose of the present invention is exactly the deficiency that exists at above-mentioned prior art, provides that a kind of flow process is simple, energy expenditure, can with Bayer process and the high pressure water chemical method method of bonded treating red mud by extracting Bayer method mother liquid organically.
The objective of the invention is to be achieved through the following technical solutions.
A kind of method for the treatment of red mud by extracting Bayer method mother liquid, it is characterized in that with liquid-liquid extraction separation of hydrogen sodium oxide from the ear method mother liquor that comprises decomposition nut liquid, circulating mother liquor or mother liquid evaporation, with the solution after the back extraction of extraction phase water, allocate lime into, Bayer process red mud is handled in stripping, the stripping slag is a waste, and dissolution fluid returns and is used for Bayer process and joins the ore deposit.
The method of a kind for the treatment of red mud by extracting Bayer method mother liquid of the present invention is characterized in that extraction agent is Fatty Alcohol(C12-C14 and C12-C18) or alkylphenol.
The method of a kind for the treatment of red mud by extracting Bayer method mother liquid of the present invention is characterized in that the extraction agent for Fatty Alcohol(C12-C14 and C12-C18) is that carbon chain lengths is the Fatty Alcohol(C12-C14 and C12-C18) of 6-20 or their mixture.
The method of a kind for the treatment of red mud by extracting Bayer method mother liquid of the present invention is characterized in that the extraction agent for induced by alkyl hydroxybenzene, and the position on its alkyl substituted benzene ring can be preferably in contraposition for ortho position, a position and contraposition, and single alkyl branches length is 12-18 carbon.
The method of a kind for the treatment of red mud by extracting Bayer method mother liquid of the present invention is characterized in that its its thinner of induced by alkyl hydroxybenzene extraction agent is that carbon chain lengths is the alkane of 6-18 carbon or the mixture of kerosene and Fatty Alcohol(C12-C14 and C12-C18).
The method of a kind for the treatment of red mud by extracting Bayer method mother liquid of the present invention is characterized in that extraction phase water or the back extraction of aluminium hydroxide washings, obtains not contain aluminium or the very high alkaline solution of causticity coefficient.
The method of a kind for the treatment of red mud by extracting Bayer method mother liquid of the present invention, the processing condition that it is characterized in that its process are: extraction and back extraction temperature are 70～95 ℃, extraction phase ratio: oil: water volume ratio=1～3: 1, back extraction is compared: oil: water=1～3: 1, extraction progression is 20～45 grades, and back extraction progression is 6～8 grades.
The method of a kind for the treatment of red mud by extracting Bayer method mother liquid of the present invention is characterized in that with the high causticity coefficient (α that obtains after the back extraction
K) the alkaline solution stripping handle Bayer process red mud, the dissolution fluid behind the exsolution red mud directly returns and is used for Bayer process and joins the ore deposit.
The method of a kind for the treatment of red mud by extracting Bayer method mother liquid of the present invention, it is characterized in that the processing parameter of stripping processing Bayer process red mud is: the lime addition is with calcium silicon C/S, and the mole ratio counts 1.4～3.0; As the mother liquor exsolution red mud, its concentration is N after the adjustment of strip liquor concentration
K60～350g/L; Batching caustic ratio α
K7～15; 240～320 ℃ of stripping temperature; Dissolution time 30～150 minutes.
The method of a kind for the treatment of red mud by extracting Bayer method mother liquid that the present invention proposes, utilize Fatty Alcohol(C12-C14 and C12-C18) or the alkylphenol extraction agent as free alkali in the sodium aluminate solution, as strippant, stripping efficiency reaches more than 95% with pure water in the extraction back, strip liquor is for containing the NaOH solution of sodium aluminate, N hardly
KConcentration can reach about 60～250g/L.With this NaOH strong solution stripping Bayer process red mud that contains sodium aluminate hardly, obtain causticity than 9～16 dissolution fluid, this dissolution fluid is used further to the stripping of bauxite, thus the series connection by Bayer process-extraction-high pressure aquation method realizes Bayer high pressure aquation method smoothly.Handle Bayer process red mud with the alkali lye after the back extraction, can the efficient recovery Bayer process abandon aluminum oxide and sodium oxide in the red mud, resource is efficiently utilized and reduced the harm of red mud significantly environment.The dissolution fluid of the higher causticity ratio behind the exsolution red mud is used for bauxite and joins the ore deposit, and can improve ore proportioning quantity, thereby improves the output capacity of dissolution efficiency and solution.
Description of drawings
Fig. 1 is a kind of method basic flowsheet of coal preparation for the treatment of red mud by extracting Bayer method mother liquid.
Embodiment
A kind of method for the treatment of red mud by extracting Bayer method mother liquid, with liquid-liquid extraction from Bayer process mother liquor (comprising decomposition nut liquid, circulating mother liquor or mother liquid evaporation) separation of hydrogen sodium oxide, obtain aluminiferous hardly sodium hydroxide solution after the back extraction of extraction phase water, Bayer process red mud is handled in stripping after allocating lime under certain condition into this sodium hydroxide solution again, the stripping slag is a waste, and dissolution fluid returns and is used for Bayer process and joins the ore deposit.With carbon chain lengths is that the Fatty Alcohol(C12-C14 and C12-C18) of 6-20 or their mixture are as the extraction agent extraction evaporation mother liquor, the water back extraction, extraction and back extraction temperature are 70～95 ℃, extraction phase is than (oil: be 1～3: 1 water volume ratio), (oil: be 1～3: 1 water) is compared in back extraction, extraction progression is 20～45 grades, and back extraction progression is 6～8 grades.Extraction agent can extract decomposition nut liquid, circulating mother liquor or mother liquid evaporation for alkylphenol, and the position on the alkyl substituted benzene ring can be preferably in contraposition for ortho position, a position and contraposition, and single alkyl branches length is 12-18 carbon.Its thinner can be the alkane of 6-18 carbon or the mixture of kerosene and Fatty Alcohol(C12-C14 and C12-C18) for carbon chain lengths.Water back extraction extraction phase.Extraction and back extraction temperature are 70～95 ℃, and extraction phase is than (oil: be 1～3: 1 water volume ratio), back extraction compares that (oil: be 1～3: 1 water), extracting progression is 20～45 grades, and back extraction progression is 6～8 grades.With the high causticity coefficient (α that obtains after the back extraction
K) the alkaline solution stripping handle Bayer process red mud, obtain dissolution fluid behind the exsolution red mud and directly return and be used for Bayer process and join the ore deposit.The processing parameter of its exsolution red mud is: the lime addition counts 1.4～3.0 with calcium silicon than (C/S, mole ratio); As the mother liquor exsolution red mud, its concentration is N after the adjustment of strip liquor concentration
K60～350g/L; The batching causticity is than 7～15; 240～320 ℃ of stripping temperature; Dissolution time 30～150 minutes.
Below in conjunction with example technology of the present invention is further described.
Embodiment 1
Extraction and back extraction.The Fatty Alcohol(C12-C14 and C12-C18) that with carbon chain lengths is 8-10 is as extraction agent extraction concentration N
KBe the mother liquid evaporation of 320g/L, the water back extraction, extraction temperature is 90 ℃, the back extraction temperature is 85 ℃; Extraction phase than (oil. water volume ratio) be 1: 1, (oil: water) be 2: 1 is compared in back extraction; Extraction progression is 40 grades, 3 minutes every order reaction time; Back extraction progression is 7 grades, 5 minutes every order reaction time.Strip liquor N after the back extraction
KBe 240g/L, causticity compares α
KBe 43 (the small part aluminium that contains is that extracting and separating does not thoroughly cause).
Embodiment 2
Extraction and back extraction.The Fatty Alcohol(C12-C14 and C12-C18) that with carbon chain lengths is 8-10 is as extraction agent extraction concentration N
KBe the mother liquid evaporation of 320g/L, the water back extraction, extraction temperature is 85 ℃, the back extraction temperature is 80 ℃; Extraction phase is than (oil: water volume ratio) be 1: 1, (oil: water) be 3: 1 is compared in back extraction; Extraction progression is 35 grades, and 5 minutes every order reaction time, back extraction progression is 6 grades, 10 minutes every order reaction time.Strip liquor N after the back extraction
KBe 255g/L, causticity compares α
KBe 44.2 (the small part aluminium that contains is that extracting and separating does not thoroughly cause).
Embodiment 3
Extraction and back extraction.Extract concentration N with n-Octanol as extraction agent
KBe the mother liquid evaporation of 320g/L, the water back extraction, extraction temperature is 75 ℃, the back extraction temperature is 70 ℃; Extraction phase than (oil: water volume ratio) be 2.5: 1, back extraction compare (oil. water) be 3: 1; Extraction progression is 20 grades, 12 minutes every order reaction time; Back extraction progression is 8 grades, 12 minutes every order reaction time.Strip liquor N after the back extraction
KBe 244g/L, causticity compares α
KBe 41.3 (the small part aluminium that contains is that extracting and separating does not thoroughly cause).
Embodiment 4
Extraction and back extraction.Extract concentration N with n-Octanol as extraction agent
KBe the mother liquid evaporation of 320g/L, the water back extraction, extraction temperature is 70 ℃, the back extraction temperature is 70 ℃; Extraction phase is than (oil: water volume ratio) be 1: 1, (oil: water) be 3: 1 is compared in back extraction; Extraction progression is 45 grades, 3 minutes every order reaction time; Back extraction progression is 8 grades, 8 minutes every order reaction time.Strip liquor N after the back extraction
KBe 255g/L, causticity compares α
KBe 42.4 (the small part aluminium that contains is that extracting and separating does not thoroughly cause).
Embodiment 5
Extraction and back extraction.With 18 alkylphenols as extraction agent, carbon chain lengths be the Fatty Alcohol(C12-C14 and C12-C18) of 8-10 as thinner, extraction concentration N
KBe the decomposition nut liquid of 170g/L, the water back extraction, extraction temperature is 85 ℃, the back extraction temperature is 80 ℃; Extraction phase is than (oil: water volume ratio) be 2: 1, (oil: water) be 2: 1 is compared in back extraction; Extraction progression is 25 grades, 5 minutes reaction times; Back extraction progression is 6 grades, 5 minutes reaction times.Strip liquor N after the back extraction
KBe 120g/L, causticity compares α
KBe 42 (the small part aluminium that contains is that extracting and separating does not thoroughly cause).
Embodiment 6
Extraction and back extraction.As extraction agent, carbon chain lengths is that the Fatty Alcohol(C12-C14 and C12-C18) of 8-10 mixes the back as thinner with kerosene, extraction concentration N with 13 alkylphenols
KBe the decomposition nut liquid of 170g/L, the water back extraction, extraction temperature is 70 ℃, the back extraction temperature is 70 ℃; Extraction phase is than (oil: water volume ratio) be 1: 1, (oil: water) be 3: 1 is compared in back extraction; Extraction progression is 35 grades, 2 minutes reaction times; Back extraction progression is 8 grades, 8 minutes reaction times.Strip liquor N after the back extraction
KBe 117g/L, causticity compares α
KBe 42.3 (the small part aluminium that contains is that extracting and separating does not thoroughly cause).
Embodiment 7
Red mud is handled in the strip liquor stripping.Red mud chemical ingredients (%): Al
2O
322.76, SiO
217.1, Fe
2O
313.03, TiO
25.35 CaO 21.0, Na
2O 5.96, K
2O 1.43, and A/S 1.33, (N+K)/and S 0.432.
The lime addition counts 1.4 with calcium silicon than (C/S); As the mother liquor exsolution red mud, its concentration is 200g/L, α after the adjustment of strip liquor concentration
KBe 43; The batching causticity is than 12; 250 ℃ of stripping temperature; Dissolution time 90 minutes.The result: the alumina recovery rate is 52% in the red mud, and the caustic alkali rate of recovery is 60.3%.
Embodiment 8
Red mud is handled in the strip liquor stripping.Red mud chemical ingredients (%) is with embodiment 7.
The lime addition counts 1.9 with calcium silicon than (C/S); As the mother liquor exsolution red mud, its concentration is 200g/L, α after the adjustment of strip liquor concentration
KBe 43; The batching causticity is than 12; 250 ℃ of stripping temperature; Dissolution time 90 minutes.The result: the alumina recovery rate is 63% in the red mud, and the caustic alkali rate of recovery is 89.1%.
Embodiment 9
Red mud is handled in the strip liquor stripping.Red mud chemical ingredients (%) is with embodiment 7.
The lime addition counts 3 with calcium silicon than (C/S); As the mother liquor exsolution red mud, its concentration is 200g/L, α after the adjustment of strip liquor concentration
KBe 43; The batching causticity is than 12; 250 ℃ of stripping temperature; Dissolution time 90 minutes.The result: the alumina recovery rate is 32.3% in the red mud, and the caustic alkali rate of recovery is 88.26%.
Embodiment 10
Red mud is handled in the strip liquor stripping.Red mud chemical ingredients (%): Al
2O
315.6.SiO
211.45, Fe
2O
334.0, TiO
26.12, CaO18.6, Na
2O 6.21, and A/S 1.36, and N/S 0.542.
The lime addition counts 21 with calcium silicon than (C/S); As the mother liquor exsolution red mud, its concentration is 200g/L, α after the adjustment of strip liquor concentration
KBe 43; The batching causticity is than 8; 250 ℃ of stripping temperature; Dissolution time 90 minutes.The result: the alumina recovery rate is 70.0% in the red mud, and the caustic alkali rate of recovery is 93.4%.
Embodiment 11
Red mud is handled in the strip liquor stripping.Red mud chemical ingredients (%) is with embodiment 10.
The lime addition counts 2.1 with calcium silicon than (C/S); As the mother liquor exsolution red mud, its concentration is 200g/L, α after the adjustment of strip liquor concentration
KBe 43; The batching causticity is than 14; 250 ℃ of stripping temperature; Dissolution time 90 minutes.The result: the alumina recovery rate is 67.8% in the red mud, and the caustic alkali rate of recovery is 87.4%.
Embodiment 12
Red mud is handled in the strip liquor stripping.Red mud chemical ingredients (%) is with embodiment 10.
The lime addition counts 2.1 with calcium silicon than (C/S); As the mother liquor exsolution red mud, its concentration is 290g/L, α after the adjustment of strip liquor concentration
KBe 43; The batching causticity is than 12; 250 ℃ of stripping temperature; Dissolution time 90 minutes.The result: the alumina recovery rate is 77.3% in the red mud, and the caustic alkali rate of recovery is 93.57%.
Embodiment 13
Red mud is handled in the strip liquor stripping.Red mud chemical ingredients (%) is with embodiment 10.
The lime addition counts 20 with calcium silicon than (C/S); As the mother liquor exsolution red mud, its concentration is 100g/L, α after the adjustment of strip liquor concentration
KBe 43; The batching causticity is than 12; 250 ℃ of stripping temperature; Dissolution time 90 minutes.The result: the alumina recovery rate is 48.5% in the red mud, and the caustic alkali rate of recovery is 90.06%.
Embodiment 14
Red mud is handled in the strip liquor stripping.Red mud chemical ingredients (%) is with embodiment 7.
The lime addition counts 2.0 with calcium silicon than (C/S); As the mother liquor exsolution red mud, its concentration is 200g/L, α after the adjustment of strip liquor concentration
KBe 43; The batching causticity is than 8; 260 ℃ of stripping temperature; Dissolution time 30 minutes.The result: the alumina recovery rate is 45.2% in the red mud, and the caustic alkali rate of recovery is 88.92%.
Embodiment 15
Red mud is handled in the strip liquor stripping.Red mud chemical ingredients (%) is with embodiment 7.
The lime addition counts 2.0 with calcium silicon than (C/S); As the mother liquor exsolution red mud, its concentration is 200g/L, α after the adjustment of strip liquor concentration
KBe 43; The batching causticity is than 8; 260 ℃ of stripping temperature; Dissolution time 150 minutes.The result: the alumina recovery rate is 49.5% in the red mud, and the caustic alkali rate of recovery is 88.94%.
Embodiment 16
Red mud is handled in the strip liquor stripping.Red mud chemical ingredients (%) is with embodiment 7.
The lime addition counts 2.0 with calcium silicon than (C/S); As the mother liquor exsolution red mud, its concentration is 200g/L, α after the adjustment of strip liquor concentration
KBe 43; The batching causticity is than 12; 300 ℃ of stripping temperature; Dissolution time 60 minutes.The result: the alumina recovery rate is 53.2% in the red mud, and the caustic alkali rate of recovery is 89.62%.
Claims (9)
1. the method for a treating red mud by extracting Bayer method mother liquid, it is characterized in that with liquid-liquid extraction separation of hydrogen sodium oxide from the Bayer process mother liquor that comprises decomposition nut liquid, circulating mother liquor or mother liquid evaporation, with the solution after the back extraction of extraction phase water, allocate lime into, Bayer process red mud is handled in stripping, the stripping slag is a waste, and dissolution fluid returns and is used for Bayer process and joins the ore deposit.
2. the method for a kind for the treatment of red mud by extracting Bayer method mother liquid according to claim 1 is characterized in that extraction agent is Fatty Alcohol(C12-C14 and C12-C18) or alkylphenol.
3. the method for a kind for the treatment of red mud by extracting Bayer method mother liquid according to claim 1 is characterized in that the extraction agent for Fatty Alcohol(C12-C14 and C12-C18) is that carbon chain lengths is the Fatty Alcohol(C12-C14 and C12-C18) of 6-20 or their mixture.
4. the method for a kind for the treatment of red mud by extracting Bayer method mother liquid according to claim 1 is characterized in that the extraction agent for induced by alkyl hydroxybenzene, and the position on its alkyl substituted benzene ring can be ortho position, a position and contraposition, and single alkyl branches length is 12-18 carbon.
5. the method for a kind for the treatment of red mud by extracting Bayer method mother liquid according to claim 1 is characterized in that its its thinner of induced by alkyl hydroxybenzene extraction agent is that carbon chain lengths is the alkane of 6-18 carbon or the mixture of kerosene and Fatty Alcohol(C12-C14 and C12-C18).
6. the method for a kind for the treatment of red mud by extracting Bayer method mother liquid according to claim 1 is characterized in that the back extraction of extraction phase water, obtains not contain aluminium or the very high alkaline solution of causticity coefficient.
7. the method for a kind for the treatment of red mud by extracting Bayer method mother liquid according to claim 1, the processing condition that it is characterized in that its process are: extraction and back extraction temperature are 70～95 ℃, extraction phase ratio: oil: water volume ratio=1～3: 1, back extraction is compared: oil: water=1～3: 1, extraction progression is 20～45 grades, and back extraction progression is 6～8 grades.
8. the method for a kind for the treatment of red mud by extracting Bayer method mother liquid according to claim 1 is characterized in that with the high causticity coefficient (α that obtains after the back extraction
K) the alkaline solution stripping handle Bayer process red mud, the dissolution fluid behind the exsolution red mud directly returns and is used for Bayer process and joins the ore deposit.
9. the method for a kind for the treatment of red mud by extracting Bayer method mother liquid according to claim 1, it is characterized in that stripping handles the processing parameter of Bayer process red mud and be: the lime addition is with calcium silicon C/S, and the mole ratio counts 1.4～3.0; As the mother liquor exsolution red mud, its concentration is N after the adjustment of strip liquor concentration
K60～350g/L; Batching caustic ratio α
K7～15; 240～320 ℃ of stripping temperature; Dissolution time 30～150 minutes.
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| CN100532262C (en) * | 2007-07-12 | 2009-08-26 | 中国铝业股份有限公司 | Method for producing aluminium oxide by middle-low grade alumyte |
| CN102336423B (en) * | 2010-07-16 | 2013-07-10 | 中国科学院过程工程研究所 | Method for alumina separation in chromium salt clean production |
| CA2829049C (en) | 2011-03-18 | 2014-12-02 | Orbite Aluminae Inc. | Processes for recovering rare earth elements from aluminum-bearing materials |
| WO2012149642A1 (en) | 2011-05-04 | 2012-11-08 | Orbite Aluminae Inc. | Processes for recovering rare earth elements from various ores |
| RU2013157943A (en) | 2011-06-03 | 2015-07-20 | Орбит Элюминэ Инк. | HEMATITIS METHOD |
| CN102303941B (en) * | 2011-09-14 | 2013-08-21 | 中国科学院过程工程研究所 | Deep dealkalizing method of red mud in alumina factory |
| JP2014526431A (en) | 2011-09-16 | 2014-10-06 | オーバイト アルミナ インコーポレイテッド | Preparation process for alumina and various other products |
| CN102500596B (en) * | 2011-10-20 | 2013-08-07 | 安徽理工大学 | Red mud harmless comprehensive recycling technology suitable for Bayer process |
| US9023301B2 (en) | 2012-01-10 | 2015-05-05 | Orbite Aluminae Inc. | Processes for treating red mud |
| AU2013203808B2 (en) | 2012-03-29 | 2016-07-28 | Orbite Aluminae Inc. | Processes for treating fly ashes |
| WO2014008586A1 (en) | 2012-07-12 | 2014-01-16 | Orbite Aluminae Inc. | Processes for preparing titanium oxide and various other products |
| BR112015006536A2 (en) | 2012-09-26 | 2017-08-08 | Orbite Aluminae Inc | processes for preparing alumina and magnesium chloride by hcl leaching of various materials. |
| EP2920114A4 (en) | 2012-11-14 | 2016-03-02 | Orbite Aluminae Inc | Methods for purifying aluminium ions |
| CN103482654B (en) * | 2013-09-23 | 2015-02-04 | 攀钢集团攀枝花钢铁研究院有限公司 | Method for treating sodium hydroxide solution |
| CN104803392B (en) * | 2015-05-08 | 2017-08-25 | 南京大学 | Sodium hydroxide efficiently separates the method with circulating and recovering in a kind of alkaline sodium silicate |
| CN104973607B (en) * | 2015-07-30 | 2017-10-20 | 江苏南大环保科技有限公司 | A kind of method that continuous extraction from flyash produces quick dissolved sodium silicate |
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| CN1405090A (en) * | 2002-11-12 | 2003-03-26 | 中国铝业股份有限公司 | Bayer production method for aluminium oxide |
| CN1792799A (en) * | 2006-01-16 | 2006-06-28 | 中国铝业股份有限公司 | Process for raising producing aluminium oxide circulating efficiency by Bayer process |
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