[go: up one dir, main page]

WO2008113553A1 - Procédé et installation pour la production d'oxyde métallique à partir de sels métalliques - Google Patents

Procédé et installation pour la production d'oxyde métallique à partir de sels métalliques Download PDF

Info

Publication number
WO2008113553A1
WO2008113553A1 PCT/EP2008/002145 EP2008002145W WO2008113553A1 WO 2008113553 A1 WO2008113553 A1 WO 2008113553A1 EP 2008002145 W EP2008002145 W EP 2008002145W WO 2008113553 A1 WO2008113553 A1 WO 2008113553A1
Authority
WO
WIPO (PCT)
Prior art keywords
reactor
preheater
temperature
downpipe
metal salt
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.)
Ceased
Application number
PCT/EP2008/002145
Other languages
English (en)
Inventor
Michael Missalla
Günter Schneider
Cornelis Klett
Erwin Schmidbauer
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Metso Corp
Original Assignee
Outotec Oyj
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Outotec Oyj filed Critical Outotec Oyj
Priority to EA200901271A priority Critical patent/EA016961B1/ru
Priority to BRPI0809403A priority patent/BRPI0809403B8/pt
Priority to UAA200910578A priority patent/UA101804C2/ru
Priority to AU2008228481A priority patent/AU2008228481B2/en
Publication of WO2008113553A1 publication Critical patent/WO2008113553A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • 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
    • C01F7/44—Dehydration of aluminium oxide or hydroxide, i.e. all conversions of one form into another involving a loss of water
    • C01F7/441—Dehydration of aluminium oxide or hydroxide, i.e. all conversions of one form into another involving a loss of water by calcination
    • C01F7/445—Dehydration of aluminium oxide or hydroxide, i.e. all conversions of one form into another involving a loss of water by calcination making use of a fluidised bed
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J6/00—Heat treatments such as Calcining; Fusing ; Pyrolysis
    • B01J6/001—Calcining
    • B01J6/004—Calcining using hot gas streams in which the material is moved
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
    • C01B13/14—Methods for preparing oxides or hydroxides in general
    • C01B13/18—Methods for preparing oxides or hydroxides in general by thermal decomposition of compounds, e.g. of salts or 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
    • C01F7/44—Dehydration of aluminium oxide or hydroxide, i.e. all conversions of one form into another involving a loss of water
    • C01F7/441—Dehydration of aluminium oxide or hydroxide, i.e. all conversions of one form into another involving a loss of water by calcination
    • C01F7/444—Apparatus therefor

Definitions

  • the present invention relates to a process for producing metal oxide from metal hydroxide or other metal salts, in particular from aluminum hydroxide, wherein the metal salt is dried and preheated in at least one first preheating stage at a temperature of 100 to 200 0 C, precalcined in a second preheating stage at a temperature of 200 to 500 0 C and then calcined in a reactor at a temperature of 850 to 1100 0 C to obtain metal oxide, wherein a partial stream of the metal salts is not introduced into the reactor and mixed with metal oxide withdrawn from the reactor, and wherein the product obtained then is cooled.
  • Such process for producing alumina (AI 2 O 3 ) from aluminum trihydroxide (AI(OH) 3 ) is known for instance from DE 195 42 309 A1.
  • the humid aluminum trihydroxide first is dried in a first suspension preheater with waste gas having a temperature of about 300 0 C 1 which is supplied from a cyclone separator, and preheated to a temperature of about 160 0 C.
  • the solids Upon separation in a cyclone separator, the solids are supplied to a second suspension preheater, in which they are further dried with waste gas from the recirculation cyclone of a circulating fluidized bed, and upon passing through a cyclone separator then are charged to a fluidized-bed reactor of the circulating fluidized bed, in which the aluminum hydroxide is calcined at temperatures of about 950 0 C to obtain alumina.
  • a partial stream of the aluminum trihydroxide preheated in the first sus- pension preheater is branched off and mixed with hot alumina withdrawn from the recirculation cyclone of the circulating fluidized bed.
  • a mixing time of at least two minutes is provided.
  • the hot product mixture is cooled in a multi-stage suspension cooler in direct contact with air and is then supplied to a fluidized-bed cooler for final cooling.
  • alumina of increased quality can be produced with the process known from DE 195 42 309 A1 , this process still has some disadvantages.
  • the aluminum trihydroxide branched off from the first suspension preheater has a temperature of about 160 0 C and is mixed with alumina withdrawn from the fluidized-bed furnace at a temperature of about 1000 0 C. Due to the low temperature of the dehydrated aluminum hydroxide and the high expenditure of energy for calcination, merely a relatively small amount of aluminum hydroxide can be branched off as partial stream and be admixed to the alumina.
  • the amount of this partial stream is about 10%, in order to ensure that the product mixture is op- timally calcined in the mixing tank. Due to the low content of aluminum hydroxide guided around the reactor, a high expenditure is required to achieve a good mixture with a uniform distribution of the aluminum hydroxide in the mixing tank. In addition, the mixture is impaired in that very much steam is generated by dehydrating the aluminum trihydroxide. This generation of steam leads to local differ- ences in temperature (local subcooling due to heat required for evaporation). The steam generated also drives the reacting particles away from the alumina particles and leads to the particles floating on the hot alumina, so that they cannot be incorporated.
  • a so-called aperture blocker frequently is used for dividing streams of solids, which is a mechanical solids valve in the form of a lance with a cone-shaped tip which fits into a corresponding cone- shaped opening of the tank wall. By withdrawing or inserting the lance into the opening, the cross-section is increased or reduced, so that the outflow can be stopped.
  • Problematic at using this aperture blocker is the fact that the control aperture blocker includes mechanically moving parts which are in contact with the hot solids. Therefore, it must be cooled by water cooling.
  • this object substantially is solved with the invention in that the partial stream of the metal salt is branched off after the, at least partial, precalcination in the second preheating stage and supplied to a mixing tank, in which it is mixed with the metal oxide withdrawn from the reactor.
  • precalcination is understood to be the partial dehydration or removal of compounds, e.g. HCI and NOx. Calcination, however, refers to the complete dehydration or removal of compounds, e.g. SO 2 .
  • Metal salts in accordance with the invention preferably are metal hydroxide or metal carbonate, in particular aluminum hydroxide.
  • the aluminum trihydroxide When using aluminum trihydroxide as feedstock, the aluminum trihydroxide is pre- calcined by the elevated temperature in the second preheating stage and at least partly converted to aluminum monohydrate (AIOOH). If this aluminum monohy- drate is admixed to the alumina withdrawn from the reactor, a lower specific formation of steam is obtained as compared to the admixture of aluminum trihydroxide provided in the prior art. As a result, the precalcined aluminum hydroxide can more easily be mixed with the alumina from the reactor. This leads to a more uniform mixing in the mixing tank, lower local temperature differences and a reduced for- mation and circulation of dust. Moreover, the energy demand of the process and the retention time in the mixing tank can be reduced further.
  • AIOOH aluminum monohydrate
  • the partial stream of aluminum monohydrate branched off has a temperature of 200 to 500 0 C 1 preferably about 300 to 400 0 C, considerably warmer material is mixed with the hot alumina of about 1000 0 C from the reactor, whereby the thermal shock is decreased and the disintegration of particles is reduced.
  • a greater amount of aluminum hydroxide can be guided around the reactor due to the higher temperature and the reduced energy demand for the further calcination of the aluminum monohydrate.
  • about 10 to 40%, preferably 11 to 25%, in particular about 15 to 20% of the pre- calcined metal hydroxide is not introduced into the reactor.
  • the temperature in the mixing tank also is more stable due to the smaller temperature difference between the joined streams of material.
  • a temperature of about 500 to 820 0 C, preferably about 600 to 800 0 C, particularly preferably 700 to 78O 0 C is adjusted in the mixing tank in accordance with the invention for the production of alumina.
  • a complete dehydration of the aluminum monohydrate and hence a complete conversion of the starting product aluminum trihydroxide to alumina can be ensured thereby.
  • the retention time in the mixing tank can be reduced.
  • a further temperature increase in the mixing tank to e.g. 820 to 900 0 C is possible and leads to a further reduction of the retention time.
  • the quantity delivered in the bypass must then be reduced considerably.
  • a separator When a suspension preheater is used as second preheating stage, a separator will be provided downstream of the same in accordance with the invention, in which the precalcined metal hydroxide is separated from the gas stream. The separation of the partial stream guided around the reactor then is effected after this separator.
  • the stream of solids withdrawn after the second preheating stage is at least partly discharged via a downpipe and fluidized at the bottom of the downpipe by supplying a conveying gas, and that at least part of the stream of solids is delivered by the conveying gas via a rising pipe branched off from the first downpipe to a mixing tank.
  • a downpipe/rising pipe arrangement which is also referred to as seal pot, a division of the stream of solids thus is effected without movable parts of the apparatus getting in direct contact with the hot solids.
  • the various process stages no longer must be built one on top of the other, but can also be erected one beside the other. Construction height and hence costs will be saved thereby.
  • the supply of the conveying gas at the bottom of the downpipe is varied by a control means. In this way, the quantity of the stream of metal hydroxide branched off before the reactor can be determined particularly easily.
  • the temperature in the mixing tank is used as a control variable for supplying the stream of conveying gas, so that suitable process conditions are ensured for the mixture and for the complete dehydration of the metal hydroxide.
  • the temperature in the mixing tank differs from a specified setpoint, the supply of the fluidizing gas is adapted such that correspondingly more or less solids are delivered through the rising pipe and as a result the temperature in the mixing tank is returned to the desired value.
  • the temperature can be measured very easily, so that a reliable control is easily possible.
  • the pressure difference between the bottom and the top of the downpipe is kept smaller than the pressure loss corresponding to a fluidized downpipe. If, as likewise provided in accordance with the invention, the pressure at the bottom of the downpipe is kept greater than the pressure at the top of the downpipe, the solids in the downpipe behave like a sinking bed with a porosity close to that of a fixed bed. Thus, a non- fluidized, traversed moving bed is present in the downpipe.
  • ⁇ P D The pressure difference of the downpipe, ⁇ P D , here is defined by
  • ⁇ P R is the pressure loss over the rising pipe, which depends on the conveying gas flow and the solids mass flow. Since the gas supply to the rising pipe is varied, in order to realize a certain solids mass flow, a corresponding pressure loss is obtained here.
  • PR,K is the pressure at the top of the rising pipe, which in the case of a recirculation of solids into a fluidized bed mostly is equal to the pressure in the fluidized bed at the point where the rising pipe is connected to the fluidized-bed tank.
  • This pressure need not be constant, because it depends for instance on the variable solids inventory of the fluidized-bed tank.
  • the pressure can also be much higher than the ambient pressure. If the rising pipe opens into an expansion tank, ambient pressure will exist there in many cases. The pressure can vary, however, e.g. when the waste air suction of a fluidizing channel is too strong and a negative pressure is produced. If a further process part is provided downstream of the rising pipe, the pressure PR , « can also be much higher than the ambient pressure, for instance also higher than the pressure Po.
  • the pressure P 0 in the head space of the connected fluidized bed must be considered, and the pressure ⁇ P W S.B. which is caused by the fluidized bed of the bed height H W S, B above the downpipe inlet. Both pressures depend on the plant behavior of the fluidized-bed tank or of possibly further upstream apparatuses.
  • the pressure difference ⁇ P D over the downpipe is obtained automatically corresponding to the adjustment of the conveying gas flow.
  • this pressure difference should not become greater than that which would be obtained if the downpipe was fluidized. This would mean that the porosity in the downpipe is reduced and the backpressure from the rising pipe, or also from the fluidized-bed tank, no longer could be sealed off reliably. This is expressed by
  • the bulk material in the downpipe acts as a pressure seal, and the pressure at the top of the rising pipe is decoupled from the pressure at the inlet of the downpipe.
  • the solids mass flow now delivered or the bed height and the solids inventory in the fluidized-bed tank can be adjusted or controlled by varying the conveying gas.
  • the conveying gas for instance air, flows upwards in the rising pipe for the major part and delivers as much solids to the top as corresponds to its load bearing capacity. A minor part of the conveying gas traverses the moving bed in the downpipe and thereby causes the pressure loss in the downpipe.
  • a preheating stage consists of at least one, but also several pre- heaters.
  • the first preheating stage consists of a drier, which dries and heats the aluminum hydroxide to about 110 0 C, and a further preheater, which heats the dried aluminum hydroxide to about 150-190 0 C.
  • the second preheating stage only consists of one preheater, which preheats the dried aluminum trihydroxide to about 300-400 0 C and at least partly precalcines the same.
  • the first preheating stage consists of a drier, which dries and heats the aluminum trihydroxide to about 110 0 C, and of a second preheating stage, comprising two preheaters, in which the dried aluminum hydrate is heated and precalcined in a first preheater first to about 210-250°C and then to about 350-400 0 C. It is likewise possible that the two preheating stages each consist of two or more pre- heaters.
  • the precalcined aluminum hydroxide is removed from a preheater of the second preheating stage at a temperature of greater than 160 0 C, preferably greater than 200 0 C, usually greater than 220°C.
  • a temperature of greater than 160 0 C preferably greater than 200 0 C, usually greater than 220°C.
  • Such arrangement has advantages because of the lower energy demand for calcination and the higher temperature of the stream of metal hydroxide branched off as compared to the process known from DE 195 42 309 A1.
  • further preheating stages it is of course possible to also perform the division of the stream of metal hydroxide only after these further preheating stages, the efficiency of the process being changed in this case. It is furthermore possible to constructively solve the preheating such that several preheaters operate in parallel one beside the other and heat the divided stream of material to the same temperatures.
  • This invention also extends to a plant for producing metal oxide from metal hydroxide with the features of claim 11.
  • the bypass conduit for the precalcined metal hydroxide here is branched off from a conduit which directly or indirectly supplies the metal hydroxide to the reactor.
  • a downpipe for delivering the stream of solids withdrawn from the second preheating stage of which a rising pipe is branched off to the top, is provided after a preheater of the second preheating stage or after a separator provided downstream of the same.
  • conveying gas Via a conveying gas supply, conveying gas is introduced into the first downpipe below the rising pipe, in order to deliver solids through the rising pipe to the mixing tank.
  • the variation of the supply of conveying gas is effected via a control valve, wherein a temperature measuring device is provided on the mixing tank in accordance with a preferred aspect of the invention, and wherein the open position of the control valve can be controlled via a control circuit on the basis of the temperature measured with the temperature measuring device.
  • a third preheater is provided behind the second preheater, wherein after the third preheater the bypass conduit is branched off from the conduit supplying the metal hydroxide to the reactor.
  • Fig. 1 schematically shows a plant for performing the process of the invention
  • Fig. 2 schematically shows an apparatus for dividing the stream of solids in the plant as shown in Fig. 1.
  • filter-humid aluminum trihydroxide (AI(OH) 3 ) is introduced by means of a conveying screw 1 into a first suspension preheater 2 (first preheating stage) and entrained by a waste gas stream coming from a second suspension preheater 5 (second preheating stage). Subsequently, the gas-solids stream is separated in a succeeding cyclone separator 3. For dedusting purposes, the waste gas dis- charged from the cyclone separator 3 is supplied to an electrostatic gas cleaning 4 and finally to a chimney (not shown).
  • AI(OH) 3 filter-humid aluminum trihydroxide
  • the solids discharged from the cyclone separator 3 and the electrostatic gas cleaning 4 subsequently are introduced into the second suspension preheater 5, in which the solids are entrained by the waste gas discharged from a recirculation cyclone 6 of a circulating fluidized bed and are further dewatered at temperatures of about 35O 0 C and dehydrated to obtain aluminum monohydrate (AIOOH).
  • AIOOH aluminum monohydrate
  • a separation of the gas-solids stream is effected again, wherein the aluminum monohydrate is supplied downwards and the waste gas is introduced into the first suspension preheater 2.
  • the stream of aluminum monohydrate is divided by means of an apparatus described in detail below (cf. Fig. 2).
  • a main stream containing about 80 to 90% of the stream of solids is supplied via a conduit (conveying means 30) to a fluidized bed reactor 8, in which the aluminum monohydrate is calcined at temperatures of about 1000 0 C and completely dehydrated to obtain alumina (AI 2 O 3 ).
  • the supply of the fuel required for calcination is effected via a fuel conduit 9, which is disposed at a small height above the grid of the fluidized-bed reactor 8.
  • the oxygen- containing gas streams required for combustion are supplied via supply conduit 10 as fluidizing gas and via supply conduit 11 as secondary gas.
  • the gas-solids suspension enters the recirculation cyclone 6 of the circulating fluidized bed, in which another separation of gas and solids is effected.
  • a mixing temperature of about 750 0 C is adjusted corresponding to the mixing ratio between the hot alumina stream supplied via conduit 13 and the aluminum monohydrate stream supplied via bypass conduit 15.
  • the two product streams are thoroughly mixed in the mixing tank 14, which includes a fluidized bed, in order to also completely calcine the aluminum monohydrate supplied via the bypass conduit 15 to obtain alumina.
  • a very long retention time of up to 30 min or up to 60 min leads to an excellent calcination in the mixing tank. It was noted, however, that in general a retention time of less than two minutes, in particular about one minute, already is sufficient for this purpose. A retention time of less than 45 s, in particular less than 30 s, is preferred quite particularly.
  • the product obtained is supplied to a first suspension cooler formed of rising pipe 16 and cyclone separator 17.
  • the waste gas of the cyclone separator 17 flows into the fluidized-bed reactor 9 via conduit 11, the solids are introduced into the second suspension cooler formed of rising pipe 18 and cyclone separator 19 and finally into the third suspension cooler formed of rising pipe 20 and cyclone separator 21.
  • the gas flow through the individual suspension coolers is effected in counterflow to the solids via conduits 22 and 23.
  • the alumina produced undergoes a final cooling in the fluidized-bed cooler 24 equipped with three cooling chambers.
  • the fluidizing gas supplied to the fluidized-bed reactor 9 is heated, in the succeeding second chambers it is cooled against a heat transfer medium, preferably water, which is guided in counterflow.
  • the alumina finally is discharged through conduit 25.
  • Fig. 2 shows an apparatus for dividing the stream of solids withdrawn from the separating cyclone 7 after the second preheater 5.
  • 35O 0 C is withdrawn from the separating cyclone at about ambient pressure.
  • the conveying means 30 designed for instance as fluidizing channel, at least part of the aluminum monohydrate flows off via a downpipe 31 , while the other part is moved on in the conveying means 30 and supplied to the fluidized-bed reactor 8 via various non-illustrated process stages.
  • a rising pipe 33 is branched off, which substantially extends vertically to the top.
  • the solids at the bottom of the downpipe 31 are fluidized by means of at least one nozzle 34. There is shown an upwardly directed nozzle 34, but it is also possible to direct the nozzle downwards, so that clogging can be prevented more reliably.
  • One of skill in the art can employ all measures known to him for suitably fluidizing the solids at the bottom of the downpipe 31. It is possible, for instance, to provide a cap nozzle or a nozzle with a porous body provided at its end, which should prevent clogging of the nozzle. It is also possible to supply the conveying gas via a fluidizing cloth or other porous medium, which is disposed at the bottom of the downpipe above a non-illustrated gas distributor.
  • the solids rise through the rising pipe 33 into an expansion tank 35 and are supplied from the same via a delivery conduit 36 to the mixing tank 14.
  • a simple elbow can also be provided at the end of the rising pipe 33.
  • the aluminum monohydrate is mixed with alumina from the fluidized-bed reactor 8, which is supplied via conduit 13.
  • the alumina has a tem- perature of about 1000 0 C, so that with the mixing ratio provided in the fluidized mixing tank 11 a mixing temperature of about 750 0 C and a retention time of 20 s are obtained.
  • the pressure in the mixing tank 14 is about 1.14 bar (abs), i.e. there is a slight excess pressure with respect to the surroundings.
  • the mixing tank 14 can be arranged above or below the conveying means 30.
  • the temperature in the mixing tank 14 depends on the mixing ratio between the aluminum monohydrate supplied via the rising pipe 33 and the alumina supplied via conduit 13 and on the temperatures of these streams of solids.
  • the temperature in the mixing tank 14 is controlled by the amount and the temperature of the solid streams from the furnace and the preheating stage.
  • the solids mass flows in the rising pipe 33 and in conduit 13 can be measured only with difficulty. Therefore, it is preferred in accordance with the invention to detect the easily measurable temperature in the mixing tank 14 by means of a temperature measuring device 37 and use it as a control variable for controlling a control valve 38 in the supply conduit 39 to the nozzle 34, by means of which the supply of the conveying gas at the bottom 32 of the downpipe 31 is adjusted.
  • the mixing ratio and hence the temperature in the mixing tank 14 can be influenced very easily, in that the supply of conveying gas via the nozzle 34 is increased when the actual temperature in the mixing tank 14 exceeds the setpoint and hence a greater amount of colder aluminum monohydrate is introduced into the mixing tank 14. As a result, the temperature in the mixing tank is decreasing again. When the temperature in the mixing tank 14 decreases below the setpoint, the supply of the aluminum monohydrate is reduced by correspondingly closing the control valve 38.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Geology (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

Lors de la production d'un oxyde métallique à partir de sels métalliques, le sel métallique, en particulier l'hydroxyde d'aluminium, est séché et préchauffé dans un premier dispositif de préchauffage (2) à une température de 100 à 200°C, précalciné dans un second dispositif de préchauffage (5) à une température de 300 à 400°C, puis calciné dans un réacteur (8) à une température de 850 à 1 100°C pour obtenir un oxyde métallique, en particulier l'alumine. Après précalcination dans le second dispositif de préchauffage (5), un courant partiel du sel métallique est dérivé et adressé à un réservoir de mélange (14), dans lequel il est mélangé avec l'oxyde métallique soutiré du réacteur (8).
PCT/EP2008/002145 2007-03-22 2008-03-18 Procédé et installation pour la production d'oxyde métallique à partir de sels métalliques Ceased WO2008113553A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
EA200901271A EA016961B1 (ru) 2007-03-22 2008-03-18 Способ и установка для производства оксида металла из солей металла
BRPI0809403A BRPI0809403B8 (pt) 2007-03-22 2008-03-18 Processo e instalação para produzir óxido metálico a partir de sais metálicos
UAA200910578A UA101804C2 (ru) 2007-03-22 2008-03-18 Способ и установка для производства оксида металла из солей металла
AU2008228481A AU2008228481B2 (en) 2007-03-22 2008-03-18 Process and plant for producing metal oxide from metal salts

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102007014435.2A DE102007014435B4 (de) 2007-03-22 2007-03-22 Verfahren und Anlage zur Herstellung von Metalloxid aus Metallsalzen
DE102007014435.2 2007-03-22

Publications (1)

Publication Number Publication Date
WO2008113553A1 true WO2008113553A1 (fr) 2008-09-25

Family

ID=39587875

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2008/002145 Ceased WO2008113553A1 (fr) 2007-03-22 2008-03-18 Procédé et installation pour la production d'oxyde métallique à partir de sels métalliques

Country Status (6)

Country Link
AU (1) AU2008228481B2 (fr)
BR (1) BRPI0809403B8 (fr)
DE (1) DE102007014435B4 (fr)
EA (1) EA016961B1 (fr)
UA (1) UA101804C2 (fr)
WO (1) WO2008113553A1 (fr)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2009100840A3 (fr) * 2008-02-13 2010-02-25 Outotec Oyj Processus industriel de raffinage de matières premières contenant des constituants organiques
WO2009100841A3 (fr) * 2008-02-13 2010-02-25 Outotec Oyj Procédé et installation pour le raffinage de matières brutes contenant des constituants organiques
WO2010083961A1 (fr) * 2009-01-26 2010-07-29 Outotec Oyj Procédé et installation pour la production d'oxyde métallique à partir de sels métalliques
US8460624B2 (en) 2009-01-26 2013-06-11 Outotec Oyj Process and plant for producing metal oxide from metal salts
WO2019114922A1 (fr) * 2017-12-11 2019-06-20 Outotec (Finland) Oy Procédé et installation de décomposition thermique d'hydrate de chlorure d'aluminium en oxyde d'aluminium
WO2021104613A1 (fr) * 2019-11-26 2021-06-03 Outotec (Finland) Oy Procédé semi-sec optimisé pour le frittage d'aluminosilicates dans la production d'alumine

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102010050495B4 (de) 2010-11-08 2018-05-24 Outotec Oyj Verfahren und Anlage zur Herstellung von Aluminiumoxid aus Aluminiumhydroxid

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19542309A1 (de) * 1995-11-14 1997-05-15 Metallgesellschaft Ag Verfahren zur Herstellung von Aluminiumoxid aus Aluminiumhydroxid
WO2005005318A2 (fr) * 2003-07-11 2005-01-20 Outokumpu Technology Oy Procede et equipement de production d'oxyde metallique a partir d'hydroxyde metallique

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3107711A1 (de) 1981-02-28 1982-10-07 Creusot-Loire Entreprises, 92150 Suresnes Verfahren zur herstellung von zementklinker
WO2006106443A2 (fr) 2005-04-06 2006-10-12 Ffe Minerals Denmark A/S Procede et installation de fabrication de l'alumine

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19542309A1 (de) * 1995-11-14 1997-05-15 Metallgesellschaft Ag Verfahren zur Herstellung von Aluminiumoxid aus Aluminiumhydroxid
WO2005005318A2 (fr) * 2003-07-11 2005-01-20 Outokumpu Technology Oy Procede et equipement de production d'oxyde metallique a partir d'hydroxyde metallique

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8613783B2 (en) 2008-02-13 2013-12-24 Outotec Oyj Process and plant for refining raw materials containing organic constituents
WO2009100841A3 (fr) * 2008-02-13 2010-02-25 Outotec Oyj Procédé et installation pour le raffinage de matières brutes contenant des constituants organiques
US9764300B2 (en) 2008-02-13 2017-09-19 Outotec Oyj Process and plant for refining raw materials containing organic constituents
WO2009100840A3 (fr) * 2008-02-13 2010-02-25 Outotec Oyj Processus industriel de raffinage de matières premières contenant des constituants organiques
US8936657B2 (en) 2008-02-13 2015-01-20 Outotec Oyj Process and plant or refining raw materials containing organic constituents
GB2478671A (en) * 2009-01-26 2011-09-14 Outotec Oyj Process and plant for production metal oxide from metal salts
US8460624B2 (en) 2009-01-26 2013-06-11 Outotec Oyj Process and plant for producing metal oxide from metal salts
EA019025B1 (ru) * 2009-01-26 2013-12-30 Ототек Оюй Способ и установка для получения оксида металла из гидроксида металла
GB2478671B (en) * 2009-01-26 2014-04-09 Outotec Oyj Process and plant for producing metal oxide from metal salts
AU2010206320B2 (en) * 2009-01-26 2014-10-09 Outotec Oyj Process and plant for producing metal oxide from metal salts
US8313715B2 (en) 2009-01-26 2012-11-20 Outotec Oyj Process and plant for producing metal oxide from metal salts
WO2010083961A1 (fr) * 2009-01-26 2010-07-29 Outotec Oyj Procédé et installation pour la production d'oxyde métallique à partir de sels métalliques
WO2019114922A1 (fr) * 2017-12-11 2019-06-20 Outotec (Finland) Oy Procédé et installation de décomposition thermique d'hydrate de chlorure d'aluminium en oxyde d'aluminium
WO2021104613A1 (fr) * 2019-11-26 2021-06-03 Outotec (Finland) Oy Procédé semi-sec optimisé pour le frittage d'aluminosilicates dans la production d'alumine

Also Published As

Publication number Publication date
AU2008228481B2 (en) 2013-03-21
UA101804C2 (ru) 2013-05-13
AU2008228481A1 (en) 2008-09-25
EA200901271A1 (ru) 2010-02-26
BRPI0809403B1 (pt) 2018-07-31
DE102007014435A1 (de) 2008-09-25
EA016961B1 (ru) 2012-08-30
DE102007014435B4 (de) 2014-03-27
BRPI0809403A2 (pt) 2014-09-16
BRPI0809403B8 (pt) 2023-03-28

Similar Documents

Publication Publication Date Title
US8460624B2 (en) Process and plant for producing metal oxide from metal salts
AU2008228481B2 (en) Process and plant for producing metal oxide from metal salts
US8313715B2 (en) Process and plant for producing metal oxide from metal salts
US20250250196A1 (en) High temperature hydrator
US7549859B2 (en) Installation and process for calcining a mineral load containing a carbonate in order to produce a hydraulic binder
CN102519224B (zh) 一种多级固体燃料干燥系统
UA81284C2 (en) Method and plant for heat treatment in fluidized bed
HU180947B (en) Improved process for preparing anhydrous alum earth
EA010273B1 (ru) Способ и установка для производства оксида металла из соединений металла
AU2008291392B2 (en) Process and plant for the thermal treatment of granular solids
Fish Alumina calcination in the fluid-flash calciner
WO2008104251A1 (fr) Procédé et appareil pour la séparation d'un flux de solides
CN107879365A (zh) 一种利用脱硅粉煤灰烧结法生产氧化铝的系统及方法
Williams et al. Flash-and CFB calciners, history and difficulties of development of two calcination technologies
WO2012062593A1 (fr) Procédé et installation pour produire de l'alumine à partir d'hydroxyde d'aluminium
JP3032198B1 (ja) 石灰泥の焼成方法及び装置
CN207792721U (zh) 一种利用脱硅粉煤灰烧结法生产氧化铝的系统
OA16406A (en) Process and plant for producing alumina from aluminum hydroxide.

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 08716603

Country of ref document: EP

Kind code of ref document: A1

DPE1 Request for preliminary examination filed after expiration of 19th month from priority date (pct application filed from 20040101)
WWE Wipo information: entry into national phase

Ref document number: 2008228481

Country of ref document: AU

WWE Wipo information: entry into national phase

Ref document number: 1406/MUMNP/2009

Country of ref document: IN

ENP Entry into the national phase

Ref document number: 2008228481

Country of ref document: AU

Date of ref document: 20080318

Kind code of ref document: A

NENP Non-entry into the national phase

Ref country code: DE

WWE Wipo information: entry into national phase

Ref document number: 200901271

Country of ref document: EA

122 Ep: pct application non-entry in european phase

Ref document number: 08716603

Country of ref document: EP

Kind code of ref document: A1

ENP Entry into the national phase

Ref document number: PI0809403

Country of ref document: BR

Kind code of ref document: A2

Effective date: 20090918