CN101045559A - Method for producing sodium chromate non-calcium calcined by ferrochrome mine - Google Patents
Method for producing sodium chromate non-calcium calcined by ferrochrome mine Download PDFInfo
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Abstract
A process for preparing sodium chrominate by non-Ca calcination of chromite includes such steps as mixing chromite, sodium carbonate and returned dregs, calcining in rotary kiln, wet separation (wet grinding, cyclone liquid separation, and filtering while washing to obtain the alkaline solution of sodium chromate) or dry separation (extracting in bath, pneumatic separation, and separating powder), neutralizing said alkaline solution, removing aluminum hydroxide containing 6-valence Cr ions to obtain neutral solution of sodium chromate, further processing to obtain sodium bichromate, preparing alumina from the recovered aluminum hydroxide, and preparing chromium black pigment from coarse dregs.
Description
Technical field the present invention relates to a kind of method of being produced Sodium chromate by chromite through calcium-free roasting.
Background technology industry Sodium chromate method for making is in the presence of filler, chromite is mixed the back with yellow soda ash carry out oxidizing roasting in rotary kiln, makes Cr in the ore deposit
2O
3Be oxidized to Sodium chromate Na
2CrO
4Roasting grog water dissolution, the chromium acid sodium solution that obtains further are processed into sodium dichromate 99, chromium hydroxide or other chromium cpds, and insoluble part is called the chromium slag.
Because about 1100 ℃ of roasting optimum temps, and only 655 ℃ of eutectic mixture fusing points that raw material yellow soda ash and product Sodium chromate form, this liquation covers unreacted chromite particle surface, both having hindered oxidizing reaction proceeds, make the serious sintering of furnace charge again and stick to the rotary kiln inwall, form accretion.In general, furnace charge liquation content surpasses at 30% o'clock, and a large amount of accretions just are deposited on the rotary kiln inwall, form ring-type accretion---ring formation, seriously stops the furnace charge reach, and roasting process can't be continued.Filler claims liquation thinner or liquation dispersion agent again, and its effect is brought down below 30% with furnace charge liquation content on the one hand, reduces accretion and generates, and avoids ring formation; On the other hand most of liquation is dispersed in filling surface, makes the liquid film attenuate that covers unreacted chromite surface, be beneficial to oxygen and arrive unreacted chromite surface, the assurance oxidizing reaction is constantly carried out.
The traditional chromic acid process for producing sodium is called the calcium sinter process, use rhombspar, Wingdale or calcium cpds such as unslaked lime, white lime to make filler, these calcareous fillers generate periclasite, Calucium Silicate powder and the iron calcium aluminate that fusing point is higher than maturing temperature when roasting, be good liquation dispersion agent.But calcareous filler is also with chromium generation side reaction under maturing temperature, generation has the yellow ultramarine of carcinogenic danger, and the yellow ultramarine under the high temperature can enter the crystal of Calucium Silicate powder, iron calcium aluminate---form sosoloid, after grog leaching, just enter environment, in 1.5～2.5 tons of chromium slags of sodium dichromate 99 product discharging per ton (look chromite grade and calcium cpd kind and different) with the chromium slag.The yellow ultramarine of sosoloid form solubleness in water is little in the chromium slag, but be dissolved in acid (comprising the acidated water of carbonic acid gas), be called sour molten sexavalent chrome, when the chromium slag is exposed in the atmosphere, under the effect of carbonic acid gas and water, along with the aquation (weathering) of Calucium Silicate powder, iron calcium aluminate, the intravital yellow ultramarine of solid solution dissociates out, or be dissolved in surface water, underground water, or be involved in atmosphere by wind, thus contaminate environment.
Prior art is mixed the chromium slag of chromite, yellow soda ash and not sorting, adds the promotor SODIUMNITRATE, with roasting behind the alkaline solution mist projection granulating.Because the not sorting of chromium slag causes detrimental impurity (to be dissolved with Al, Mg, the water glass Na of Fe with amorphous substance
2SiO
3) form constantly accumulation in the chromium slag (increase with geometric progression increase with cycle index), and amorphous substance temperature about 500 ℃ promptly softening, and the rapid fusion of following temperature rising, even accretion and ring formation still appear in the furnace charge granulation, rotary kiln can not steady running; And add promotor and alkaline solution granulation (and pellet drying) and increased operation, increased cost.
Summary of the invention the object of the invention provides a kind of method of being produced Sodium chromate by chromite through calcium-free roasting.
First kind of embodiment of the present invention is wet separation, comprises the following steps:
A, batch mixing: the return slag that chromite, yellow soda ash and sorting are obtained mixes, and uniformity coefficient reaches 99%, and each raw material is consisting of of percentage composition meter by weight, chrome ore 25～28%, yellow soda ash 20～23%, sorting return slag 50～55%;
B, roasting: in rotary kiln, carry out oxidizing roasting, 560～700 ℃ of kiln end temperatures, 1100～1150 ℃ of high temperature zone temperatures, material was kiln residence time 240～260 minutes;
C, wet-milling: the grog that roasting obtains enters the wet-type ball mill grinding through being cooled to 350～400 ℃, liquid-solid ratio (65～70): (35～30); Be 80～120mm with ball radius in the wet-milling, preferred ball radius is 90～110mm.Make that the size-grade distribution of slag is after the wet-milling: 100 orders account for 15～30%, account for 40～65%, 200 orders between 100 orders and 200 orders and account for 20～40%.The size-grade distribution of slag is preferably after the wet-milling, and 100 orders account for 20～25%, accounts for 45～60%, 200 orders between 100 orders and 200 orders and accounts for 25～30%.The size-grade distribution of slag most preferably is after the wet-milling, and 100 orders account for 18～22%, accounts for 48～52%, 200 orders between 100 orders and 200 orders and accounts for 28～32%.
D, spinning liquid separate: the slip behind the grinding enters cyclone classification, and thick slurry flows out from the bottom, and screened stock overflows from the top; Be Φ 120～Φ 180mm with the waterpower cyclone diameter during spinning liquid separates, intake pressure is 0.2～0.5MPa.Cyclone diameter is preferably Φ 140～Φ 160mm, and intake pressure is preferably 0.2～0.3MPa, and thick slurry: the weight ratio of screened stock is (60～65): (35～40), and thick slurry: the weight ratio of screened stock is preferably 3: 1,
E, diafiltration: the thickness slurry carries out diafiltration with filter respectively, and filter is selected from band filter, drum filter or automatic pressure filter, and strainer speed is 1.5～2 meters/minute, carries out the continuous diafiltration of Pyatyi with band filter in the diafiltration.Filtrate is chromium acid sodium alkaline liquid, and thick slag is as the return slag circular batching, and the grog that wash water and roasting obtain is sent into ball mill continuously and carried out wet-milling.
Second kind of embodiment of the present invention is dry-type separation, comprises the following steps:
A, batch mixing: the return slag that chromite, yellow soda ash and sorting are obtained mixes, and uniformity coefficient reaches 99%, and each raw material is consisting of of percentage composition meter by weight, chrome ore 25～28%, yellow soda ash 20～23%, sorting return slag 50～55%;
B, roasting: in rotary kiln, carry out oxidizing roasting, 560～590 ℃ of kiln end temperatures, 1100～1150 ℃ of high temperature zone temperatures, material was kiln residence time 240～260 minutes;
The leaching of C, slot type: the grog that roasting obtains is delivered to steel tank and is soaked and diafiltration with rare chromium acid sodium solution through being cooled to 350～400 ℃, goes into the ball mill grinding after the filter residue drying, controls grinding machine fineness 200 orders of slagging tap and accounts for 85～90%, and 100 orders account for 10～15%; The temperature that is used to steep the last time wash water of washing in the slot type leaching is 80～90 ℃, and it is 6～12 times that bubble is washed number of times, and bubble is washed number of times and is preferably 8～10 times.
D, selection by winnowing: go out to grind slag and enter the powder selector sorting, 1000～1500 rev/mins of control powder selector rotor speeds, air quantity 10000～16000m
3/ h, blast 2000～3000Pa;
After E, the powder selector sorting, thin slag accounts for 35～45% and effluxes, and thick slag accounts for 60～65%, returns batching.
The present invention utilizes x-ray analysis and chemical phase analysis (selective dissolution analytical method), finds that calcium-free roasting chromium slag is mainly by 5 kinds of thing phase composites of following table.
| The thing phase | Form | Fusing point ℃ | Relative proportion | Magnetic | Solubility in acid |
| Chromite | Mg[Cr，Al，Fe] 2O 4 | ～1700 | 4.75 | A little less than | Diluted acid is insoluble |
| Magnesioferrite | Mg[Fe，Al] 2O 4 | 1750 | 4.5 | By force | Diluted acid is insoluble |
| Periclasite | MgO | 2800 | 3.58 | Do not have | Be dissolved in diluted acid |
| Aluminum magnesium silicate sodium | Na-4MgAl-2Si-3 O-1-2 | ＞1200 | ～3 | Do not have | Be dissolved in diluted acid |
| Amorphous substance | Be dissolved with Al, Mg, the Na-2SiO-3 of Fe | ～3 | Do not have | Be dissolved in diluted acid |
Unreacted chromite, magnesioferrite and periclasite fusing point all are much higher than maturing temperature in the table, are suitable for doing filler, and the fusing point of aluminum magnesium silicate sodium and amorphous substance is a little higher than or be lower than maturing temperature, is to try hard in the filler avoid.The purpose of sorting is to remove aluminum magnesium silicate sodium and amorphous substance, reclaims dystectic chromite, magnesioferrite is made filler (being called return slag).If the not sorting of chromium slag directly recycles, because aluminum magnesium silicate sodium easily generates the new water glass that is in the liquation state at maturing temperature with yellow soda ash reaction, not only increase liquation amount in the furnace charge, and aluminium, magnesium, iron (comprising aluminum magnesium silicate sodium itself) in the furnace charge can also be fused in the liquation, the danger of furnace charge sintering, ring formation increases, even the inadequate kiln discharge of such furnace charge, amorphous substance content is more in the slag of leaching back, if still not sorting, its carrier performance from smoke into smother.
This shows, soak the whether quality of sorting and separating effect of slag, is the key that can calcium-free roasting normal circulation steady running.
As seen from the above table, utilize magnetic separation, gravity treatment or acid choosing, can make return slag, tailings or sour molten part detoxifcation back discharging after the magnesioferrite of filler and the unreacted chromite enrichment being suitable for doing.
The present invention mixes chromite, yellow soda ash and return slag, carries out oxidizing roasting in rotary kiln.After the grog that roasting obtains is handled, obtain chromium acid sodium alkaline liquid, thick slag and thin slag respectively.Chromium acid sodium alkaline liquid is removed aluminium mud (containing chromic aluminium hydroxide) through neutralization, and filtrate is the Sodium chromate neutral solution, further is processed into sodium dichromate 99; Aluminium mud is made electrolytic metal aluminium aluminum oxide after reclaiming sexavalent chrome.Thick slag is as filler (return slag) circular batching.Thin slag detoxifcation is potting porcelain black pigment---chrome black afterwards, also can smelt to become to contain chromium pig iron.
Grog is 560～700 ℃ in the temperature of rotary kiln outlet, is not of uniform size spherical, and surface coverage thickness by the liquations of some microns near millimeter, and liquation is made of the aluminium that fuses under Sodium chromate-yellow soda ash-sodium silicate mixture and the high temperature, magnesium, iron.Grog is in the process of cooling behind kiln, separate out the crystal Sodium chromate rapidly and be deposited on particle surfaces such as magnesioferrite, unreacted chromite, periclasite, if speed of cooling is slow, also the part silicon, aluminium, magnesium, the iron that fuse into can be separated out with crystal aluminum magnesium silicate sodium and magnesioferrite form, the then remaining liquation of continuation cooling hardens gradually and forms amorphous substance---the molten glassy shell that aluminium, magnesium, iron are arranged in the water glass matrix.
First kind of embodiment of the present invention is wet separation.
After the grog cooling, send into ball mill continuously together with the wash water after the diafiltration, in ball mill, abrading-ball is peeled off with the dissolving of Sodium chromate the fragmentation of stiff glass shell and is mutually promoted synchronously, has quickened leaching process and has improved leaching yield.Grating---the diameter and the relative quantity of abrading-ball of abrading-ball in the control ball mill, ball radius is advisable (100mm ± 10mm is better) with 80～120mm, and sphere diameter is crossed senior general and is reduced the Sodium chromate leaching rate, causes slag and contains the sexavalent chrome height; Cross the young pathbreaker and wear into a large amount of ultrafine powders, reduce the wet cyclone separating effect, and reduce diafiltration speed, increase thin slag band and decrease.Slurries behind the mill are delivered to hydrocyclone with slush pump and are carried out the spinning liquid separation.The hydrocyclone specification is decided with throughput, and as if 10,000 tons/year of sodium dichromate 99 throughput, should select diameter for use is the hydrocyclone of 120～180mm (150mm ± 10mm is better).Thick dreg slurry flows out from swirler end opening (gape), and thin dreg slurry is discharged from swirler (overflow port) suitable for reading.Because thick, thin slag all is grittiness, very easily diafiltration, the intensity filter during vacuum tightness 500mmHg reaches filtrate 2.08m
3/ m
2H can use high-intensity diafiltration machinery, as band filter, and drum filter, automatic pressure filter.More suitable with level of automation height, less investment, band filter that working cost is cheap.Slurries send band filter to carry out continuous diafiltration respectively, and thick, screened stock filtrate (alkali solution) merging is sent to neutralization and removes aluminium.Thick slag contains total chromium 6～7.5%, and sexavalent chrome 0.1～0.3% (all is accustomed to Cr by present chromium salt factory
2O
3Meter, down together), dry back is as the return slag circular batching.Thin slag contains total chromium 5～6%, sexavalent chrome 0.1～0.2%, the comprehensive utilization of detoxifcation back.
Second kind of embodiment of the present invention is dry-type separation.
Send into the steel tank that is covered with orifice plate and woven wire after grog is cold, soak and diafiltration with rare chromium acid sodium solution (adverse current washes out water).Because there is the hard glass mass shell of one deck on the grog surface, this shell constitutes by being difficult to water-soluble amorphous substance, must use hot wash water adverse current washing by soaking repeatedly.Water temperature should be hot to 80 ℃ or higher, if water temperature is low, leaching speed is slow; Bubble is washed number of times suitable 6～12 times (8～10 times better), and number of times is few, and it is low that sexavalent chrome leaches yield.Diafiltration liquid goes out through the control dry tap.The Extract that first and second time concentration is high is an alkali solution, sends to neutralization and removes aluminium.Slag drying after washing is thick, thin slag with the levigate back of ball mill with the powder selector cyclonic separation.The requirement of powder selector is: 1000～1500 rev/mins of rotor speeds, air quantity 10000～16000m
3/ h, blast 2000～3000Pa.The thick slag that obtains contains total chromium: 10～14%, and sexavalent chrome 0.3～0.5%, circulation is as return slag; Thin slag contains total chromium: 5～8%, and sexavalent chrome 0.3%, the comprehensive utilization of detoxifcation back.
The present invention carries out sorting to the chromium slag, makes rotary kiln accretion and ring formation not occur, energy steady running; Simplify operation, reduced cost.
Description of drawings Fig. 1 is the schema of first kind of embodiment of the present invention;
Fig. 2 is the schema of second kind of embodiment of the present invention.
The embodiment the following examples can make those skilled in the art more fully understand the present invention, but do not limit the present invention in any way.
Embodiment 1: wet separation (contains Cr by chrome ore
2O
343%) 25%, yellow soda ash 20%, sorting return slag 50% proportioning is through mixing material, after uniformity coefficient reaches 99%, go into rotary kiln baking, 560 ℃ of kiln end temperatures, 1100 ℃ of high temperature zone temperatures, material was kiln residence time 240 minutes, and grog enters the wet-type ball mill grinding through being cooled to 350 ℃.Select suitable steel ball grating, assurance material fineness 100 orders account between 15%, 100 order and 200 orders and account for 40%, 200 orders account for 20%, liquid-solid ratio 65: 35, and the slip behind the grinding enters cyclone classification, cyclone diameter Φ 120mm keeps intake pressure 0.2MPa, thickness slurry weight ratio 60: 35.Thick slurry flows out from the bottom, and screened stock overflows from the top.Main useful composition Cr, Fe enrichment in the thick slurry, oxious component Si reduces, and helps the utilization again of roasting and Cr, Fe composition; Main useful composition Cr, Fe reduce in the thin slag, and oxious component Si raises.After the spinning liquid classification, the thickness slurry that obtains carries out the Pyatyi diafiltration with band filter respectively, 1.5 meters/minute of strainer speed.Filtrate is chromium acid sodium alkaline liquid, contains Sodium chromate Na
2CrO
4300～350g/l, free alkali is (with Na
2Co
3Meter) 10～15g/L.
Embodiment 2: (contain Cr by chrome ore
2O
343%) 28%, yellow soda ash 23%, sorting return slag 55% proportioning is through mixing material, after uniformity coefficient reaches 99%, go into rotary kiln baking, 700 ℃ of kiln end temperatures, 1150 ℃ of high temperature zone temperatures, material was kiln residence time 260 minutes, and grog enters the wet-type ball mill grinding through being cooled to 400 ℃.Select suitable steel ball grating, assurance material fineness 100 orders account between 30%, 100 order and 200 orders and account for 65%, 200 orders account for 40%, liquid-solid ratio 70: 30, and the slip behind the grinding enters cyclone classification, cyclone diameter Φ 180mm keeps intake pressure 0.5MPa, thickness slurry weight ratio 65: 40.Thick slurry flows out from the bottom, and screened stock overflows from the top.After the spinning liquid classification, the thickness slurry that obtains carries out the Pyatyi diafiltration with band filter respectively, 2 meters/minute of strainer speed.
Embodiment 3: (contain Cr by chrome ore
2O
343%) 26%, yellow soda ash 21%, sorting return slag 52% proportioning is through mixing material, after uniformity coefficient reaches 99%, go into rotary kiln baking, 630 ℃ of kiln end temperatures, 1120 ℃ of high temperature zone temperatures, material was kiln residence time 250 minutes, and grog enters the wet-type ball mill grinding through being cooled to 370 ℃.Select suitable steel ball grating, assurance material fineness 100 orders account between 18%, 100 order and 200 orders and account for 45%, 200 orders account for 25%, liquid-solid ratio 67: 33, and the slip behind the grinding enters cyclone classification, cyclone diameter Φ 140mm keeps intake pressure 0.3MPa, thickness slurry weight ratio 62: 37.Thick slurry flows out from the bottom, and screened stock overflows from the top.After the spinning liquid classification, the thickness slurry that obtains carries out the Pyatyi diafiltration with band filter respectively, 1.7 meters/minute of strainer speed.
Embodiment 4:
(contain Cr by chrome ore
2O
343%) 27%, yellow soda ash 22%, sorting return slag 53% proportioning is through mixing material, after uniformity coefficient reaches 99%, go into rotary kiln baking, 600 ℃ of kiln end temperatures, 1130 ℃ of high temperature zone temperatures, material was kiln residence time 255 minutes, and grog enters the wet-type ball mill grinding through being cooled to 380 ℃.Select suitable steel ball grating, assurance material fineness 100 orders account between 22%, 100 order and 200 orders and account for 60%, 200 orders account for 30%, liquid-solid ratio 68: 34, and the slip behind the grinding enters cyclone classification, cyclone diameter Φ 160mm keeps intake pressure 0.4MPa, thickness slurry weight ratio 63: 38.Thick slurry flows out from the bottom, and screened stock overflows from the top.After the spinning liquid classification, the thickness slurry that obtains carries out the Pyatyi diafiltration with band filter respectively, 1.8 meters/minute of strainer speed.
Embodiment 5: wet separation
Repeat embodiment 1, following difference is arranged: select suitable steel ball grating, guarantee that material fineness 100 orders account for to account for 48%, 200 order between 20%, 100 order and 200 orders and account for 28%.
Embodiment 6: wet separation
Repeat embodiment 1, following difference is arranged: select suitable steel ball grating, guarantee that material fineness 100 orders account for to account for 52%, 200 order between 25%, 100 order and 200 orders and account for 32%.
Embodiment 7: dry-type separation
(contain Cr by chrome ore
2O
343%) 25%, yellow soda ash 20%, slag 50% proportioning is through mixing material, after uniformity coefficient reaches 99%, go into rotary kiln baking, 560 ℃ of kiln end temperatures of control, 1100 ℃ of high temperature zone temperatures, material was kiln residence time 240 minutes, grog enters the vat leaching through being cooled to 350 ℃, goes into the ball mill grinding after the slag drying.Control grinding machine fineness 200 orders of slagging tap account for 85%, 100 order and account for 10%, go out to grind slag and enter the powder selector sorting, 1000 rev/mins of control powder selector rotor speeds, air quantity 10000m
3/ h, blast 2000Pa.After the powder selector sorting, thin slag accounts for 35% and effluxes, and thick slag accounts for 60%, returns batching.Main useful composition Cr, Fe enrichment in the thick slag, oxious component Si reduces, and helps the utilization again of roasting and Cr, Fe composition; Main useful composition Cr, Fe reduce in the thin slag, and oxious component Si raises.Chromium acid sodium alkaline liquid further is processed into sodium dichromate 99 or other chromium cpds, thin slag detoxifcation back comprehensive utilization.
Embodiment 8: dry-type separation
(contain Cr by chrome ore
2O
343%) 28%, yellow soda ash 23%, slag 55% proportioning is through mixing material, after uniformity coefficient reaches 99%, go into rotary kiln baking, 590 ℃ of kiln end temperatures of control, 1150 ℃ of high temperature zone temperatures, material was kiln residence time 260 minutes, grog enters the vat leaching through being cooled to 400 ℃, goes into the ball mill grinding after the slag drying.Control grinding machine fineness 200 orders of slagging tap account for 90%, 100 order and account for 15%, go out to grind slag and enter the powder selector sorting, 1500 rev/mins of control powder selector rotor speeds, air quantity 16000m
3/ h, blast 000Pa.After the powder selector sorting, thin slag accounts for 45% and effluxes, and thick slag accounts for 65%, returns batching.Main useful composition Cr, Fe enrichment in the thick slag, oxious component Si reduces, and helps the utilization again of roasting and Cr, Fe composition; Main useful composition Cr, Fe reduce in the thin slag, and oxious component Si raises.Chromium acid sodium alkaline liquid further is processed into sodium dichromate 99 or other chromium cpds, thin slag detoxifcation back comprehensive utilization.
Claims (9)
1, a kind of method of producing Sodium chromate by chromite through calcium-free roasting, it is characterized in that: it comprises the following steps: A, batch mixing: the return slag that chromite, yellow soda ash and sorting are obtained mixes, uniformity coefficient reaches 99%, each raw material is consisting of of percentage composition meter by weight, chrome ore 25～28%, yellow soda ash 20～23%, sorting return slag 50～55%;
B, roasting: in rotary kiln, carry out oxidizing roasting, 560～700 ℃ of kiln end temperatures, 1100～1150 ℃ of high temperature zone temperatures, material was kiln residence time 240～260 minutes;
C, wet-milling: the grog that roasting obtains enters the wet-type ball mill grinding through being cooled to 350～400 ℃, liquid-solid ratio (65～70): (35～30);
D, spinning liquid separate: the slip behind the grinding enters cyclone classification, and thick slurry flows out from the bottom, and screened stock overflows from the top;
E, diafiltration: the thickness slurry carries out diafiltration with filter respectively, filter is selected from band filter, drum filter or automatic pressure filter, strainer speed is 1.5～2 meters/minute, filtrate is chromium acid sodium alkaline liquid, thick slag is as the return slag circular batching, and the grog that wash water and roasting obtain is sent into ball mill continuously and carried out wet-milling.
2, method of producing Sodium chromate by chromite through calcium-free roasting according to claim 1, it is characterized in that: be 80～120mm with ball radius in the described step C wet-milling, make that the size-grade distribution of slag is after the wet-milling: 100 orders account for 15～30%, account for 40～65%, 200 orders between 100 orders and 200 orders and account for 20～40%.
3, method of producing Sodium chromate by chromite through calcium-free roasting according to claim 1 and 2, it is characterized in that: be 90～110mm with ball radius in the described step C wet-milling, the size-grade distribution of slag is after the wet-milling, 100 orders account for 20～25%, account for 45～60%, 200 orders between 100 orders and 200 orders and account for 25～30%.
4, method of producing Sodium chromate through calcium-free roasting according to claim 3 by chromite, it is characterized in that: the size-grade distribution of slag is after the described step C wet-milling, and 100 orders account for 18～22%, accounts for 48～52%, 200 orders between 100 orders and 200 orders and accounts for 28～32%; The hydrocyclone diameter was Φ 120～Φ 180mm during step D spinning liquid separated, and intake pressure is 0.2～0.5MPa.
5, method of producing Sodium chromate by chromite through calcium-free roasting according to claim 4, it is characterized in that: the hydrocyclone diameter was Φ 140～Φ 160mm during step D spinning liquid separated, intake pressure is 0.2～0.3MPa, and thick slurry: the weight ratio of screened stock is (60～65): (35～40).
6, method of producing Sodium chromate through calcium-free roasting by chromite according to claim 5, it is characterized in that: slightly starch during step D spinning liquid separates: the weight ratio of screened stock is 3: 1, carries out the continuous diafiltration of Pyatyi with band filter in the step e diafiltration.
7, a kind of method of producing Sodium chromate by chromite through calcium-free roasting, it is characterized in that: it comprises the following steps: A, batch mixing: the return slag that chromite, yellow soda ash and sorting are obtained mixes, uniformity coefficient reaches 99%, each raw material is consisting of of percentage composition meter by weight, chrome ore 25～28%, yellow soda ash 20～23%, sorting return slag 50～55%;
B, roasting: in rotary kiln, carry out oxidizing roasting, 560～590 ℃ of kiln end temperatures, 1100～1150 ℃ of high temperature zone temperatures, material was kiln residence time 240～260 minutes;
The leaching of C, slot type: the grog that roasting obtains is delivered to steel tank and is soaked and diafiltration with rare chromium acid sodium solution through being cooled to 350～400 ℃, goes into the ball mill grinding after the filter residue drying, controls grinding machine fineness 200 orders of slagging tap and accounts for 85～90%, and 100 orders account for 10～15%;
D, selection by winnowing: go out to grind slag and enter the powder selector sorting, 1000～1500 rev/mins of control powder selector rotor speeds, air quantity 10000～16000m
3/ h, blast 2000～3000Pa;
After E, the powder selector sorting, thin slag accounts for 35～45% and effluxes, and thick slag accounts for 60～65%, returns batching.
8, method of producing Sodium chromate through calcium-free roasting by chromite according to claim 7 is characterized in that: the temperature that is used to steep the last time wash water of washing in the leaching of step C slot type is 80～90 ℃, and it is 6～12 times that bubble is washed number of times.
9, according to claim 7 or 8 described methods of producing Sodium chromate through calcium-free roasting by chromite, it is characterized in that: to wash number of times be 8～10 times to bubble in the leaching of step C slot type.
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Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| NL6806812A (en) * | 1968-05-14 | 1969-11-18 | ||
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| CN1579947A (en) * | 2003-08-06 | 2005-02-16 | 民乐县化工厂 | Process for producing sodium chromate by calcium-free calcination |
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