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WO2009026989A1 - Processus et centrale de traitement thermique de matières solides granuleuses - Google Patents

Processus et centrale de traitement thermique de matières solides granuleuses Download PDF

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Publication number
WO2009026989A1
WO2009026989A1 PCT/EP2008/005619 EP2008005619W WO2009026989A1 WO 2009026989 A1 WO2009026989 A1 WO 2009026989A1 EP 2008005619 W EP2008005619 W EP 2008005619W WO 2009026989 A1 WO2009026989 A1 WO 2009026989A1
Authority
WO
WIPO (PCT)
Prior art keywords
fluidized
solids
conduit
bed reactor
delivery conduit
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/EP2008/005619
Other languages
English (en)
Inventor
Pekka Hiltunen
Günter Schneider
Michael Missalla
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 EA201000417A priority Critical patent/EA016569B1/ru
Priority to UAA201003637A priority patent/UA100992C2/ru
Priority to BRPI0816090A priority patent/BRPI0816090B1/pt
Priority to AU2008291392A priority patent/AU2008291392B2/en
Publication of WO2009026989A1 publication Critical patent/WO2009026989A1/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
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/005—Separating solid material from the gas/liquid stream
    • B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/005—Separating solid material from the gas/liquid stream
    • B01J8/006—Separating solid material from the gas/liquid stream by filtration
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
    • B01J2208/00141—Coils
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/0053—Controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling

Definitions

  • This invention relates to the thermal treatment of granular solids, in particular the production of alumina from aluminium hydroxide, wherein upon preheating in at least one preheating stage the solids are heated, in particular calcined, in a fluid- ized-bed reactor and are then supplied to at least one fluidized-bed cooler, in which the thermally treated solids are cooled by means of fluidizing gas, wherein the fluidizing gas is withdrawn from the cooler and introduced into the fluidized-bed reactor as secondary gas.
  • Such process for producing anhydrous alumina (AI 2 O 3 ) from aluminium hydroxide (AI(OH) 3 ) is known from EP 0 861 208 B1.
  • the aluminium hydroxide is cal- cined in a circulating fluidized bed upon traversing two preheating stages.
  • Preheating the aluminium hydroxide is effected by means of waste gas from a separator provided downstream of the fluidized-bed reactor.
  • anhydrous hot alumina is branched off and directly and indirectly cooled with air in a fluidized-bed cooler.
  • the air indirectly heated thereby is introduced into the fluidized-bed reactor as fluidizing air, whereas the air introduced into the fluidized-bed cooler as fluidizing air for direct cooling is withdrawn from the cooler and likewise introduced into the fluidized-bed reactor as secondary air.
  • this object substantially is solved with the invention in that the secondary gas stream is divided in a controlled way at one or more points of the stream, and one bypass stream or several bypass streams is/are guided past the fluidized-bed reactor into a delivery conduit for the solids.
  • the transport and combustion tasks of the air thus are decoupled.
  • the part of the secondary gas stream introduced into the fluidized-bed reactor as combustion air can be controlled corresponding to the fuel supply sufficient for calcining the solids supplied.
  • the remaining part of the secondary gas stream is guided past the fluid- ized-bed reactor as a bypass stream directly into a delivery conduit for the solids, so that a sufficient amount of conveying gas is ensured there.
  • the size of the bypass stream is variable, and is controlled together with the fuel supply in dependence on the supply rate of solids into the fluidized-bed reactor.
  • the ⁇ ratio in the fluidized-bed reactor can be adjusted optimally for different load conditions of the reactor.
  • the bypass stream is introduced into the delivery conduit before a preheating stage for the solids, in order to ensure a sufficient fluidization therein.
  • the thermal energy contained in the secondary gas can also be utilized for preheating the solids.
  • the solids are supplied to a preheater, in particular a suspension preheater, in which they are preheated with waste gas from a separator provided downstream of the fluidized-bed reactor, wherein the gas/solids mixture from the suspension preheater is supplied to a second separator via a second delivery conduit, the bypass stream is fed into the second delivery conduit in accordance with a particularly preferred aspect of the invention.
  • a preheater in particular a suspension preheater, in which they are preheated with waste gas from a separator provided downstream of the fluidized-bed reactor, wherein the gas/solids mixture from the suspension preheater is supplied to a second separator via a second delivery conduit
  • the bypass stream is fed into the second delivery conduit in accordance with a particularly preferred aspect of the invention.
  • the bypass stream is fed into a first delivery conduit, through which waste gas from the first separator downstream of the fluidized-bed reactor is introduced into the suspension preheater.
  • the gas/solids mixture from the suspension preheater is supplied to a second separator, whose waste gas is supplied to a first preheating stage via a third delivery conduit for preheating and delivering fresh solids, wherein the bypass stream is fed directly into the third delivery conduit.
  • the secondary gas stream can be divided at every point of the process into one or more bypass streams. In the preferred embodiment of the invention, however, the secondary gas stream is divided upon traversing the preheating stages of the secondary gas stream (cooling stages of the material from the reactor).
  • a plant for the thermal treatment of granular solids which is suitable for performing the process of the invention, comprises a fluidized-bed reactor in which the solids are heated, in particular calcined, at least one preheating stage for preheating the solids before introduction into the fluidized-bed reactor, and at least one fluidized- bed cooler, in which the solids withdrawn from the fluidized-bed reactor via a discharge conduit are cooled by means of fluidizing gas, wherein the fluidizing gas is withdrawn from the cooler and introduced into the fluidized-bed reactor via a secondary gas conduit.
  • one bypass conduit or several bypass conduits is/are branched off from the secondary gas conduit, which is/are guided past the fluidized-bed reactor and is/are connected with a delivery conduit for the solids
  • a control valve, gate or the like including preferably a measuring device for the volumetric flow rate, is provided in accordance with a development of the invention. Furthermore, a means for controlling the pressure and/or the pressure loss can be provided in the bypass conduit and/or in the remaining secondary air conduit, in accordance with a development of the invention.
  • bypass conduit is connected with a delivery conduit leading to at least one preheating stage.
  • a first separator is provided downstream of the fluidized-bed reactor, whose waste gas is introduced into a preheater, in particular a suspension preheater, via a first delivery conduit, wherein the suspension preheater is connected with a second separator via a second delivery conduit and the bypass conduit opens into the second delivery conduit.
  • bypass conduit is connected with the first delivery conduit.
  • second separator is connected with a first preheating stage for fresh solids via a third delivery conduit, and the bypass conduit opens into the third delivery conduit.
  • feed points for the bypass conduits as described above can be provided alternatively or cumulatively in dependence on the plant conditions, wherein the respective amounts are controlled individually by means of the control valves provided in the bypass conduits.
  • the procedure in accordance with the invention can be employed for all processes that require a delivery of solids, e.g. calcination of magnesium carbonate, breakdown of magnesium sulfate, calcination of ores or preheating of iron ore.
  • Fig. 1 schematically shows a plant for performing the process of the invention in accordance with a first embodiment of the invention
  • Fig. 2 shows a plant for performing the process of the invention in accordance with a second embodiment
  • Fig. 3 schematically shows a plant for performing the process of the invention in accordance with a third embodiment
  • Fig. 4 schematically shows a plant for performing the process of the invention in accordance with a fourth embodiment
  • Fig. 5 schematically shows a plant for performing the process of the inven- tion in accordance with a fifth embodiment
  • Fig. 6 schematically shows a plant for performing the process of the invention in accordance with a sixth embodiment
  • Fig. 7 schematically shows a plant for performing the process of the invention in accordance with a seventh embodiment
  • Fig. 8 schematically shows a plant for performing the process of the invention in accordance with an eighth embodiment
  • Fig. 9 shows a diagram which illustrates the reduction of the specific energy consumption in dependence on the bypass stream guided past the fluidized-bed reactor.
  • filter-moist aluminium hydroxide (AI(OH) 3 ) is introduced at a charging station 1 into a first flash reactor 2 or a suspension preheater (first preheating stage), in which it is entrained by the waste gas stream coming from the plant and supplied to a separating means 3.
  • the waste gas emerging from the separating means 3 is supplied to an e.g. electrostatic gas cleaning 4 for dedust- ing and finally to a non-illustrated chimney.
  • the solids emerging from the separating means 3 are delivered via a conduit 5 into a second preheater, which in particular constitutes a suspension preheater 6 (second preheating stage), in which the solids are entrained by the waste gas emerging from a recirculation cyclone (first separator) 8 of a circulating fluidized bed via a first delivery conduit 7 and are further dewatered or dehydrated.
  • a second delivery conduit 9 the gas/solids mixture from the suspension preheater 6 is supplied to a separation cyclone (second separator) 10, in which the solids are separated from the gas.
  • the gas is introduced into the flash reactor 2 as conveying gas and conveys the fresh aluminium hydroxide to the separating means 3, preheating the solids at the same time.
  • the solids separated in the separation cyclone 10 are introduced into a fluidized-bed reactor 13a, in which they are calcined at a temperature in the range from 850 to 1000 0 C by means of fuel supplied via a fuel conduit 14.
  • the oxygen-containing gas streams e.g. air or air enriched with oxygen, required for combustion are supplied as fluidizing gas via a primary gas conduit 15 and as secondary gas via a secondary gas conduit 16.
  • the gas-solids suspension enters the recirculation cyclone 8 of the circulating fluidized bed, in which gas and solids are newly separated.
  • the solids emerging from the recirculation cyclone 8 are supplied to a first suspension cooler formed of rising conduit 19 and cyclone separator 20.
  • the waste gas of the cy- clone separator 20 flows into the fluidized-bed reactor 13a, the solids are delivered into a second suspension cooler formed of rising conduit 21 and cyclone separator 22.
  • the waste gas of the second suspension cooler is introduced as conveying gas into the rising conduit 19 of the first suspension cooler.
  • the alumina produced undergoes a final cooling in a fluidized-bed cooler 24 equipped with four cooling chambers.
  • the fluidizing gas (primary gas) supplied to the fluidized-bed reactor 13a is heated, in the downstream chambers it is cooled against a heat-transfer medium, preferably water, which is guided in counterflow.
  • the alumina finally is discharged via conduit 25.
  • a bypass conduit 26a which opens into the second delivery conduit 9, is branched off from the secondary gas conduit 16 before the fluidized-bed reactor 13.
  • a control valve 27a or a gate or the like is provided, in order to adjust the amount of the bypass stream branched off from the secondary gas con- duit 16 in correspondence with the plant load.
  • control valve 27a In full-load operation of the plant, the control valve 27a will normally be closed, so that the entire secondary gas supplied via the secondary gas conduit 16 and the associated upstream coolers and conduits is fed into the fluidized-bed reactor 13a and is available for combustion.
  • the amount of secondary gas fed into the fluidized-bed reactor 13 via conduit 16 can be reduced, in order to adapt the ⁇ ratio to the lower fuel supply required for calcining smaller amounts of aluminium hydroxide and avoid an increase in the combustion and hence waste gas temperatures.
  • the remaining part of the secondary gas stream is directly fed into the second delivery conduit 9 via the bypass conduit 26a and promotes the delivery of the solids from the suspension preheater 6 through the further parts of the plant. This ensures that a sufficient amount of conveying gas is always available and a deposition and ac- cretion of particles on the walls of the delivery conduits or separators is avoided. At the same time, the thermal energy contained in the bypass stream is utilized for preheating the solids.
  • the bypass stream from the secondary gas conduit can for instance also be branched off from the conduit 23 or from the cooler 29.
  • the second embodiment of the present invention as shown in Figure 2 substantially has the same configuration as the plant shown in Figure 1.
  • the fluidized-bed cooler is composed of two separate cooling stages 29, 30, wherein the first cooling stage 29 corresponds to the first chamber of the fluidized-bed cooler 24 in accordance with the first embodiment and serves to heat up the fluidizing gas (primary gas) supplied to the fluidized-bed reactor 13a.
  • the alumina produced is finally cooled in three cooling chambers against a heat-transfer medium, preferably water, which is guided in counterflow.
  • a partial stream of the moderately warm aluminium hydroxide is branched off before being fed into the suspension preheater 6 and supplied via a hydrate bypass 31 to a mixing chamber 32, in which it is added to the hot alumina produced in the fluidized-bed reactor 13a.
  • This process is described in detail in EP 0 861 208 B1.
  • the bypass conduit 26b branched off from the secondary gas conduit 16 leads into the first delivery conduit 7, through which the hot waste gas from the recirculation cyclone 8 is introduced into the suspension preheater 6.
  • the gas stream available for fluidization in the suspension preheater 6 is increased thereby.
  • the size of the bypass stream is controlled by means of the control valve 27b.
  • the configuration and operation of the plant shown in Figure 3 correspond to the plant of the first embodiment as shown in Figure 1 , so that reference can be made to the above description.
  • the fourth embodiment of a plant in accordance with the invention as shown in Figure 4 only differs from the plant shown in Figure 3 in that the branching point for the hydrate bypass 33 has been shifted.
  • the hydrate bypass 33 of the plant shown in Figure 4 is branched off after the second separator 10 before introducing the sol- ids into the fluidized-bed reactor 13a.
  • a precalcination of the aluminium hydroxide contained in the bypass stream is already achieved, so that the final calcination of these solids in the mixing chamber 32 is accelerated.
  • the fifth embodiment of the present invention as shown in Figure 5 substantially has the same configuration as the plant shown in Figure 3. However, merely the feed point for the bypass conduit 26c has been shifted.
  • the bypass conduit 26c branched off from the secondary gas conduit 16 leads into the third delivery conduit 11 , which connects the separation cyclone 10 with the flash reactor 2.
  • the fresh aluminium hydroxide added via the charging sta- tion 1 is further preheated in the first preheating stage.
  • the fluidized-bed cooler has been configured with two separate cooling stages 29, 30.
  • FIGS 7 and 8 Alternative aspects of the fluidized-bed reactor 13 are shown in Figures 7 and 8. While in the embodiments shown in Figures 1 to 6 a circulating fluidized bed with a fluidized-bed reactor 13a and a return conduit 13a' is provided, a flash reactor 13b is provided in the seventh embodiment of the invention as shown in Figure 7. In the eighth embodiment of the invention as shown in Figure 8, however, an annular fluidized-bed reactor 13c is provided, as it is described for instance in detail in DE 102 60 741 A1. Moreover, the mode of function and operation of the plants shown in Figures 7 and 8 corresponds to the first to sixth embodiments, so that in so far reference is made to the above description. It is, however, always possible to also use reactors other than fluidized-bed or flash reactors with separators, such as cyclones, rotary kilns or similar industrial furnaces.
  • separators such as cyclones, rotary kilns or similar industrial furnaces.
  • bypass conduit 26a, b, c into the second delivery conduit 9, first delivery conduit 7 or third delivery conduit 11 and the configuration of the fluidized-bed reactor 13 or of the fluidized-bed cooler, as they have been described in detail in the individual plants, can also be used in any combination in the respective plants shown in the other Figures. It is also possible to provide all three feed points of the bypass conduits 26a, b, c cumulatively. In this case, the division of the bypass stream is effected by corresponding actuation of the control valves 27a, b, c corresponding to the requirements of the plant. Furthermore, it is of course possible to dispose the branching points at any point of the secondary gas conduit or of the entire upstream supply conduits for secondary gas.
  • the specific energy consumption of a calcining plant can substantially be reduced in partial-load operation.
  • the specific energy consumption of a plant shown in Fig. 1 is illustrated as a function of the partial load of 1250 t/d to 2500 t/d.
  • the upper, continuous curve corresponds to the course of the specific energy consumption, when no bypass stream is used.
  • I 1 third delivery conduit 12 solids supply conduit
  • conduit 24 fluidized-bed cooler conduit a,b,c bypass conduita,b,c control valve first cooling stage second cooling stage hydrate bypass mixing chamber hydrate bypass

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Thermal Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Geology (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
  • Crucibles And Fluidized-Bed Furnaces (AREA)

Abstract

Au cours de la production d'alumine à partir d'hydroxyde d'aluminium, l'hydroxyde d'aluminium est calciné dans un réacteur à lit fluidisé, lors du préchauffage au cours d'au moins une étape de préchauffage, puis amené à au moins un dispositif de refroidissement à lit fluidisé, dans lequel les matières solides calcinées sont refroidies au moyen d'un air de fluidisation, l'air de fluidisation étant prélevé du dispositif de refroidissement et introduit à l'intérieur du réacteur à lit fluidisé en tant qu'air secondaire. Afin de réduire au minimum la consommation d'énergie spécifique au cours d'une opération à charge partielle de la centrale, le courant d'air secondaire est divisé et un courant de dérivation est guidé au-delà du réacteur à lit fluidisé et introduit à l'intérieur d'une conduite de distribution des matières solides.
PCT/EP2008/005619 2007-09-01 2008-07-10 Processus et centrale de traitement thermique de matières solides granuleuses Ceased WO2009026989A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
EA201000417A EA016569B1 (ru) 2007-09-01 2008-07-10 Способ и установка для термической обработки зернистых твердых частиц
UAA201003637A UA100992C2 (ru) 2007-09-01 2008-07-10 Способ и установка для термической обработки зернистых твердых частиц
BRPI0816090A BRPI0816090B1 (pt) 2007-09-01 2008-07-10 processo e instalação para tratamento térmico de sólidos granulados
AU2008291392A AU2008291392B2 (en) 2007-09-01 2008-07-10 Process and plant for the thermal treatment of granular solids

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102007041586.0 2007-09-01
DE102007041586.0A DE102007041586B4 (de) 2007-09-01 2007-09-01 Verfahren und Anlage zur Wärmebehandlung von körnigen Feststoffen

Publications (1)

Publication Number Publication Date
WO2009026989A1 true WO2009026989A1 (fr) 2009-03-05

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PCT/EP2008/005619 Ceased WO2009026989A1 (fr) 2007-09-01 2008-07-10 Processus et centrale de traitement thermique de matières solides granuleuses

Country Status (6)

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AU (1) AU2008291392B2 (fr)
BR (1) BRPI0816090B1 (fr)
DE (1) DE102007041586B4 (fr)
EA (1) EA016569B1 (fr)
UA (1) UA100992C2 (fr)
WO (1) WO2009026989A1 (fr)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010083961A1 (fr) * 2009-01-26 2010-07-29 Outotec Oyj Procédé et installation pour la production d'oxyde métallique à partir de sels métalliques
WO2017144469A1 (fr) * 2016-02-23 2017-08-31 Outotec (Finland) Oy Procédé et dispositif pour le traitement thermique de solides granulaires
WO2017157906A1 (fr) * 2016-03-15 2017-09-21 Outotec (Finland) Oy Procédé et installation pour le traitement thermique de solides granulaires
CN107709240A (zh) * 2015-06-02 2018-02-16 奥图泰(芬兰)公司 用于热处理颗粒状固体的方法和系统
CN108083294A (zh) * 2018-02-12 2018-05-29 沈阳鑫博工业技术股份有限公司 一种从赤泥中提取氧化铝和氧化钠的装置及方法
WO2018095815A1 (fr) * 2016-11-22 2018-05-31 Outotec (Finland) Oy Procédé et installation de traitement thermique dans un réacteur à lit fluidisé

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DE102009006095B4 (de) * 2009-01-26 2019-01-03 Outotec Oyj Verfahren und Anlage zur Herstellung von Aluminiumoxid aus Aluminiumhydroxid

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US3565408A (en) * 1967-06-16 1971-02-23 Metallgesellschaft Ag Production of alumina from aluminum hydroxide
DE2048207A1 (de) * 1970-10-01 1972-04-06 Kloeckner Humboldt Deutz Ag Einrichtung zur Herstellung von Tonerde aus Tonerdehydrat
WO1997018165A1 (fr) * 1995-11-14 1997-05-22 Metallgesellschaft Aktiengesellschaft Procede de production d'oxyde d'aluminium a partir d'hydroxyde d'aluminium

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DE1767628C3 (de) * 1968-05-30 1985-03-14 Metallgesellschaft Ag, 6000 Frankfurt Verfahren zur Durchführung endothermer Prozesse
DE2524540C2 (de) * 1975-06-03 1986-04-24 Metallgesellschaft Ag, 6000 Frankfurt Verfahren zur Durchführung endothermer Prozesse
DE10260741A1 (de) * 2002-12-23 2004-07-08 Outokumpu Oyj Verfahren und Anlage zur Wärmebehandlung von feinkörnigen Feststoffen

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3565408A (en) * 1967-06-16 1971-02-23 Metallgesellschaft Ag Production of alumina from aluminum hydroxide
DE2048207A1 (de) * 1970-10-01 1972-04-06 Kloeckner Humboldt Deutz Ag Einrichtung zur Herstellung von Tonerde aus Tonerdehydrat
WO1997018165A1 (fr) * 1995-11-14 1997-05-22 Metallgesellschaft Aktiengesellschaft Procede de production d'oxyde d'aluminium a partir d'hydroxyde d'aluminium

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2478671A (en) * 2009-01-26 2011-09-14 Outotec Oyj Process and plant for production 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
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
WO2010083961A1 (fr) * 2009-01-26 2010-07-29 Outotec Oyj Procédé et installation pour la production d'oxyde métallique à partir de sels métalliques
CN107709240B (zh) * 2015-06-02 2019-07-16 奥图泰(芬兰)公司 用于热处理颗粒状固体的方法和系统
CN107709240A (zh) * 2015-06-02 2018-02-16 奥图泰(芬兰)公司 用于热处理颗粒状固体的方法和系统
WO2017144469A1 (fr) * 2016-02-23 2017-08-31 Outotec (Finland) Oy Procédé et dispositif pour le traitement thermique de solides granulaires
US10569245B2 (en) 2016-02-23 2020-02-25 Outotec (Finland) Oy Method and device for the heat treatment of granular solids
WO2017157906A1 (fr) * 2016-03-15 2017-09-21 Outotec (Finland) Oy Procédé et installation pour le traitement thermique de solides granulaires
CN109982775A (zh) * 2016-11-22 2019-07-05 奥图泰(芬兰)公司 用于流化床反应器中热处理的方法和设备
WO2018095815A1 (fr) * 2016-11-22 2018-05-31 Outotec (Finland) Oy Procédé et installation de traitement thermique dans un réacteur à lit fluidisé
AU2017365247B2 (en) * 2016-11-22 2019-10-31 Metso Metals Oy Process and plant for thermal treatment in a fluidized bed reactor
CN109982775B (zh) * 2016-11-22 2022-03-29 奥图泰(芬兰)公司 用于流化床反应器中热处理的方法和设备
CN108083294A (zh) * 2018-02-12 2018-05-29 沈阳鑫博工业技术股份有限公司 一种从赤泥中提取氧化铝和氧化钠的装置及方法

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EA016569B1 (ru) 2012-05-30
BRPI0816090A2 (pt) 2015-04-07
DE102007041586A1 (de) 2009-03-05
AU2008291392B2 (en) 2013-05-23
AU2008291392A1 (en) 2009-03-05
DE102007041586B4 (de) 2014-03-27
UA100992C2 (ru) 2013-02-25
BRPI0816090B1 (pt) 2018-09-11

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