CN108083294A - A kind of device and method that aluminium oxide and sodium oxide molybdena are extracted from red mud - Google Patents
A kind of device and method that aluminium oxide and sodium oxide molybdena are extracted from red mud Download PDFInfo
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- CN108083294A CN108083294A CN201810143667.5A CN201810143667A CN108083294A CN 108083294 A CN108083294 A CN 108083294A CN 201810143667 A CN201810143667 A CN 201810143667A CN 108083294 A CN108083294 A CN 108083294A
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- China
- Prior art keywords
- red mud
- preheater
- heat exchange
- rotary kiln
- aluminium oxide
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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Links
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 title claims abstract description 144
- KKCBUQHMOMHUOY-UHFFFAOYSA-N sodium oxide Chemical compound [O-2].[Na+].[Na+] KKCBUQHMOMHUOY-UHFFFAOYSA-N 0.000 title claims abstract description 48
- 229910001948 sodium oxide Inorganic materials 0.000 title claims abstract description 38
- JKQOBWVOAYFWKG-UHFFFAOYSA-N molybdenum trioxide Chemical compound O=[Mo](=O)=O JKQOBWVOAYFWKG-UHFFFAOYSA-N 0.000 title claims abstract description 37
- 238000000034 method Methods 0.000 title claims abstract description 26
- 238000004090 dissolution Methods 0.000 claims abstract description 54
- 238000005245 sintering Methods 0.000 claims abstract description 48
- 239000000463 material Substances 0.000 claims abstract description 46
- 238000000926 separation method Methods 0.000 claims abstract description 35
- 239000012530 fluid Substances 0.000 claims abstract description 31
- 239000000654 additive Substances 0.000 claims abstract description 24
- 230000000996 additive effect Effects 0.000 claims abstract description 24
- 239000002893 slag Substances 0.000 claims abstract description 24
- 239000002002 slurry Substances 0.000 claims abstract description 21
- 238000001035 drying Methods 0.000 claims abstract description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 18
- 239000012065 filter cake Substances 0.000 claims abstract description 16
- 239000007787 solid Substances 0.000 claims abstract description 12
- 238000003756 stirring Methods 0.000 claims abstract description 7
- 239000007789 gas Substances 0.000 claims description 62
- 239000003513 alkali Substances 0.000 claims description 34
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 30
- 238000004131 Bayer process Methods 0.000 claims description 28
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 23
- 239000011734 sodium Substances 0.000 claims description 21
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 20
- 229910052593 corundum Inorganic materials 0.000 claims description 20
- 229910001845 yogo sapphire Inorganic materials 0.000 claims description 20
- 239000004615 ingredient Substances 0.000 claims description 16
- 229910052681 coesite Inorganic materials 0.000 claims description 15
- 229910052906 cristobalite Inorganic materials 0.000 claims description 15
- 239000000377 silicon dioxide Substances 0.000 claims description 15
- 229910052682 stishovite Inorganic materials 0.000 claims description 15
- 229910052905 tridymite Inorganic materials 0.000 claims description 15
- 239000002912 waste gas Substances 0.000 claims description 14
- 238000001914 filtration Methods 0.000 claims description 13
- 230000008676 import Effects 0.000 claims description 13
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 claims description 10
- 230000029087 digestion Effects 0.000 claims description 9
- 239000000706 filtrate Substances 0.000 claims description 9
- 239000000203 mixture Substances 0.000 claims description 7
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims description 5
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 5
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 claims description 5
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 5
- JTCFNJXQEFODHE-UHFFFAOYSA-N [Ca].[Ti] Chemical compound [Ca].[Ti] JTCFNJXQEFODHE-UHFFFAOYSA-N 0.000 claims description 5
- 230000009471 action Effects 0.000 claims description 5
- 239000011575 calcium Substances 0.000 claims description 5
- 229910052791 calcium Inorganic materials 0.000 claims description 5
- 230000000694 effects Effects 0.000 claims description 5
- 239000008187 granular material Substances 0.000 claims description 5
- 238000002386 leaching Methods 0.000 claims description 5
- 239000004571 lime Substances 0.000 claims description 5
- 229910052710 silicon Inorganic materials 0.000 claims description 5
- 239000010703 silicon Substances 0.000 claims description 5
- 239000000126 substance Substances 0.000 claims description 5
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 4
- 238000002360 preparation method Methods 0.000 claims description 3
- 238000003912 environmental pollution Methods 0.000 abstract 1
- 239000003518 caustics Substances 0.000 description 6
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 239000003245 coal Substances 0.000 description 4
- 239000000428 dust Substances 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 238000005406 washing Methods 0.000 description 4
- 230000003466 anti-cipated effect Effects 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 239000003643 water by type Substances 0.000 description 3
- 239000004411 aluminium Substances 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000002817 coal dust Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 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
- 235000019738 Limestone Nutrition 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000001351 cycling effect Effects 0.000 description 1
- 230000004069 differentiation Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000012163 sequencing technique Methods 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D1/00—Oxides or hydroxides of sodium, potassium or alkali metals in general
- C01D1/02—Oxides
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D1/00—Oxides or hydroxides of sodium, potassium or alkali metals in general
- C01D1/04—Hydroxides
-
- 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
- C01F7/0693—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 from waste-like raw materials, e.g. fly ash or Bayer calcination dust
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Geology (AREA)
- Treatment Of Sludge (AREA)
Abstract
A kind of device and method that aluminium oxide and sodium oxide molybdena are extracted from red mud, device include slurrying tank, filter, drying machine, the first preheater, the second preheater, rotary kiln and digester；Slurrying tank, filter, drying machine are sequentially connected with the first preheater, and the second preheater is connected respectively with drying machine and rotary kiln, and rotary kiln is connected with digester；Slurrying tank is set there are four feed inlet, and digester sets two feed inlets and two discharge ports.Method and step is：Water is added in into slurrying tank, red mud, additive A, B, stirs evenly into slurries, it is filtered that filter cake enters drying machine, heat exchange type is into gas after material after heat exchange and heat exchange, and material forms separation of material and secondary gas solid separation is carried out after secondary heat exchange through gas solid separation after heat exchange, secondary separation material enters rotary kiln, sinter sintering feed into, the sintering feed after exchanging heat and must exchange heat, through dissolving out to obtain dissolution fluid and dissolution slag.The device and method is easy to operate, can obtain distinct economic and reduce environmental pollution.
Description
Technical field：
The invention belongs to regenerated resources technical field of comprehensive utilization, and in particular to one kind extracts aluminium oxide and oxygen from red mud
Change the device and method of sodium.
Background technology：
According to statistics, China's aluminium oxide yield in 2017 is sure to occupy the first in the world more than 66,500,000 tons, is aoxidized by 1t is often prepared
Aluminium averagely generates the calculating of 1.3t red muds, exhausts 86,450,000 tons of red muds.It is averaged by alumina content in Bayer process red mud per ton
25.0%, caustic alkali average content 5.0% calculates, and just wastes within only 2017 21610000 tons of aluminium oxide and 4,320,000 tons of caustic alkali (foldings
Close 13,270,000 tons of 42%NaOH solution), if these useful constituents are not recycled, not only business economic is caused to imitate
Benefit declines, but also can destroy ecological environment.
China Patent No. " a kind of method of red mud comprehensive utilization " disclosed in 201310312592.6, this method is mentioned to
Aluminium oxide and sodium oxide molybdena in recycling red mud, but the hydrochloric acid reaction method of this method, are difficult to industrial practice, reason is exactly
The corrosivity of hydrochloric acid is strong, considerably increases equipment investment, the economic benefit for reducing enterprise.
Therefore, how recycling and cycling and reutilization to greatest extent are carried out to the aluminium oxide in recycling red mud and sodium oxide molybdena,
Achieve the purpose that energy-saving and emission-reduction and increase Business Economic Benefit, be the important topic that faces of each aluminium oxide scientific worker it
One.
The content of the invention：
The purpose of the present invention is overcoming above-mentioned the shortcomings of the prior art, provide one kind extracted from red mud aluminium oxide and
The device and method of sodium oxide molybdena.
To achieve the above object, the present invention uses following technical scheme：
A kind of device that aluminium oxide and sodium oxide molybdena are extracted from red mud, including slurrying tank, filter, drying machine, first is pre-
Hot device, the second preheater, rotary kiln and digester, wherein：
The slurrying tank discharge port is connected with filtering machine inlet；
The filter discharge port is connected with dry machine inlet；
The discharge hole of drying machine is connected with the first preheater feed inlet；
The second preheater gas outlet is connected with drying machine air inlet；
The second preheater feed inlet is connected with rotary kiln gas outlet；
The second preheater discharge port is connected with rotary kiln feed inlet；
The first preheater discharge port is connected to the pipe that rotary kiln gas outlet is connected with the second preheater feed inlet
On road；
The rotary kiln discharge end is connected with digester feed inlet；
The dust-laden exhaust gas of the first preheater gas outlet empties after conventional treatment；
The slurrying tank is set there are four feed inlet, is respectively red mud import, additive A import, additive B import and water
Import；
The digester is set there are two feed inlet and two discharge ports；
Described two feed inlets of digester are respectively material inlet and circulation alkali liquor import, and the digester two goes out
Material mouth is respectively dissolution fluid leakage fluid dram and dissolution slag discharge gate.
The filter is horizontal plate and frame filter press, one kind in vertical type blotter press or horizontal-shaft disk filter；It is preferred that
Ground selects vertical type blotter press.
The drying machine be rapid dryer, specially the horizontal drier with baffle plate or break up in drying machine one
Kind.
The rotary kiln heat source generates heat by coal dust firing and provides, and rotary kiln discharge end is connected with digester feed inlet
Pipeline is equipped with auxiliary air air inlet.
The auxiliary air by the high-temperature material of rotary kiln discharge and recycles the heat in high-temperature material for cooling.
The additive A is carbide slag, one kind in lime or agstone, and the additive B is molten for sodium oxide molybdena
One kind in liquid or piece alkali is preferably piece alkali.
A kind of method that aluminium oxide and sodium oxide molybdena are extracted from red mud, using above device, comprises the following steps：
Step 1, dispensing, pulp and filtering：
(1) water is added in into slurrying tank, starts stirring, and red mud, additive A and additive B is separately added into pulp
Slot is sufficiently stirred mixing, is prepared into slurries, and the aqueous mass percent of the slurries is 33~35%；
(2) slurries enter filter filtering, obtain filter cake and the filtrate, (quality of filter cake moisture content≤25%
Than)；
Step 2, preheat：
(1) filter cake enters drying machine, and granular material is formed under the effect of breaing up, and is carried out in drying machine with dust-laden hot waste gas
Heat exchange forms material and gas after heat exchange after heat exchange, and temperature of charge is 140~170 DEG C after the heat exchange, containing water quality hundred
Divide ratio≤2%, gas temperature is 140~170 DEG C after the heat exchange；
(2) material carries out gas solid separation, forms separation of material and contain with gas after heat exchange into the first preheater after exchanging heat
Dirt exhaust gas, separation of material enter in the pipeline that rotary kiln gas outlet is connected with the second preheater air inlet and with containing heat dust gas
Latter the second preheater of entrance of secondary heat exchange is carried out, carries out secondary gas solid separation, forms secondary separation material and dust-laden heat
Exhaust gas；
Step 3, sintering and dissolution：
(1) secondary separation material enters rotary kiln, is sintered, and is prepared into sintering feed；Wherein, the sintering temperature is
1120~1180 DEG C, material is 40~90min in revolution kiln residence time, and the sintering feed is loose porous, granularity≤
25mm, 1100~1300kg/m of unit weight3；
(2) sintering feed described in after going out rotary kiln, first exchanges heat with auxiliary air, sintering feed and heat exchange after must exchanging heat
Auxiliary air afterwards；
(3) sintering feed enters after digester dissolved out after exchanging heat, and under the action of circulation alkali liquor, obtains dissolution fluid and dissolution
Slag, the dissolution fluid main component are aluminium oxide and sodium oxide molybdena；Wherein, the 20~40min of dissolution time, leaching temperature
70~90 DEG C, additive amount in mass ratio, circulation alkali liquor：Sintering feed=(3~4)：1.
In the step 1 (1), red mud is Bayer process red mud, and the additive A is carbide slag, lime or lime stone
One kind in powder, the additive B are one kind in sodium hydroxide solution or piece alkali.
In the step 1 (1), the chemical composition and mass percent of Bayer process red mud are SiO2：15.94%, Al2O3：
25.45%, Fe2O3：8.55%, CaO：22.15%, Na2O：7.17%, TiO2：9.78%, LOI：8.00%, it is other：
2.96%, the Bayer process red mud attached water mass percent is 35%, the Bayer process red mud fineness -0.074mm matter
Measure percentage composition >=90%.
In the step 1 (1)：The slurry content of preparation meets：Calcium silicon mol ratio [C]/[S]=1.9~2.1, alkali rubs
You are than [N]/([A]+[F])=0.95~1, calcium titanium molar ratio [C]/[T]=1.0.
In the step 1 (2), filtrate is water, returns to slurrying tank and recycles.
In the step 2 (1), dust-laden hot waste gas comes from the second preheater gas outlet, the dust-laden heatrejection
For 500~700 DEG C.
In the step 2 (2), dust-laden exhaust gas empties after conventional purified treatment.
In the step 2 (2), dust-laden hot gas temperature is 800~1000 DEG C, from rotary kiln gas outlet.
In the step 2 (2), dust-laden heatrejection is 500~700 DEG C, and dust-laden hot waste gas, which enters in drying machine, to be used
In progress heat exchange.
In the step 2 (2), secondary separation temperature of charge is 500~700 DEG C, is sintered into rotary kiln.
In the step 3 (1), the heat source of rotary kiln comes from the burning of coal dust.
In the step 3 (2), sintering feed temperature is 750~850 DEG C, and sintering feed temperature is 60~90 DEG C after heat exchange, is changed
Estimated secondary air temperature is 500~600 DEG C after heat.
In the step 3 (2), it is combustion-supporting to enter rotary kiln for auxiliary air after heat exchange.
In the step 3 (3), before sintering feed enters digester after heat exchange, anticipate to granularity≤8mm.
In the step 3 (3), circulation alkali liquor ingredient is Al2O3：37.22g/L Na2Ok：45.34g/L Na2Oc：
19.76g/L α k=2.01；
In the step 3 (3), dissolution fluid ingredient is Al2O3：118.3~130.2g/L, Na2Ok：100~110g/L,
Na2Oc：20~25g/L, SiO2：4~6g/L, α k=1.39.
In the step 3 (3), sodium oxide molybdena net digestion efficiency >=95% in the dissolution fluid, the aluminium oxide is only molten
Extracting rate >=85%, dissolution fluid α k=1.39.
In the step 3 (3), dissolution slag (butt quality ratio) ingredient is SiO2：25.15~25.61%, Al2O3：
2.28~3.42%, Fe2O3：11.97~12.19%, CaO：43.43~44.22%, Na2O：0.39~0.97%, TiO2：
13.36~13.60%, LOI：1.70~1.71%.
In the step 3 (3)：
The dissolution fluid processing mode is：Workshop section and later routine are prepared using the sperm in conventional Bayer process flow
Flow recycles aluminium oxide and sodium oxide molybdena；
The dissolution Slag treatment mode is：Caustic alkali is recycled using filtering red mud washing room in conventional Bayer process flow
It recycles.
Beneficial effects of the present invention：
(1) compared with prior art, exemplified by producing 1,000,000 tons of aluminium oxide year, 286331.5 tons of oxygen can be recycled every year more
Change aluminium, more 52435.5 tons of sodium oxide molybdenas of recycling (being equivalent to 161092.2 tons of the sodium hydroxide that concentration is 42%), economic benefit is shown
It writes；
(2) due to having recycled most alkali in red mud, significantly reduce red mud to soil, underground water, vegetation and
Pollution to ambient enviroment.
Description of the drawings：
Fig. 1 is the apparatus structure schematic diagram that aluminium oxide and sodium oxide molybdena are extracted in the slave red mud of the embodiment of the present invention 1, wherein：
1- slurrying tanks, 2- vertical type blotter press, horizontal driers of the 3- with baffle plate, the first preheaters of 4-, 5- second are preheated
Device, 6- rotary kilns, 7- digesters；A- Bayer process red muds, B- additive As, C- additive Bs, D- coal dusts, E- circulation alkali liquors, F- contain
Dirt exhaust gas, G- dissolution slags, H- dissolution fluids, J- water, K- auxiliary airs, sintering feed after L- heat exchange.
Specific embodiment：
With reference to embodiment, the present invention is described in further detail.
In the description of the present invention, it is necessary to which explanation, unless otherwise clearly defined and limited, term ' connection ' should be done
It broadly understood, for example, it may be being fixedly connected or being detachably connected or be integrally connected；It can be directly connected,
It can also be indirectly connected by intermediary, can also be the connection inside two elements.For the ordinary skill people of this field
For member, the concrete meaning of above-mentioned term in the present invention can be understood with concrete condition.
The present invention is described in further details with specific embodiment below in conjunction with the accompanying drawings, described is the solution to the present invention
It releases rather than limits.
The the first, the second grade descriptions in following embodiment are only used for device feature differentiation, do not represent sequencing；Connection
Mode includes being directly connected to, and a variety of connection modes such as is indirectly connected with；
Carbide slag used, lime, agstone, piece alkali, sodium hydroxide solution are purchased in market, sodium hydroxide solution mass concentration
For 42%.
Embodiment 1
A kind of device that aluminium oxide and sodium oxide molybdena are extracted from red mud, structure diagram is as shown in Figure 1, including slurrying tank
1, vertical type blotter press 2, the horizontal drier 3 with baffle plate, the first preheater 4, the second preheater 5, rotary kiln 6 and digester 7,
Wherein：
The slurrying tank 1 be equipped with discharge port and four feed inlets, respectively with Bayer process red mud import, additive A import,
Additive B import and water inlet, 1 discharge port of slurrying tank are connected with 2 feed inlet of vertical type blotter press；
2 discharge port of vertical type blotter press is connected with 3 feed inlet of horizontal drier with baffle plate；
3 discharge port of horizontal drier with baffle plate is connected with 4 feed inlet of the first preheater；
Second preheater, 5 gas outlet is connected with 3 air inlet of horizontal drier with baffle plate；
Second preheater, 5 feed inlet is connected with 6 gas outlet of rotary kiln；
Second preheater, 5 discharge port is connected with 6 feed inlet of rotary kiln；
First preheater, 4 discharge port is connected to what 6 gas outlet of rotary kiln was connected with 5 feed inlet of the second preheater
On pipeline；
6 discharge end of rotary kiln is connected with 7 feed inlet of digester, 6 discharge end of rotary kiln and digester 7 into
Material mouth connecting pipe is equipped with auxiliary air air inlet；
The digester 7 is set there are two feed inlet and two discharge ports, and two feed inlets are respectively material inlet and follow
Ring lye import, two discharge ports are respectively dissolution fluid leakage fluid dram and dissolution slag discharge gate.
A kind of method that aluminium oxide and sodium oxide molybdena are extracted from red mud, using above device, comprises the following steps：
Step 1, dispensing, pulp and filtering：
(1) water J is added in into slurrying tank 1, starts stirring, and by Bayer process red mud A, carbide slag B and sodium hydroxide solution C
Slurrying tank 1 is separately added into, is sufficiently stirred mixing, is prepared into slurries, the aqueous mass percent of the slurries is 33~35%；Match somebody with somebody
The slurry content of system meets：Calcium silicon mol ratio [C]/[S]=1.9, alkali molar ratio [N]/([A]+[F])=0.95, calcium titanium mole
Than [C]/[T]=1.0；
The chemical composition and mass percent of Bayer process red mud A is SiO2：15.94%, Al2O3：25.45%, Fe2O3：
8.55%, CaO：22.15%, Na2O：7.17%, TiO2：9.78%, LOI：8.00%, it is other：2.96%；The Bayer process
Red mud A attached waters mass percent is 35%, fineness -0.074mm mass percentage >=90%；
(2) slurries enter vertical type blotter press 2 and filter, acquisition filter cake and filtrate, and filter cake moisture content mass percentage≤
25%；Filtrate is water, returns to slurrying tank 1 and recycles；
Step 2, preheat：
(1) filter cake enters the horizontal drier 3 with baffle plate, and granular material is formed under the effect of breaing up, in band baffle plate
Horizontal drier 3 in from 5 air outlet temperature of the second preheater be 500 DEG C dust-laden hot waste gas carry out heat exchange, formed
Temperature is 140 DEG C, and material and temperature are gas after 140 DEG C of heat exchange after the heat exchange of aqueous mass percent≤2%；
(2) material carries out gas solid separation with gas after heat exchange into the first preheater 4 after exchanging heat, formed separation of material and
Dust-laden exhaust gas F, dust-laden exhaust gas F are emptied after conventional purified treatment, and separation of material enters 6 gas outlet of rotary kiln and the second preheater
The heat dust gas that contains for being 800 DEG C in the pipeline that 5 air inlets are connected and with the temperature from 6 gas outlet of rotary kiln carries out second heat
Secondary gas solid separation is carried out into the second preheater 5 together after exchange, forms secondary separation material and temperature that temperature is 500 DEG C
The dust-laden hot waste gas for 500 DEG C is spent, dust-laden hot waste gas, which enters in the horizontal drier 3 with baffle plate, to be used to carry out heat exchange；
Step 3, sintering and dissolution：
(1) secondary separation material enters rotary kiln 6, and providing heat by combusting coal fines D is sintered, and sintering temperature is
1120 DEG C, material residence time in rotary kiln 6 is 90min, is prepared into the sintering feed that temperature is 750 DEG C, the sintering feed
It is loose porous, granularity≤25mm, unit weight 1100kg/m3；
(2) after the sintering feed described in goes out rotary kiln 6, first exchange heat with auxiliary air K, after obtaining the heat exchange that temperature is 60 DEG C
Sintering feed L and temperature are auxiliary air after 500 DEG C of heat exchange, and it is combustion-supporting to enter rotary kiln 6 for auxiliary air after heat exchange；
(3) sintering feed L is anticipated to granularity≤8mm after exchanging heat, into digester 7 under the action of circulation alkali liquor E
Dissolved out, additive amount in mass ratio, circulation alkali liquor E：Sintering feed=3：1, dissolution time 40min, 70 DEG C of leaching temperature, obtain molten
Go out liquid H and dissolution slag G, wherein：
Circulation alkali liquor E ingredients are Al2O3：37.22g/L Na2Ok：45.34g/L Na2Oc：19.76g/L α k=2.01；
Dissolution fluid H ingredients are Al2O3：124.3g/L, Na2Ok：105.0g/L, Na2Oc：25g/L, SiO2：4g/L；Dissolution fluid
Sodium oxide molybdena net digestion efficiency 95% in H, aluminium oxide net digestion efficiency 85%, the α k=1.39 of dissolution fluid H；
Dissolution slag G (butt quality ratio) ingredient is SiO2：25.15%, Al2O3：3.42%, Fe2O3：11.97%, CaO：
43.43%, Na2O：0.97%, TiO2：13.36%, LOI：1.70%；
Dissolution fluid H processing modes are：Workshop section and later old process are prepared using the sperm in conventional Bayer process flow,
Recycle aluminium oxide and sodium oxide molybdena；
Dissolving out slag G processing modes is：Caustic recirculation is recycled using filtering red mud washing room in conventional Bayer process flow
It utilizes.
Embodiment 2
A kind of device of aluminium oxide and sodium oxide molybdena that extracted from red mud of the present embodiment is the same as embodiment 1.
A kind of method that aluminium oxide and sodium oxide molybdena are extracted from red mud, using above device, comprises the following steps：
Step 1, dispensing, pulp and filtering：
(1) water J is added in into slurrying tank 1, starts stirring, and Bayer process red mud A, lime B and piece alkali C is separately added into
Slurrying tank 1, is sufficiently stirred mixing, is prepared into slurries, and the aqueous mass percent of the slurries is 33~35%；The slurries of preparation
Ingredient meets：Calcium silicon mol ratio [C]/[S]=2, alkali molar ratio [N]/([A]+[F])=0.95, calcium titanium molar ratio [C]/[T]=
1.0；
The chemical composition and mass percent of Bayer process red mud A is SiO2：15.94%, Al2O3：25.45%, Fe2O3：
8.55%, CaO：22.15%, Na2O：7.17%, TiO2：9.78%, LOI：8.00%, it is other：2.96%；The Bayer process
Red mud A attached waters mass percent is 35%, fineness -0.074mm mass percentage >=90%；
(2) slurries enter vertical type blotter press 2 and filter, acquisition filter cake and filtrate, and filter cake moisture content mass percentage≤
25%；Filtrate is water, returns to slurrying tank 1 and recycles；
Step 2, preheat：
(1) filter cake enters the horizontal drier 3 with baffle plate, and granular material is formed under the effect of breaing up, in band baffle plate
Horizontal drier 3 in from 5 air outlet temperature of the second preheater be 600 DEG C dust-laden hot waste gas carry out heat exchange, formed
Temperature is 150 DEG C, and material and temperature are gas after 150 DEG C of heat exchange after the heat exchange of aqueous mass percent≤2%；
(2) material carries out gas solid separation with gas after heat exchange into the first preheater 4 after exchanging heat, formed separation of material and
Dust-laden exhaust gas F, dust-laden exhaust gas F are emptied after conventional purified treatment, and separation of material enters 6 gas outlet of rotary kiln and the second preheater
The heat dust gas that contains for being 900 DEG C in the pipeline that 5 air inlets are connected and with the temperature from 6 gas outlet of rotary kiln carries out second heat
Secondary gas solid separation is carried out into the second preheater 5 together after exchange, forms secondary separation material and temperature that temperature is 600 DEG C
The dust-laden hot waste gas for 600 DEG C is spent, dust-laden hot waste gas, which enters in the horizontal drier 3 with baffle plate, to be used to carry out heat exchange；
Step 3, sintering and dissolution：
(1) secondary separation material enters rotary kiln 6, and providing heat by combusting coal fines D is sintered, and sintering temperature is
1150 DEG C, material residence time in rotary kiln 6 is 60min, is prepared into the sintering feed that temperature is 800 DEG C, the sintering feed
It is loose porous, granularity≤25mm, unit weight 1220kg/m3；
(2) after the sintering feed described in goes out rotary kiln 6, first exchange heat with auxiliary air K, after obtaining the heat exchange that temperature is 80 DEG C
Sintering feed L and temperature are auxiliary air after 550 DEG C of heat exchange, and it is combustion-supporting to enter rotary kiln 6 for auxiliary air after heat exchange；
(3) sintering feed L is anticipated to granularity≤8mm after exchanging heat, into digester 7 under the action of circulation alkali liquor E
Dissolved out, additive amount in mass ratio, circulation alkali liquor E：Sintering feed=3：1, dissolution time 30min, 80 DEG C of leaching temperature, obtain molten
Go out liquid H and dissolution slag G, wherein：
Circulation alkali liquor E ingredients are Al2O3：37.22g/L Na2Ok：45.34g/L Na2Oc：19.76g/L α k=2.01；
Dissolution fluid H ingredients are Al2O3：130.2g/L, Na2Ok：110g/L, Na2Oc：22g/L, SiO2：5g/L；Dissolution fluid H
Middle sodium oxide molybdena net digestion efficiency 96%, aluminium oxide net digestion efficiency 88%, the α k=1.39 of dissolution fluid H；
Dissolution slag G (butt quality ratio) ingredient is SiO2：25.38%, Al2O3：2.75%, Fe2O3：12.08%, CaO：
43.83%, Na2O：0.77%, TiO2：13.48%, LOI：1.71%；
Dissolution fluid H processing modes are：Workshop section and later old process are prepared using the sperm in conventional Bayer process flow,
Recycle aluminium oxide and sodium oxide molybdena；
Dissolving out slag G processing modes is：Caustic recirculation is recycled using filtering red mud washing room in conventional Bayer process flow
It utilizes.
Embodiment 3
A kind of device of aluminium oxide and sodium oxide molybdena that extracted from red mud of the present embodiment is the same as embodiment 1.
A kind of method that aluminium oxide and sodium oxide molybdena are extracted from red mud, using above device, comprises the following steps：
Step 1, dispensing, pulp and filtering：
(1) water J is added in into slurrying tank 1, starts stirring, and Bayer process red mud A, agstone B and piece alkali C is distinguished
Slurrying tank 1 is added in, is sufficiently stirred mixing, is prepared into slurries, the aqueous mass percent of the slurries is 33~35%；It prepares
Slurry content meets：Calcium silicon mol ratio [C]/[S]=2.1, alkali molar ratio [N]/([A]+[F])=1, calcium titanium molar ratio [C]/
[T]=1.0；
The chemical composition and mass percent of Bayer process red mud A is SiO2：15.94%, Al2O3：25.45%, Fe2O3：
8.55%, CaO：22.15%, Na2O：7.17%, TiO2：9.78%, LOI：8.00%, it is other：2.96%；The Bayer process
Red mud A attached waters mass percent is 35%, fineness -0.074mm mass percentage >=90%；
(2) slurries enter vertical type blotter press 2 and filter, acquisition filter cake and filtrate, and filter cake moisture content mass percentage≤
25%；Filtrate is water, returns to slurrying tank 1 and recycles；
Step 2, preheat：
(1) filter cake enters the horizontal drier 3 with baffle plate, and granular material is formed under the effect of breaing up, in band baffle plate
Horizontal drier 3 in from 5 air outlet temperature of the second preheater be 700 DEG C dust-laden hot waste gas carry out heat exchange, formed
Temperature is 170 DEG C, and material and temperature are gas after 170 DEG C of heat exchange after the heat exchange of aqueous mass percent≤2%；
(2) material carries out gas solid separation with gas after heat exchange into the first preheater 4 after exchanging heat, formed separation of material and
Dust-laden exhaust gas F, dust-laden exhaust gas F are emptied after conventional purified treatment, and separation of material enters 6 gas outlet of rotary kiln and the second preheater
It is in the pipeline that 5 air inlets are connected and secondary for 1000 DEG C of progress containing heat dust gas with the temperature from 6 gas outlet of rotary kiln
Together into the second preheater 5 after heat exchange, carry out secondary gas solid separation, is formed secondary separation material that temperature is 700 DEG C with
Temperature is 700 DEG C of dust-laden hot waste gas, and dust-laden hot waste gas, which enters in the horizontal drier 3 with baffle plate, to be used to carry out heat exchange；
Step 3, sintering and dissolution：
(1) secondary separation material enters rotary kiln 6, and providing heat by combusting coal fines D is sintered, and sintering temperature is
1180 DEG C, material residence time in rotary kiln 6 is 40min, is prepared into the sintering feed that temperature is 850 DEG C, the sintering feed
It is loose porous, granularity≤25mm, unit weight 1300kg/m3；
(2) after the sintering feed described in goes out rotary kiln 6, first exchange heat with auxiliary air K, after obtaining heat exchange at a temperature of 90 °C
Sintering feed L and temperature are auxiliary air after 600 DEG C of heat exchange, and it is combustion-supporting to enter rotary kiln 6 for auxiliary air after heat exchange；
(3) sintering feed L is anticipated to granularity≤8mm after exchanging heat, into digester 7 under the action of circulation alkali liquor E
Dissolved out, additive amount in mass ratio, circulation alkali liquor E：Sintering feed=4：1, dissolution time 20min, 90 DEG C of leaching temperature, obtain molten
Go out liquid H and dissolution slag G, wherein：
Circulation alkali liquor E ingredients are Al2O3：37.22g/L Na2Ok：45.34g/L Na2Oc：19.76g/L α k=2.01；
Dissolution fluid H ingredients are Al2O3：118.3g/L, Na2Ok：100g/L, Na2Oc：20g/L, SiO2：6g/L；Dissolution fluid H
Middle sodium oxide molybdena net digestion efficiency 98%, aluminium oxide net digestion efficiency 90%, the α k=1.39 of dissolution fluid H；
Dissolution slag G (butt quality ratio) ingredient is SiO2：25.61%, Al2O3：2.28%, Fe2O3：12.19%, CaO：
44.22%, Na2O：0.39%, TiO2：13.60%, LOI：1.71%；
Dissolution fluid H processing modes are：Workshop section and later old process are prepared using the sperm in conventional Bayer process flow,
Recycle aluminium oxide and sodium oxide molybdena；
Dissolving out slag G processing modes is：Caustic recirculation is recycled using filtering red mud washing room in conventional Bayer process flow
It utilizes.
Claims (10)
1. a kind of device that aluminium oxide and sodium oxide molybdena are extracted from red mud, which is characterized in that including slurrying tank, filter, drying
Machine, the first preheater, the second preheater, rotary kiln and digester, wherein：
The slurrying tank discharge port is connected with filtering machine inlet；
The filter discharge port is connected with dry machine inlet；
The discharge hole of drying machine is connected with the first preheater feed inlet；
The second preheater gas outlet is connected with drying machine air inlet；
The second preheater feed inlet is connected with rotary kiln gas outlet；
The second preheater discharge port is connected with rotary kiln feed inlet；
The first preheater discharge port is connected on the pipeline that rotary kiln gas outlet is connected with the second preheater feed inlet；
The rotary kiln discharge end is connected with digester feed inlet；
The dust-laden exhaust gas of the first preheater gas outlet empties after conventional treatment；
The slurrying tank is set there are four feed inlet, is respectively red mud import, additive A import, additive B import and water inlet
Connection；
The digester is set there are two feed inlet and two discharge ports；
Described two feed inlets of digester are respectively material inlet and circulation alkali liquor import, described two discharge ports of digester
Respectively dissolution fluid leakage fluid dram and dissolution slag discharge gate.
2. the device according to claim 1 that aluminium oxide and sodium oxide molybdena are extracted from red mud, which is characterized in that the mistake
Filter is horizontal plate and frame filter press, one kind in vertical type blotter press or horizontal-shaft disk filter；The drying machine is fast rapid-curing cutback
Dry machine specially the horizontal drier with baffle plate or breaks up one kind in drying machine.
3. a kind of method that aluminium oxide and sodium oxide molybdena are extracted from red mud, using device described in claim 1, feature exists
In comprising the following steps：
Step 1, dispensing, pulp and filtering：
(1) water is added in into slurrying tank, starts stirring, and red mud, additive A and additive B are separately added into slurrying tank, is filled
Divide and stir and evenly mix, be prepared into slurries, the aqueous mass percent of the slurries is 33~35%；
(2) slurries enter filter filtering, obtain filter cake and filtrate, (mass ratio) of filter cake moisture content≤25%；
Step 2, preheat：
(1) filter cake enters drying machine, and granular material is formed under the effect of breaing up, and hot friendship is carried out with dust-laden hot waste gas in drying machine
It changes, forms material and gas after heat exchange after heat exchange, temperature of charge is 140~170 DEG C after the heat exchange, aqueous mass percent
Gas temperature is 140~170 DEG C after heat exchange described in≤2%；
(2) material carries out gas solid separation, forms separation of material and dust-laden gives up with gas after heat exchange into the first preheater after exchanging heat
Gas, the first preheater separation of material enters in the pipeline that rotary kiln gas outlet is connected with the second preheater air inlet and and dust-laden
Hot gas carries out secondary latter the second preheater of entrance of heat exchange, carries out secondary gas solid separation, formed secondary separation material and
Dust-laden hot waste gas；
Step 3, sintering and dissolution：
(1) secondary separation material enters rotary kiln, is sintered, and is prepared into sintering feed；Wherein, the sintering temperature is 1120
~1180 DEG C, material is 40~90min in revolution kiln residence time, and the sintering feed is loose porous, granularity≤25mm, is held
Weigh 1100~1300kg/m3；
(2) sintering feed described in after going out rotary kiln, first exchanges heat with auxiliary air, sintering feed and after heat exchange two after must exchanging heat
Secondary air；
(3) sintering feed enters digester and is dissolved out after exchanging heat, and under the action of circulation alkali liquor, obtains dissolution fluid and dissolution slag, institute
The dissolution fluid main component stated is aluminium oxide and sodium oxide molybdena；Wherein, the 20~40min of dissolution time, leaching temperature 70~
90 DEG C, additive amount in mass ratio, circulation alkali liquor：Sintering feed=(3~4)：1.
4. the method according to claim 3 that aluminium oxide and sodium oxide molybdena are extracted from red mud, which is characterized in that the step
In rapid 3 (2), sintering feed temperature is 750~850 DEG C, and sintering feed temperature is 60~90 DEG C after heat exchange, estimated secondary air temperature after heat exchange
For 500~600 DEG C.
5. the method according to claim 3 that aluminium oxide and sodium oxide molybdena are extracted from red mud, which is characterized in that the step
In rapid 1 (1), red mud is Bayer process red mud, and the additive A is one kind in carbide slag, lime or agstone, described
Additive B is one kind in sodium hydroxide solution or piece alkali.
6. the method according to claim 3 that aluminium oxide and sodium oxide molybdena are extracted from red mud, which is characterized in that the step
In rapid 1 (1), the chemical composition and mass percent of Bayer process red mud are SiO2：15.94%, Al2O3：25.45%, Fe2O3：
8.55%, CaO：22.15%, Na2O：7.17%, TiO2：9.78%, LOI：8.00%, it is other：2.96%, the Bayer process
Red mud attached water mass percent is 35%, Bayer process red mud fineness -0.074mm mass percentage >=90%.
7. the method according to claim 3 that aluminium oxide and sodium oxide molybdena are extracted from red mud, which is characterized in that the step
Suddenly in (1)：The slurry content of preparation meets：Calcium silicon mol ratio [C]/[S]=1.9~2.1, alkali molar ratio [N]/([A]+[F])
=0.95~1, calcium titanium molar ratio [C]/[T]=1.0.
8. the method according to claim 3 that aluminium oxide and sodium oxide molybdena are extracted from red mud, which is characterized in that the step
In rapid 3 (3), circulation alkali liquor ingredient is Al2O3：37.22g/L Na2Ok：45.34g/L Na2Oc：19.76g/L α k=2.01；
Dissolution fluid ingredient is Al2O3：118.3~130.2g/L, Na2Ok：100~110g/L, Na2Oc：20~25g/L, SiO2：4~6g/
L。
9. the method according to claim 3 that aluminium oxide and sodium oxide molybdena are extracted from red mud, which is characterized in that the step
In rapid 3 (3), sodium oxide molybdena net digestion efficiency >=95% in the dissolution fluid, aluminium oxide net digestion efficiency >=85%, dissolution fluid
α k=1.39.
10. the method according to claim 5 that aluminium oxide and sodium oxide molybdena are extracted from red mud, which is characterized in that described
In step 3 (3), dissolution slag (butt quality ratio) ingredient is SiO2：25.15~25.61%, Al2O3：2.28~3.42%,
Fe2O3：11.97~12.19%, CaO：43.43~44.22%, Na2O：0.39~0.97%, TiO2：13.36~13.60%,
LOI：1.70~1.71%.
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Application publication date: 20180529 |