CN104649303A - Low temperature Bayer process for alumina production - Google Patents
Low temperature Bayer process for alumina production Download PDFInfo
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- CN104649303A CN104649303A CN201310575999.8A CN201310575999A CN104649303A CN 104649303 A CN104649303 A CN 104649303A CN 201310575999 A CN201310575999 A CN 201310575999A CN 104649303 A CN104649303 A CN 104649303A
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F7/00—Compounds of aluminium
- C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
- C01F7/04—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom
- C01F7/06—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom by treating aluminous minerals or waste-like raw materials with alkali hydroxide, e.g. leaching of bauxite according to the Bayer process
- C01F7/062—Digestion
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Abstract
The invention provides a low temperature Bayer process for alumina production. The process comprises the steps of preparation of raw ore slurry and lime milk, dissolution and dilution of raw pulp, red mud separation and washing, fine liquid cooling and decomposition, classification of aluminium hydroxide slurry, filtration and washing, and aluminium hydroxide roasting. The process realizes pulp dissolution under the lower temperature, and is similar to the sintering process; and many devices can be in common use, and just a little improvement is required. The process has the characteristics of short process, low energy consumption and low cost; and the prepared alumina has good quality and high purity.
Description
Technical field
The present invention relates to a kind of process for making alumina, especially low temperature Bayer process process for making alumina
.
Background technology
Alumina-producing method is broadly divided into four classes, i.e. alkaline process, acid system, using acid and alkali combination method and Re Fa.But almost entirely belong to alkaline process for industrial at present.Alkaline process produces aluminum oxide, is process aluminum ore with alkali (NaOH or Na2C03), makes the aluminum oxide in ore be transformed into sodium aluminate solution.The silicon of the impurity such as the iron in ore, titanium and the overwhelming majority then becomes undissolved compound, by undissolved residue (owing to taking on a red color containing ferric oxide, therefore be called red mud) and solution separating, discard or fully utilize, to reclaim useful component wherein after washing.Pure decomposing sodium aluminate solution separates out aluminium hydroxide, carries out roasting, obtain alumina product after being separated with mother liquor, washing.Decomposition nut liquid can be recycled, and processes other a collection of ore.
Alkaline process is produced aluminum oxide and is divided into again the kinds of processes such as Bayer process, sintering process and Bayer-sintering integrated process.I
What oneself the alumina producing corporate boss that builds up of state will adopt is sintering process and Bayer-sintering integrated process technique, newly-built
Or the rebuilding and expansion of the of the existing enterprises be mostly bayer process.Sintering process is relative to Bayer process and mixed combining method, there is the advantage that can process low-grade bauxite, but it also has the remarkable shortcomings such as technical process is long, equipment configuration is complicated, energy consumption is high, quality product is poor, high expensive simultaneously, especially cost one, in today of alumina market cut-throat competition, sintering process is produced aluminum oxide and is in competitive disadvantages.
Summary of the invention
The object of the invention is the above-mentioned shortcoming for overcoming current sintering process for alumina production, adopting the Bayer process production technique through improving.
For achieving the above object, the technical solution used in the present invention is as follows:
A kind of low temperature Bayer process process for making alumina is provided, comprises the following steps:
(1) raw pulp and milk of lime preparation: circulating mother liquor and bauxite are sent into raw material grinding mill in proportion, grind into raw pulp, raw pulp enters dashpot one, be pumped into hydrocyclone group again, the coarse grain ore pulp that contains of swirler bottom discharge returns raw material grinding mill, top is overflowed and is entered dashpot two containing particulate bauxite pulp gravity flow, with pump, the ore pulp in dashpot two is sent into pulp tank one and carries out pre-desiliconizing, obtained raw pulp; Lime enters lime slaking machine together with hot water, makes milk of lime and sends into the thick liquid bath of digestion workshop.
(2) raw pulp stripping and dilution: by ore slurry pump the raw pulp in pulp tank one sent into the pulp tank two in digestion workshop and proceed pre-desiliconizing, the two-stage double pipe heater being not less than 140 DEG C by high pressure ore slurry pump through preheating temperature again sends into heating digester, and press-in insulation digester, soaking time is no less than l hour, dissolved mineral slurry enters two-stage flash-pot and is cooled to 105 DEG C, dilution trap is pressed into again by two-stage flash-pot, add red mud wash liquor simultaneously, white clay washing lotion or supplementary a little recirculated water, by after dissolved mineral slurry concentration dilution to 140g/L with being pumped into red-mud separation subsider,
(3) red-mud separation and washing: the ore pulp of dilution at red-mud separation subsider through flocculating settling; solid-liquor separation; its seston is less than the overflowing liquid of 1g/L from flowing into thick liquid bath; the underflow that its liquid-solid ratio is less than 3 sends into washing settling groove by underflow pump with secondary cleaning water after separating underflow groove mixes; after carrying out five backflushs successively; last underflow filters through horizontal filter, reclaims attached liquid; Red mud filter cake mixes in the outer emissions groove of red mud with recirculated water, send stockyard by red mud efflux pump, and red mud backwater returns hot water tank heating and does bath water; Separation tank overflowing liquid is prepared after a small amount of milk of lime sent here in workshop mixes in thick liquid bath with ore pulp, thick liquid containing coagulant aids sends into triumphant sharp horizontal leaf filter, most of solid in thick liquid is removed by press filtration, filter cake bath water unloads backlash to filter cake groove, with being pumped into dissolved mineral slurry dilution trap, seston is less than 0.0159/L refined liquid and is pumped to seminal fluid cooling by seminal fluid;
(4) seminal fluid cooling Sum decomposition: seminal fluid is lowered the temperature through two-stage plate-type heat exchanger, first step plate-type heat exchanger side is hot seminal fluid, opposite side is seed precipitation solution, plate-type heat exchanger side, the second stage is the hot seminal fluid after one-level cooling, opposite side is recirculated water, after cooling, seminal fluid send kind of a point first groove after vertical plate mixes with seed aluminum hydroxide, after cooling seminal fluid and seed aluminum hydroxide enter the first groove of seed precipitation tank, slurries chute through between groove enters subsequent decomposition groove successively, through the continuous decomposition of 50 hours, obtained aluminum hydroxide slurry flowed into kind of a separating groove;
(5) aluminum hydroxide slurry classification: plant the aluminum hydroxide slurry of separating groove outflow through hydroclone classification;
(6) filter and wash: certainly flowing into aluminum hydroxide slurry groove containing the aluminum hydroxide slurry that particle is thicker after classification, then be separated with being pumped into horizontal table filter, the qualified aluminium hydroxide of washing output supplies roasting;
(7) Aluminium hydroxide roasting: Aluminium hydroxide roasting is become qualified aluminum oxide finished product by gaseous pollutant control.
Al in bauxite described in step (1)
2o
3content be 45-55%, alumina silica ratio A/S>=5; Described circulating mother liquor concentration N
k=170-200g/L; Described raw pulp concentration is 240-260g/L.
The present invention adopts a kind of bayer process carrying out ore pulp stripping at a lower temperature, and close with sintering process technique, much equipment can be general, only need do a little improvement, have the advantages that flow process is short, energy consumption is low, cost is economized, obtained quality of alumina is good, and purity is high.
Embodiment
Below by two embodiments, the invention will be further described.
Embodiment 1
A kind of low temperature Bayer process process for making alumina, comprises the following steps:
(1) raw pulp and milk of lime preparation: circulating mother liquor and bauxite are sent into raw material grinding mill in proportion, grind into raw pulp, raw pulp enters dashpot one, be pumped into hydrocyclone group again, the coarse grain ore pulp that contains of swirler bottom discharge returns raw material grinding mill, top is overflowed and is entered dashpot two containing particulate bauxite pulp gravity flow, with pump, the ore pulp in dashpot two is sent into pulp tank one and carries out pre-desiliconizing, obtained raw pulp; Lime enters lime slaking machine together with hot water, makes milk of lime and sends into the thick liquid bath of digestion workshop; Al in bauxite
2o
3content be 45%, alumina silica ratio A/S=5, circulating mother liquor concentration N
k=170g/L, obtained raw pulp concentration is 240g/L;
(2) raw pulp stripping and dilution: by ore slurry pump the raw pulp in pulp tank one sent into the pulp tank two in digestion workshop and proceed pre-desiliconizing, the two-stage double pipe heater being not less than 140 DEG C by high pressure ore slurry pump through preheating temperature again sends into heating digester, and press-in insulation digester, soaking time is no less than l hour, dissolved mineral slurry enters two-stage flash-pot and is cooled to 105 DEG C, dilution trap is pressed into again by two-stage flash-pot, add red mud wash liquor simultaneously, white clay washing lotion or supplementary a little recirculated water, by after dissolved mineral slurry concentration dilution to 140g/L with being pumped into red-mud separation subsider,
(3) red-mud separation and washing: the ore pulp of dilution at red-mud separation subsider through flocculating settling; solid-liquor separation; its seston is less than the overflowing liquid of 1g/L from flowing into thick liquid bath; the underflow that its liquid-solid ratio is less than 3 sends into washing settling groove by underflow pump with secondary cleaning water after separating underflow groove mixes; after carrying out five backflushs successively; last underflow filters through horizontal filter, reclaims attached liquid; Red mud filter cake mixes in the outer emissions groove of red mud with recirculated water, send stockyard by red mud efflux pump, and red mud backwater returns hot water tank heating and does bath water; Separation tank overflowing liquid is prepared after a small amount of milk of lime sent here in workshop mixes in thick liquid bath with ore pulp, thick liquid containing coagulant aids sends into triumphant sharp horizontal leaf filter, most of solid in thick liquid is removed by press filtration, filter cake bath water unloads backlash to filter cake groove, with being pumped into dissolved mineral slurry dilution trap, seston is less than 0.0159/L refined liquid and is pumped to seminal fluid cooling by seminal fluid;
(4) seminal fluid cooling Sum decomposition: seminal fluid is lowered the temperature through two-stage plate-type heat exchanger, first step plate-type heat exchanger side is hot seminal fluid, opposite side is seed precipitation solution, plate-type heat exchanger side, the second stage is the hot seminal fluid after one-level cooling, opposite side is recirculated water, after cooling, seminal fluid send kind of a point first groove after vertical plate mixes with seed aluminum hydroxide, after cooling seminal fluid and seed aluminum hydroxide enter the first groove of seed precipitation tank, slurries chute through between groove enters subsequent decomposition groove successively, through the continuous decomposition of 50 hours, obtained aluminum hydroxide slurry flowed into kind of a separating groove;
(5) aluminum hydroxide slurry classification: plant the aluminum hydroxide slurry of separating groove outflow through hydroclone classification;
(6) filter and wash: certainly flowing into aluminum hydroxide slurry groove containing the aluminum hydroxide slurry that particle is thicker after classification, then be separated with being pumped into horizontal table filter, the qualified aluminium hydroxide of washing output supplies roasting;
(7) Aluminium hydroxide roasting: Aluminium hydroxide roasting is become qualified aluminum oxide finished product by gaseous pollutant control.
Embodiment 2
A kind of low temperature Bayer process process for making alumina, comprises the following steps:
(1) raw pulp and milk of lime preparation: circulating mother liquor and bauxite are sent into raw material grinding mill in proportion, grind into raw pulp, raw pulp enters dashpot one, be pumped into hydrocyclone group again, the coarse grain ore pulp that contains of swirler bottom discharge returns raw material grinding mill, top is overflowed and is entered dashpot two containing particulate bauxite pulp gravity flow, with pump, the ore pulp in dashpot two is sent into pulp tank one and carries out pre-desiliconizing, obtained raw pulp; Lime enters lime slaking machine together with hot water, makes milk of lime and sends into the thick liquid bath of digestion workshop; Al in bauxite
2o
3content be 55%, alumina silica ratio A/S=6, circulating mother liquor concentration N
k=200g/L, obtained raw pulp concentration is 260g/L;
(2) raw pulp stripping and dilution: by ore slurry pump the raw pulp in pulp tank one sent into the pulp tank two in digestion workshop and proceed pre-desiliconizing, the two-stage double pipe heater being not less than 140 DEG C by high pressure ore slurry pump through preheating temperature again sends into heating digester, and press-in insulation digester, soaking time is no less than l hour, dissolved mineral slurry enters two-stage flash-pot and is cooled to 105 DEG C, dilution trap is pressed into again by two-stage flash-pot, add red mud wash liquor simultaneously, white clay washing lotion or supplementary a little recirculated water, by after dissolved mineral slurry concentration dilution to 140g/L with being pumped into red-mud separation subsider,
(3) red-mud separation and washing: the ore pulp of dilution at red-mud separation subsider through flocculating settling; solid-liquor separation; its seston is less than the overflowing liquid of 1g/L from flowing into thick liquid bath; the underflow that its liquid-solid ratio is less than 3 sends into washing settling groove by underflow pump with secondary cleaning water after separating underflow groove mixes; after carrying out five backflushs successively; last underflow filters through horizontal filter, reclaims attached liquid; Red mud filter cake mixes in the outer emissions groove of red mud with recirculated water, send stockyard by red mud efflux pump, and red mud backwater returns hot water tank heating and does bath water; Separation tank overflowing liquid is prepared after a small amount of milk of lime sent here in workshop mixes in thick liquid bath with ore pulp, thick liquid containing coagulant aids sends into triumphant sharp horizontal leaf filter, most of solid in thick liquid is removed by press filtration, filter cake bath water unloads backlash to filter cake groove, with being pumped into dissolved mineral slurry dilution trap, seston is less than 0.0159/L refined liquid and is pumped to seminal fluid cooling by seminal fluid;
(4) seminal fluid cooling Sum decomposition: seminal fluid is lowered the temperature through two-stage plate-type heat exchanger, first step plate-type heat exchanger side is hot seminal fluid, opposite side is seed precipitation solution, plate-type heat exchanger side, the second stage is the hot seminal fluid after one-level cooling, opposite side is recirculated water, after cooling, seminal fluid send kind of a point first groove after vertical plate mixes with seed aluminum hydroxide, after cooling seminal fluid and seed aluminum hydroxide enter the first groove of seed precipitation tank, slurries chute through between groove enters subsequent decomposition groove successively, through the continuous decomposition of 50 hours, obtained aluminum hydroxide slurry flowed into kind of a separating groove;
(5) aluminum hydroxide slurry classification: plant the aluminum hydroxide slurry of separating groove outflow through hydroclone classification;
(6) filter and wash: certainly flowing into aluminum hydroxide slurry groove containing the aluminum hydroxide slurry that particle is thicker after classification, then be separated with being pumped into horizontal table filter, the qualified aluminium hydroxide of washing output supplies roasting;
(7) Aluminium hydroxide roasting: Aluminium hydroxide roasting is become qualified aluminum oxide finished product by gaseous pollutant control.
Claims (2)
1. a low temperature Bayer process process for making alumina, is characterized in that comprising the following steps:
(1) raw pulp and milk of lime preparation: circulating mother liquor and bauxite are sent into raw material grinding mill in proportion, grind into raw pulp, raw pulp enters dashpot one, be pumped into hydrocyclone group again, the coarse grain ore pulp that contains of swirler bottom discharge returns raw material grinding mill, top is overflowed and is entered dashpot two containing particulate bauxite pulp gravity flow, with pump, the ore pulp in dashpot two is sent into pulp tank one and carries out pre-desiliconizing, obtained raw pulp; Lime enters lime slaking machine together with hot water, makes milk of lime and sends into the thick liquid bath of digestion workshop;
(2) raw pulp stripping and dilution: by ore slurry pump the raw pulp in pulp tank one sent into the pulp tank two in digestion workshop and proceed pre-desiliconizing, the two-stage double pipe heater being not less than 140 DEG C by high pressure ore slurry pump through preheating temperature again sends into heating digester, and press-in insulation digester, soaking time is no less than l hour, dissolved mineral slurry enters two-stage flash-pot and is cooled to 105 DEG C, dilution trap is pressed into again by two-stage flash-pot, add red mud wash liquor simultaneously, white clay washing lotion or supplementary a little recirculated water, by after dissolved mineral slurry concentration dilution to 140g/L with being pumped into red-mud separation subsider,
(3) red-mud separation and washing: the ore pulp of dilution at red-mud separation subsider through flocculating settling; solid-liquor separation; its seston is less than the overflowing liquid of 1g/L from flowing into thick liquid bath; the underflow that its liquid-solid ratio is less than 3 sends into washing settling groove by underflow pump with secondary cleaning water after separating underflow groove mixes; after carrying out five backflushs successively; last underflow filters through horizontal filter, reclaims attached liquid; Red mud filter cake mixes in the outer emissions groove of red mud with recirculated water, send stockyard by red mud efflux pump, and red mud backwater returns hot water tank heating and does bath water; Separation tank overflowing liquid is prepared after a small amount of milk of lime sent here in workshop mixes in thick liquid bath with ore pulp, thick liquid containing coagulant aids sends into triumphant sharp horizontal leaf filter, most of solid in thick liquid is removed by press filtration, filter cake bath water unloads backlash to filter cake groove, with being pumped into dissolved mineral slurry dilution trap, seston is less than 0.0159/L refined liquid and is pumped to seminal fluid cooling by seminal fluid;
(4) seminal fluid cooling Sum decomposition: seminal fluid is lowered the temperature through two-stage plate-type heat exchanger, first step plate-type heat exchanger side is hot seminal fluid, opposite side is seed precipitation solution, plate-type heat exchanger side, the second stage is the hot seminal fluid after one-level cooling, opposite side is recirculated water, after cooling, seminal fluid send kind of a point first groove after vertical plate mixes with seed aluminum hydroxide, after cooling seminal fluid and seed aluminum hydroxide enter the first groove of seed precipitation tank, slurries chute through between groove enters subsequent decomposition groove successively, through the continuous decomposition of 50 hours, obtained aluminum hydroxide slurry flowed into kind of a separating groove;
(5) aluminum hydroxide slurry classification: plant the aluminum hydroxide slurry of separating groove outflow through hydroclone classification;
(6) filter and wash: certainly flowing into aluminum hydroxide slurry groove containing the aluminum hydroxide slurry that particle is thicker after classification, then be separated with being pumped into horizontal table filter, the qualified aluminium hydroxide of washing output supplies roasting;
(7) Aluminium hydroxide roasting: Aluminium hydroxide roasting is become qualified aluminum oxide finished product by gaseous pollutant control.
2. low temperature Bayer process process for making alumina according to claim 1, is characterized in that: Al in bauxite described in step (1)
2o
3content be 45-55%, alumina silica ratio A/S>=5; Described circulating mother liquor concentration N
k=170-200g/L; Described raw pulp concentration is 240-260g/L.
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| CN201310575999.8A CN104649303A (en) | 2013-11-18 | 2013-11-18 | Low temperature Bayer process for alumina production |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106276995A (en) * | 2015-06-25 | 2017-01-04 | 沈阳铝镁设计研究院有限公司 | A kind of synthetic filter process in aluminum oxide production process |
| CN106315644A (en) * | 2015-07-03 | 2017-01-11 | 北京华索科技股份有限公司 | Method and system for acquiring refined fluid in alumina production process |
| CN107827131A (en) * | 2017-12-25 | 2018-03-23 | 河南有色汇源铝业有限公司 | A kind of method of alumina producing Bayer process |
| CN109678185A (en) * | 2018-12-18 | 2019-04-26 | 杭州科创有色金属研究有限公司 | A kind of devices and methods therefor for crude liquid refining in alumina producing |
| CN109850929A (en) * | 2018-12-31 | 2019-06-07 | 贵州博汇联润铝业有限公司 | A kind of seed precipitation tank dilution crude ore pulp prepares aluminium hydroxide micro powder method |
| CN111410219A (en) * | 2020-03-26 | 2020-07-14 | 重庆市南川区先锋氧化铝有限公司 | Bauxite dissolving-out process |
| CN116287767A (en) * | 2023-02-17 | 2023-06-23 | 贵港沃斯顿科技有限公司 | Method for improving dissolution rate of indissolvable bauxite |
| CN116425183A (en) * | 2023-04-07 | 2023-07-14 | 湖南省庭宇环保科技发展有限公司 | Alumina production method |
-
2013
- 2013-11-18 CN CN201310575999.8A patent/CN104649303A/en active Pending
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106276995A (en) * | 2015-06-25 | 2017-01-04 | 沈阳铝镁设计研究院有限公司 | A kind of synthetic filter process in aluminum oxide production process |
| CN106315644A (en) * | 2015-07-03 | 2017-01-11 | 北京华索科技股份有限公司 | Method and system for acquiring refined fluid in alumina production process |
| CN107827131A (en) * | 2017-12-25 | 2018-03-23 | 河南有色汇源铝业有限公司 | A kind of method of alumina producing Bayer process |
| CN107827131B (en) * | 2017-12-25 | 2020-05-12 | 河南有色汇源铝业有限公司 | Method for producing aluminum oxide by Bayer process |
| CN109678185A (en) * | 2018-12-18 | 2019-04-26 | 杭州科创有色金属研究有限公司 | A kind of devices and methods therefor for crude liquid refining in alumina producing |
| CN109850929A (en) * | 2018-12-31 | 2019-06-07 | 贵州博汇联润铝业有限公司 | A kind of seed precipitation tank dilution crude ore pulp prepares aluminium hydroxide micro powder method |
| CN111410219A (en) * | 2020-03-26 | 2020-07-14 | 重庆市南川区先锋氧化铝有限公司 | Bauxite dissolving-out process |
| CN111410219B (en) * | 2020-03-26 | 2022-11-11 | 重庆市九龙万博新材料科技有限公司 | Bauxite dissolving-out process |
| CN116287767A (en) * | 2023-02-17 | 2023-06-23 | 贵港沃斯顿科技有限公司 | Method for improving dissolution rate of indissolvable bauxite |
| CN116425183A (en) * | 2023-04-07 | 2023-07-14 | 湖南省庭宇环保科技发展有限公司 | Alumina production method |
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