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WO2008034196A1 - Procédé de concentration d'une liqueur bayer - Google Patents

Procédé de concentration d'une liqueur bayer Download PDF

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Publication number
WO2008034196A1
WO2008034196A1 PCT/AU2007/001407 AU2007001407W WO2008034196A1 WO 2008034196 A1 WO2008034196 A1 WO 2008034196A1 AU 2007001407 W AU2007001407 W AU 2007001407W WO 2008034196 A1 WO2008034196 A1 WO 2008034196A1
Authority
WO
WIPO (PCT)
Prior art keywords
bayer process
flue gas
process liquor
fluid
spent bayer
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/AU2007/001407
Other languages
English (en)
Inventor
Dean Ilievski
Peter Stewart Hay
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.)
Alcoa of Australia Ltd
Original Assignee
Alcoa of Australia Ltd
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
Priority claimed from AU2006905250A external-priority patent/AU2006905250A0/en
Application filed by Alcoa of Australia Ltd filed Critical Alcoa of Australia Ltd
Priority to CN200780035168.4A priority Critical patent/CN101563137B/zh
Priority to AU2007299598A priority patent/AU2007299598B2/en
Publication of WO2008034196A1 publication Critical patent/WO2008034196A1/fr
Anticipated expiration legal-status Critical
Priority to AU2011100201A priority patent/AU2011100201A4/en
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
    • C01F7/04—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom
    • C01F7/06—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom by treating aluminous minerals or waste-like raw materials with alkali hydroxide, e.g. leaching of bauxite according to the Bayer process
    • C01F7/0606—Making-up the alkali hydroxide solution from recycled spent liquor
    • 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

Definitions

  • the present invention relates to a method for concentrating a Bayer process liquor. More specifically, the present invention relates to a method for concentrating a Bayer process liquor utilising heat recovered from a waste Bayer process gas.
  • the Bayer process is widely used for the production of alumina from aluminium containing ores, such as bauxite.
  • the process involves contacting alumina- containing ores with recycled caustic aluminate solutions, at elevated temperatures, in a process commonly referred to as digestion.
  • a significant amount of organic material accompanies the bauxite, a portion of which is responsible for the presence of a range of organic compounds in the resulting solution.
  • aluminium hydroxide is added as seed to induce the precipitation of further aluminium hydroxide therefrom.
  • the precipitated aluminium hydroxide is separated from the caustic aluminate solution, with a portion of the aluminium hydroxide being recycled to be used as seed and the remainder recovered as product.
  • the remaining caustic aluminate solution is recycled for further digestion of alumina containing ore.
  • the recovered aluminium hydroxide is then heated to produce alumina, in a process known as calcination.
  • a by-product of the calcination reaction is water, as aluminium hydroxide produces alumina according to the following reaction:
  • calciner flue gas temperatures and compositions may occur; and it is estimated that approximately 35% to 50% by mass % of the gas leaving calcination ('calciner flue gas') is water, with other components including carbon dioxide and volatile organic carbon compounds. Additionally, the calciner flue gas may contain entrained particulate alumina.
  • dehumidified shall be understood to encompass gas streams in which all or a portion of the water vapour has been removed.
  • Other definitions for selected terms used herein may be found within the description of the invention and apply throughout. Unless otherwise defined, all other scientific and technical terms used herein have the same meaning as commonly understood to one of ordinary skill in the art to which the invention belongs.
  • the invention described herein may include one or more ranges of values.
  • a range of values will be understood to include all values within the range, including the values defining the range, and values adjacent to the range which lead to the same or substantially the same outcome as the values immediately adjacent to that value which defines the boundary to the range.
  • a spent Bayer process liquor is liquor that has been subjected to the precipitation phase of the Bayer process, and not yet been recycled back to the digestion phase.
  • the step of recovering heat from a Bayer process calciner flue gas more specifically comprises the step of contacting the calciner flue gas with a body of fluid, thereby heating the body of fluid.
  • the step of applying at least a portion of the recovered heat to the spent Bayer process liquor more specifically comprises contacting the spent Bayer process liquor with the heated body of fluid, thereby applying heat to the spent Bayer process liquor and cooling the body of fluid.
  • the method comprises the steps of:
  • the method comprises the step of:
  • the steps of the present invention may be repeated to provide a cyclical and/or continuous process.
  • the fluid is a liquid.
  • the liquid is, or is substantially, water.
  • the step of contacting the calciner flue gas with the body of liquid comprises directly contacting the calciner flue gas with the body of liquid.
  • the calciner flue gas is directly contacted with the body of liquid in a counter-current gas-liquid contactor.
  • calciner flue gas may contain volatile organic carbon compounds, the release of which into the atmosphere is highly environmentally undesirable. To the extent that such compounds are soluble in the body of liquid, their release by calciner flue gas in reduced. A significant range of volatile organic carbon compounds are soluble in water. Accordingly, where the fluid is water, the reduction in volatile organic carbon compounds released by way of the calciner flue gas will be appreciable.
  • calciner flue gas may contain entrained particulate alumina, the release of which into the atmosphere is also environmentally undesirable.
  • Direct contact of the calciner flue gas with the fluid causes at least a portion of the particulate alumina to remain in the fluid, thereby reducing the quantity exhausted.
  • contacting the calciner flue gas with a body of fluid, thereby heating the body of fluid comprises the step of:
  • the substantial dehumidification of the flue gas affords yet another advantage. Water contributes substantially to the visibility of the calciner flue gas plume. A visible plume is undesirable from an environmental perspective.
  • the dehumidification of the flue gas by the method of the present invention means that, at any given temperature, the visible component of the flue gas plume is reduced. Further, the method of the present invention allows recovery of water that would otherwise be lost to the atmosphere.
  • the method comprises the further step of:
  • the heat may be sourced from the alumina coolers in the Bayer calcination circuit.
  • the heat may be sourced from low pressure plant steam.
  • the heat may be sourced from a fuel fired burner.
  • the method comprises the step of:
  • heating the cooled dehumidified flue gas before discharging to the atmosphere is desirable to assist the flue gas buoyancy and enable the flue gas plume to properly disperse.
  • the method comprises the steps of:
  • the step of recovering heat from a Bayer process calciner flue gas by contacting the calciner flue gas with a body of fluid, thereby heating the body of fluid comprises the step of;
  • near atmospheric pressure shall be understood to indicate a pressure such that the vessel does not require certification as a pressure vessel.
  • the steps of the method are repeated to provide a continuous process.
  • the step of directly contacting the calciner flue gas with a body of fluid may be effected in any of a range of gas-liquid contactor apparatus known to persons skilled in the art.
  • tray tower, structured packed tower, random packed tower, fluidized packed tower, spray tower and cascade tower gas-liquid contactor apparatus are appropriate for use in the method of the present invention.
  • the gas-liquid contactor apparatus used to effect the method of the present invention contains means designed to increase the heat and mass transfer efficiency of the gas-liquid contact.
  • Said means may include static packing, fluidized packing and the use of trays and baffles.
  • Some convenient forms of packing, such as polypropylene packing may be heat sensitive and it may be necessary to reduce the temperature of the hot calciner flue gas before introducing such into any apparatus containing such packing.
  • a convenient way of achieving such in accordance with the method of the present invention is to directly contact the hot calciner flue gas with a portion of the body of fluid prior to introducing such into any contacting vessel.
  • the hot calciner flue gas is directly contacted with a portion of the heated body of fluid prior to entering any contacting vessel.
  • the step of contacting the spent Bayer process liquor with the heated body of fluid, thereby applying heat to the spent Bayer process liquor more specifically comprises indirectly contacting the spent Bayer process liquor with the heated body of fluid, thereby applying heat to the spent Bayer process liquor.
  • Apparatus allowing the spent Bayer process liquor to be heated by indirect contact with the heated body of fluid are known to persons skilled in the art, and include vertical tube falling film, horizontal tube falling film, vertical rising film, kettle boiler and forced circulation apparatus.
  • the step of indirectly contacting the spent Bayer process liquor with the heated body of fluid, thereby heating of the spent Bayer process liquor utilizes a falling film evaporator having a shell-side and a tube-side, and the method comprises the steps of:
  • the method comprises the further step of:
  • the heated body of fluid may be further heated by utilising sources of heat available within the Bayer circuit or external sources available from, for example, power stations or other industrial facilities, It will be appreciated by those skilled in the art that a variety of heat sources in Bayer circuit may be utilized.
  • the heat may be sourced from the alumina coolers in the Bayer calcination circuit.
  • the heat may be sourced from low pressure plant steam.
  • the method comprises the further step of: increasing the water vapour content of the calciner flue gas prior to the step of recovering heat from the Bayer process calciner flue gas.
  • Figure 1 is a schematic flow sheet showing a method in accordance with the present invention
  • Figure 2 is a schematic flow sheet showing a method in accordance with a first embodiment of the present invention
  • Figure 3 is a schematic flow sheet showing a method in accordance with a second embodiment of the present invention.
  • Figure 4 is a schematic flow sheet showing a method in accordance with a third embodiment of the present invention.
  • Figure 5 is a schematic flow sheet showing a method in accordance with a fourth embodiment of the present invention.
  • Figure 6 is a schematic flow sheet showing a method in accordance with a fifth embodiment of the present invention
  • Figure 7 is a schematic flow sheet showing a method in accordance with a sixth embodiment of the present invention.
  • Figure 1 there is provided a generic flow sheet showing how a method in accordance with the present invention may be utilised.
  • humidified calciner flue gas 12 is fed to a gas-liquid contactor 14 where it is directly contacted with a cooled water stream 16.
  • Latent heat recovered from the warm humidified flue gas 12 is transferred to the cooled water stream 16, thereby heating the cooled water stream 16, at least a portion of the water vapour of the warm humidified calciner flue gas 12 condenses to liquid water, so producing a cooled substantially dehumidified flue gas 18 and a warm water stream 20.
  • the gas-liquid contactor 14 is designed to increase the heat and mass transfer efficiency of the gas-liquid contact and is operated with counter-flow of the cooled water stream 16 and the warm humidified calciner flue gas 12.
  • As the means 22 to increase the heat and mass transfer efficiency of the gas-liquid contact may be heat sensitive, it may be necessary to cool the warm humidified calciner flue gas 12 prior to feeding it to the gas-liquid contactor 14.
  • the falling film evaporator 24 comprising a shell portion (not shown) and tube portion (not shown) is provided to concentrate Bayer spent liquor 28.
  • the warm water stream 20 entering the shell portion of the falling film evaporator 24 is used as a heat source to indirectly apply heat and thereby evaporate water from Bayer spent liquor 28 entering as a liquor film via the tube portion.
  • the warm water stream 20, after leaving the falling film evaporator 24, is recycled as a cooled water recycled stream 32.
  • the Bayer spent liquor feed 28 is heated, and a vapour 36 generated is transferred to a condenser 38.
  • a portion of the concentrated Bayer spent liquor 30 is returned to the liquor circuit 40, whilst a second portion of the concentrated Bayer spent liquor 30 is recycled back 42 and mixed with the Bayer spent liquor feed 28 prior to entering the falling film evaporator 24.
  • the approximate flue gas flows are: nitrogen 110 t/hr, oxygen 6 t/hr, carbon dioxide 20 t/hr, water 90 t/hr, Total 226 t/hr.
  • the flue gas is to be quenched with water to cool the gas to its dewpoint before entering the tower.
  • the design of the evaporator requires information on the physical properties of the Bayer spent liquor being treated, including, liquor composition, density, viscosity, heat capacity, thermal conductivity, vapour pressure.
  • a supplier to design an appropriate tower, e.g. a packed tower, (Rhine Rhur Pty Ltd, Australia, tower diameter, packing type, packed height and pressure drop), a tray tower, (Lisbon Engineering Pty Ltd, Australia, tower diameter, number of trays, tray design, tower height and pressure drop), and a fluidized turboid tower, (Fluid Technologies Ltd, UK, tower diameter, turboid type, static and fluidized packed height and pressure drop).
  • a packed tower e.g. a packed tower, (Rhine Rhur Pty Ltd, Australia, tower diameter, packing type, packed height and pressure drop)
  • a tray tower e.g. a tray tower, (Lisbon Engineering Pty Ltd, Australia, tower diameter, number of trays, tray design, tower height and pressure drop)
  • a fluidized turboid tower e.g. a packed tower, (Rhine Rhur Pty Ltd, Australia, tower diameter, packing type, packed height and pressure drop)
  • a tray tower e
  • the heat transfer equipment (the falling film evaporator and vapour condenser), could be designed by any person skilled in the art, by using to any standard heat exchanger design text, or references from the technical literature, or by a supplier of evaporation equipment (GEA Kestner, France, Bertrams Salt Plants, Winterthur, Switzerland).
  • the embodiments of the invention were formulated, evaluated and refined using a combination of inhouse models built on chemical engineering first principles and tuned to existing Bayer unit operations, an extensive database of Bayer properties and thermodynamic data, Bayer operating experience and flowsheet models built within ASPEN PlusTM, ASPEN Technology Inc. software process simulation software with state-of -the-art physical properties packages, including added Bayer process properties and unit operations built inhouse.
  • FIG 2 there is shown a method for concentrating spent Bayer process liquor in accordance with a first embodiment of the present invention.
  • the methods of Figures 1 and 2 are substantially similar and like numerals denote like steps and features. It is envisaged that the present embodiment will be utilised where there is provided a suitable heat sink such as a large cooling water supply.
  • the calciner flue gas 12 is quenched by direct contact with a water mist spray 50 typically at approximately 50 to 150 kl_/hr, to cool the warm humidified calciner flue gas 12 before feeding to the gas-liquid contactor 14.
  • the cooled dehumidified flue gas 18 exiting the gas-liquid contactor 14 is heated by a gas heater 52 to aid its buoyancy.
  • the gas heater 52 may operate by, for example, direct combustion of a small amount of natural gas and air in the flue gas stream 18, or by indirect heating with a steam, hot gases or hot water heat exchanger, requiring about 10 GJ/hr heat.
  • the warm water stream exits the gas-liquid contactor 14 at approximately 83 0 C and is pumped to the falling film evaporator 24 where approximately 70 t/hr of vapour 36 are generated from the Bayer spent liquor feed 28 and collected in a water cooled condenser 54.
  • Figure 3 there is shown a method for concentrating spent Bayer process liquor in accordance with a second embodiment of the present invention.
  • the methods of Figures 1 , 2 and 3 are substantially similar and like numerals denote like steps and features.
  • the present embodiment is designed for implementation at sites where it is desired to increase the recovery of water from the flue gas or when a adequate water supply for process cooling is not available.
  • the present embodiment further depicts examples of the use of alumina cooling heat from the calciners.
  • the warm water stream 20 exiting the gas-liquid contactor 14 is heated with waste heat 60 from the calciner to approximately 84 0 C before being passed to the first 62 of two falling film evaporators to provide a heated water stream 61.
  • the waste heat 60 is heat obtained during the cooling of alumina in the calciner. It will be appreciated that heat may be obtained from other sources 64 in the Bayer circuit or elsewhere.
  • the condensing flash vapour 68 from the first stage 62 is at a suitable temperature, (typically above about 60 0 C), to use indirect condensing with fin fan air coolers 70 reducing the consumption of water for process cooling, thus increasing the net recovery of water.
  • the condensing flash vapour 72 from the second falling film evaporator 66 is condensed in a water cooled condenser 74 (typically below 60 0 C).
  • the heated water stream 61 entering the shell portion of the first falling film evaporator 62 is used as a heat source to apply indirect heat and thereby evaporate water from Bayer spent liquor 28 entering as a liquor film via the tube portion.
  • Concentrated Bayer spent liquor 76 exits the first falling film evaporator 62 and enters the tube portion of the second falling film evaporator 66.
  • the heated water stream 61 after leaving the first falling film evaporator 62, enters the shell portion 78 of the second falling film evaporator 66 and is used as a heat source to apply indirect heat and thereby evaporate water from concentrated Bayer spent liquor 76.
  • FIG 4 there is shown a method for concentrating spent Bayer process liquor in accordance with a third embodiment of the present invention.
  • the methods of Figures 1 , 2, 3 and 4 are substantially similar and like numerals denote like steps and features.
  • the present embodiment is designed for implementation at sites where it is desired to increase the amount of evaporation and further reduce the plant steam needed for evaporation.
  • the present embodiment further depicts examples of the use of alumina cooling heat from the calciners.
  • the third embodiment differs from the second embodiment by the replacement of the finned fan air cooler 70 with mechanical vapour recompression 90 to upgrade the heat entering the second falling film evaporator 66.
  • FIG 5 there is shown a method for concentrating spent Bayer process liquor in accordance with a fourth embodiment of the present invention.
  • the methods of Figures 1 , 2, 3 and 4 are substantially similar and like numerals denote like steps and features.
  • a portion 100 of the flue gas 12 is passed through a gas separator 102 to strip off at least a portion of the water vapour and provide a permeate of water vapour 104 and a retentate stream of dehydrated gas 106.
  • the permeate 104 is combined with the portion 107 of the flue gas by-passing the gas separator 102 to provide a stream of 108 providing a stream with increased water vapour, thereby increasing the dewpoint.
  • the temperature of the water stream 20 exiting the gas-liquid contactor 14 is increased.
  • hot humidified calciner flue gas 100 at 165 0 C with a flow rate of approximately 141 t/hr is passed into a membrane gas separator 102, comprising for example, a Dupont Nafion membrane, to produce a permeate of water vapour 104 of 54.5 t/hr and a retentate stream of dehydrated gas 106 of 86.5 t/hr and 160 0 C.
  • the permeate of water vapour 104 is combined with the hot humidified calciner flue gas stream 107 with a flow rate of approximately 61 t/hr to provide a stream 108 with a vapour content of approximately 69 %.
  • the combined stream 108 is quenched by direct contact with a mist spray 50 typically at approximately 50 kL/hr before being fed to the gas-liquid contactor 14 at approximately 106 kPa.
  • the warm water stream 20 exits the gas-liquid contactor 14 at approximately 88 0 C and is passed to the falling film evaporator 24 generating approximately 77 t/hr evaporation 36 on a spent liquor feed 28 of approximately 2303 t/hr.
  • the cooled dehumidified flue gas 18 leaving the gas-liquid contactor is combined with the retentate stream of dehydrated gas 106 producing a flue gas exhaust 113 of 129 t/hr with an approximate dew point of 50 0 C and a temperature of about 129 0 C, sufficient for acceptable dispersion.
  • FIG 6 there is shown a method for concentrating spent Bayer process liquor in accordance with a fifth embodiment of the present invention.
  • the methods of Figures 1 , 2, 3, 4 and 5 are substantially similar and like numerals denote like steps and features.
  • the fifth embodiment differs from the fourth embodiment by the heating of the warm water stream 20 exiting the gas-liquid contactor 14 with waste heat 60 from the calciner, or other available heat sources 64, before being passed to the falling film evaporator 34.
  • One example of the embodiment uses the heat from the alumina coolers 60 to increase the temperature of the warm water stream 20 leaving the gas-liquid contactor 14 to 90.5 0 C in the warm water stream 61 entering the falling film evaporators 24 generating more than 80 t/hr of evaporation 36.
  • FIG 7 there is shown a method for concentrating spent Bayer process liquor in accordance with a sixth embodiment of the present invention.
  • the methods of Figures 1 , 2, 3, 4, 5 and 6 are substantially similar and like numerals denote like steps and features
  • Hot humidified calciner flue gas 12 typically at about 165 0 C and atmospheric pressure with a flow rate of approximately 202 t/hr is passed into a gas-gas heat exchanger 110, where it is indirectly contacted with cooled dehumidified flue gas 18. It is envisaged that a flow rate of approximately 139 t/hr of cooled dehumidified flue gas at approximately 64 0 C is fed to the gas-gas heat exchanger 110
  • the gas-gas heat exchanger 110 a portion of the sensible heat is recovered from the hot humidified calciner flue gas 12 thereby cooling the hot humidified calciner flue gas 12 to form a stream of warm humidified calciner flue gas 112, at approximately 125 0 C.
  • the warm humidified calciner flue gas 112 after exiting from the gas-gas heat exchanger 110 at a flow rate of 202 t/hr is quenched by direct contact with a mist spray 50 typically at approximately 100 kl_/hr before being fed to the gas-liquid contactor 14 where it is directly contacted with the cooled water stream 16 with a feed rate of approximately 1800 t/hr at approximately 62 0 C.
  • Latent heat recovered from the warm humidified flue gas 112 is transferred to the cooled water stream 16, thereby heating the cooled water stream 16 to such an extent that at least a portion of the water vapour of the warm humidified calciner flue gas 112 condenses to liquid water, so producing the cooled dehumidified flue gas 18 and the warm water stream 20.
  • the warm water stream 20 enters the shell portion of the falling film evaporator 24, at a flow rate of approximately 1864 t/hr and concentrated Bayer spent liquor 30 exits the falling film evaporator 24.
  • the warm water stream 20, after leaving the falling film evaporator 24, is recycled as a cooled water recycled stream 32.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Geology (AREA)
  • Inorganic Chemistry (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

L'invention concerne un procédé de concentration d'une liqueur Bayer résiduaire. Ce procédé comprend les étapes qui consistent : à récupérer de la chaleur à partir de gaz de combustion d'un four de calcination utilisé dans un procédé Bayer; à appliquer au moins une partie de la chaleur récupérée à la liqueur de Bayer résiduaire; et à évaporer l'eau présente dans la liqueur Bayer résiduaire, ce qui permet de concentrer la liqueur Bayer résiduaire.
PCT/AU2007/001407 2006-09-22 2007-09-21 Procédé de concentration d'une liqueur bayer Ceased WO2008034196A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
CN200780035168.4A CN101563137B (zh) 2006-09-22 2007-09-21 浓缩拜耳法溶液的方法
AU2007299598A AU2007299598B2 (en) 2006-09-22 2007-09-21 Method of concentrating a Bayer process liquor
AU2011100201A AU2011100201A4 (en) 2006-09-22 2011-02-18 Method of Concentrating a Bayer Process Liquor

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AU2006905250A AU2006905250A0 (en) 2006-09-22 Method of Concentrating a Bayer Process Liquor
AU2006905250 2006-09-22

Publications (1)

Publication Number Publication Date
WO2008034196A1 true WO2008034196A1 (fr) 2008-03-27

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PCT/AU2007/001407 Ceased WO2008034196A1 (fr) 2006-09-22 2007-09-21 Procédé de concentration d'une liqueur bayer

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CN (1) CN101563137B (fr)
AU (2) AU2007299598B2 (fr)
WO (1) WO2008034196A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2009114910A1 (fr) * 2008-03-18 2009-09-24 Alcoa Of Australia Limited Procédé de concentration d'une liqueur de procédé bayer

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108529657A (zh) * 2018-04-18 2018-09-14 太原理工大学 应用于氧化铝精炼厂的多效蒸发装置及工艺

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0335707B1 (fr) * 1988-03-30 1994-05-25 Alcan International Limited Procédé pour transférer de la chaleur entre différents courants liquides
AU3297995A (en) * 1994-09-30 1996-04-18 Alcoa Of Australia Limited Process for the removal of sodium oxalate
WO2000010919A1 (fr) * 1998-08-17 2000-03-02 Comalco Aluminium Limited Traitement de la charge d'alimentation permettant d'ameliorer la performance du traitement de l'oxyde d'aluminium
WO2000018685A1 (fr) * 1998-09-30 2000-04-06 Comalco Aluminium Limited Traitement d'une charge pour l'amelioration d'un procede d'obtention de l'alumine
WO2005077830A1 (fr) * 2004-02-16 2005-08-25 Alcoa Of Australia Limited Traitement de residus alcalins issus de procede bayer

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2004239558A (ja) * 2003-02-07 2004-08-26 Yazaki Corp 吸収式冷温水機
CN100396360C (zh) * 2006-04-24 2008-06-25 南京大学 一种工业过程氮氧化物(nox)废气治理及资源化的方法

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0335707B1 (fr) * 1988-03-30 1994-05-25 Alcan International Limited Procédé pour transférer de la chaleur entre différents courants liquides
AU3297995A (en) * 1994-09-30 1996-04-18 Alcoa Of Australia Limited Process for the removal of sodium oxalate
WO2000010919A1 (fr) * 1998-08-17 2000-03-02 Comalco Aluminium Limited Traitement de la charge d'alimentation permettant d'ameliorer la performance du traitement de l'oxyde d'aluminium
WO2000018685A1 (fr) * 1998-09-30 2000-04-06 Comalco Aluminium Limited Traitement d'une charge pour l'amelioration d'un procede d'obtention de l'alumine
WO2005077830A1 (fr) * 2004-02-16 2005-08-25 Alcoa Of Australia Limited Traitement de residus alcalins issus de procede bayer

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2009114910A1 (fr) * 2008-03-18 2009-09-24 Alcoa Of Australia Limited Procédé de concentration d'une liqueur de procédé bayer
CN102015048A (zh) * 2008-03-18 2011-04-13 美铝澳大利亚有限公司 用于浓缩拜耳工艺液体的方法
AU2009225953B2 (en) * 2008-03-18 2013-11-21 Alcoa Of Australia Limited Method of concentrating a Bayer process liquor

Also Published As

Publication number Publication date
AU2011100201A4 (en) 2011-03-17
AU2007299598B2 (en) 2010-11-18
AU2007299598A1 (en) 2008-03-27
CN101563137A (zh) 2009-10-21
CN101563137B (zh) 2014-03-26

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