CN101563137B - Method of concentrating a bayer process liquor - Google Patents
Method of concentrating a bayer process liquor Download PDFInfo
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- CN101563137B CN101563137B CN200780035168.4A CN200780035168A CN101563137B CN 101563137 B CN101563137 B CN 101563137B CN 200780035168 A CN200780035168 A CN 200780035168A CN 101563137 B CN101563137 B CN 101563137B
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- bayer process
- water
- process waste
- waste liquid
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- 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
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- 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
Abstract
A method for concentrating spent Bayer process liquor, the method comprising the steps of: recovering heat from a Bayer process calciner flue gas; applying at least a portion of the recovered heat to the spent Bayer process liquor; and evaporating water from the spent Bayer process liquor, thereby concentrating the spent Bayer process liquor.
Description
Technical field
The present invention relates to a kind of method of concentrated bayer liquors.Particularly, the present invention relates to utilize the heat reclaiming from discarded Bayer process gas to concentrate the method for bayer liquors.
Background technology
Bayer process is widely used in and for example, from contain the ore (bauxite) of aluminium, produces aluminium oxide.The method comprises, in being commonly referred to as the technique of stripping, at high temperature salic ore is contacted with the causticity aluminate solution of regeneration.In some cases, bauxite can be with a large amount of organic materials, and wherein a part causes in the solution generating and has certain organic compound.
After solution is cooling, add aluminium hydroxide as crystal seed with lure into more aluminium hydroxide from being wherein precipitated out.From causticity aluminate solution, isolate the aluminium hydroxide of precipitation, wherein a part of aluminium hydroxide reuses as crystal seed, and remainder is recovered as product.Remaining causticity aluminate solution is recycled the further stripping for aluminous ore.
Then, in known calcine technology, the aluminium hydroxide of heating recovery is produced aluminium oxide.When aluminium hydroxide produces aluminium oxide according to following reaction, the accessory substance of calcination reaction is water:
2Al(OH)
3→Al
2O
3+3H
2O
Commercial, for example excess air of dissimilar fuel (for example oil, gas, coal) and service condition is used in dissimilar calcining furnace design.Therefore, can produce calciner emission temperature and the composition of certain limit; According to estimates, percentage meter by weight, in calcining gas (" calciner emission ") out, nearly 35%-50% is water, other composition comprises carbon dioxide and volatile organic carbon compound.In addition, calciner emission can contain the alumina particulate of carrying secretly.
A large amount of heats is by calciner emission loss from Bayer process.According to estimates, when the steam in waste gas condenses, the available heat discharging is sensible heat or the latent heat of low level mostly.But, the latter can only under atmospheric conditions, using lower than 100 ℃, normally the dew point of 80-83 ℃ reclaims as low-grade heat.But, although a considerable number of, it has been generally acknowledged that low-grade heat is limited in the application of Bayer process.
The above-mentioned introduction to background technology of the present invention is for the ease of understanding the present invention.But, should be appreciated that this introduction not admits and approve that described any material is the application's preference common practise in Australia area during day.
Summary of the invention
Summary
In whole description, unless context separately has needs, word " all comprises " or its distortion " comprising " or " having comprised " comprises pointed whole or whole collection by being understood to refer to and do not get rid of any other whole or whole collection.
In the context of the present specification, term " dehumidification " is understood to include the air-flow of having removed all or part of steam.
The implication of other term of selecting herein can find at description of the present invention with in full.Unless otherwise defined, all other Science and Technology terms used herein all with the present invention under common the understood implication of field those of skill in the art identical.
It will be understood by those skilled in the art that the content of introducing especially except herein, the present invention can change and revise.Should be appreciated that and the present invention includes all such changes and modifications.The present invention also comprise all institutes of mentioning individually or jointly in description or pointing out in steps, feature, composition and compound, and any and all combination of step or feature or any two or more.
The present invention is not limited to the scope of the specific embodiment as herein described, and they are only used for illustrational object.The product of function equivalent, composition and method are all clearly included in scope of the present invention.
Invention described herein can comprise one or more number ranges.Should be understood that number range has comprised all numerical value within the scope of this, comprise the boundary value of limited range, and contiguous this scope causes the numerical value of identical or essentially identical result, the boundary value of these numerical value next-door neighbour restriction number range.
Whole publications (comprising patent, patent application, journal of writings, laboratory manual, books or other document) of quoting herein all again by reference as a reference.Comprise not forming and made such license, i.e. any reference has all formed a part for the common practise of prior art or various equivalent modifications of the present invention.
Particular content
According to the present invention, a kind of method for concentrated Bayer process waste liquid is provided, the method comprising the steps of:
By Bayer process calciner emission directly being contacted with water and heating this water, from Bayer process calciner emission, reclaim heat;
The heat that at least a portion is reclaimed is applied to Bayer process waste liquid; And
Transpiring moisture from Bayer process waste liquid, thereby concentrated Bayer process waste liquid.
As described in aforementioned background art part, although amount of heat by calciner emission loss from bayer process, these heats only can reclaim as low-grade heat, it has been generally acknowledged that it applies limited in Bayer process.But, have been found that this heat can be used for promoting the moisture in evaporation Bayer process waste liquid.Bayer process needs accurately to control concentration and the ratio of a large amount of compositions, and often need to remove moisture in technique with concentrated liquid.
It will be understood by those skilled in the art that Bayer process waste liquid is to have carried out the precipitate phase of Bayer process but the liquid that is not yet recycled the stripping stage.
Preferably, the step that the heat that at least a portion is reclaimed is applied to Bayer process waste liquid specifically comprises the water of Bayer waste liquid contact heating, thereby heat is applied to Bayer waste liquid cooling this water.
In the preferred embodiment of the present invention, the method comprising the steps of:
Bayer process calciner emission is contacted with cooling water, thereby reclaim heat from Bayer process calciner emission, and heating water;
By more Bayer process waste liquid is contacted with the water of heating, the heat that at least a portion is reclaimed is applied to more Bayer process waste liquid, thereby heat is applied to more Bayer process waste liquid cooling this water; And
Transpiring moisture from this more Bayer process waste liquid, thereby concentrated this more Bayer process waste liquid.
In a preferred embodiment, can repeat step of the present invention so that circulation and/or continuous technique to be provided.
In optimal way of the present invention, water is liquid.In the present invention's height optimal way, liquid is water or is water substantially.
Preferably, calciner emission directly contacts with liquid in solution-air contactor.
Calciner emission directly contacts other multiple advantage is also provided except heat recovery with liquid.
As mentioned above, calciner emission can contain volatile organic carbon compound, and its to atmosphere, to be released on environment be highly less desirable.This compound is dissolved in water, can reduces by calciner emission and discharge them.Quite the Organic Compounds of scope is all water-soluble.Therefore,, when water is water, the Organic Compounds discharging by calciner emission will significantly reduce.
As mentioned above, calciner emission can contain the alumina particulate of carrying secretly, and its to atmosphere, to be released on environment be also highly less desirable.Calciner emission directly contacts at least a portion alumina particulate is stayed in water with water, thereby reduces its discharge capacity.
Preferably, thus calciner emission is contacted with water heat described water and comprise step:
The hot calciner emission that contains water vapour is contacted with cooling water, thereby be cooled at least a portion steam to condense into the degree of aqueous water calciner emission, thereby produce substantially cooling dehumidification calciner emission and warm water.
The basic dehumidification of waste gas brings another advantage.Water acts on the visibility of calciner emission plume substantially.And will not expect to have visible plume from environmental.Waste gas dehumidification by method of the present invention means, no matter at which kind of under fixed temperature, the visible composition in waste gas plume all can reduce.In addition, method of the present invention allows to reclaim the moisture of other loss in atmosphere.
In a mode of the present invention, the method also comprises step:
Heat cooling dehumidification waste gas, to improve its buoyancy, promote to disperse.
Preferably, heat cooling dehumidification waste gas and promote the step of disperseing to improve its buoyancy, comprise by directly or indirectly contacting to heat cooling dehumidification waste gas with thermal source.
It will be understood by those skilled in the art that and can heat with the various heating sources in Bayer process pipeline cooling dehumidification waste gas.In a mode of the present invention, heat can be derived from the aluminium oxide cooler in Bayer process calcining pipeline.In an alternative of the present invention, heat can be derived from low pressure workshop steam.In another alternative of the present invention, heat can be derived from fuel burner.
Will be understood that and can provide more than one device to apply heat to cooling dehumidification waste gas.These apply a plurality of device series windings of heat or be arranged in parallel to cooling dehumidification waste gas.
In a mode of the present invention, by hot calciner emission with before cooling water contacts, the method comprising the steps of:
Make the cooling dehumidification calciner emission contact of hot calciner emission, thereby heat cooling dehumidification calciner emission.
Have been found that in cooling dehumidification toxic emission and be heated before atmosphere, help and improve the buoyancy of waste gas and impel waste gas plume suitably to disperse.
Therefore, the highly preferred embodiment according to the present invention, the method comprising the steps of:
By the hot calciner emission that contains water vapour is directly contacted to cold water, from Bayer process calciner emission, reclaim heat, thereby be cooled at least a portion steam to condense into the degree of aqueous water calciner emission, thereby produce calciner emission and the warm water of cooling basic dehumidification;
By warm water is directly contacted to Bayer process waste liquid, the heat that at least a portion is reclaimed is applied to Bayer waste liquid, thus heating bayer liquors cooling described water;
Evaporation water from Bayer process waste liquid, thereby concentrated Bayer process waste liquid;
The cooling water of at least a portion is contacted to the hot calciner emission that contains moisture again; And
Cooling dehumidification calciner emission is contacted with thermal source, thereby heat described cooling dehumidification calciner emission.
Preferably, thus by calciner emission is contacted with water, from Bayer process calciner emission, reclaim the step that heat heats described water and comprise:
At atmospheric pressure or approach the step that makes calciner emission contact water under atmospheric pressure.
In the context of the present invention, term " approaches atmospheric pressure " and should understand and refers to for making container not need to be verified as the pressure of pressure vessel.
In a preferred embodiment, the step that repeats the method is to provide continuous technique.
The step that calciner emission is directly contacted to water can be realized by any solution-air contactor arrangement well known by persons skilled in the art.For example tray tower, structured packing tower, random packed tower, fluidized packing material tower, the tower solution-air contactor of spray tower and rank are all suitable for method of the present invention.For realizing the desirable solution-air contactor arrangement of the method for the invention, comprise for improving the coefficient of overall heat transmission of solution-air contact and the device of mass transfer rate.Described device can comprise fixedly material filling type, fluidized packing material formula, and uses pallet and baffle plate.The filler that some are suitable, for example polypropylene filler, may be thermal sensitivity, therefore, before being introduced into any device that contains this filler, may reduce the temperature of hot calciner emission.
The convenient approach that realizes the method for the invention is, before hot calciner emission is introduced to any contacting container, hot calciner emission directly to be contacted to a part of water.In the optimal way of invention, hot calciner emission directly contacted a part of hot water before entering any contacting container.
Preferably, thus the step that Bayer process waste liquid contact hot water is applied to bayer liquors by heat specifically comprise Bayer process waste liquid mediate contact hot water, thereby to bayer liquors, apply heat.
Heated device is well known by persons skilled in the art by mediate contact hot water to allow Bayer process waste liquid, and comprises vertical tube falling liquid film, horizontal tube falling liquid film, vertically rises film, autoclave boiler or adding pressure type calciner plant.In a mode of the present invention, thereby the step of Bayer process waste liquid mediate contact hot water heating Bayer process waste liquid is used to the falling film evaporator with shell-side (shell-side) and pipe side (tube-side), the method comprising the steps of:
Hot water is introduced to the shell-side of falling film evaporator;
Bayer waste liquid is introduced to the pipe side of falling film evaporator;
Thereby heating Bayer process waste liquid, and cooling described water.
Should be appreciated that and can provide more than one device to heat Bayer process waste liquid.A plurality of devices that Bayer process waste liquid is heated can be arranged to series winding or parallel.
In a mode of the present invention, the method also comprises step:
Further heat described hot water.
Can utilize available from the thermal source in Bayer process pipeline or available from the external heat source of for example power station or other industrial equipment hot water is further heated.Those skilled artisans will appreciate that the various heating sources that can utilize in Bayer process pipeline.In a mode of the present invention, heat can be derived from the aluminium oxide cooler in Bayer process calcining pipeline.In alternative of the present invention, heat can be derived from low pressure workshop steam.
In a mode of the present invention, the method also comprises step:
Reclaim heat from Bayer process calciner emission before, increase the vapour content in calciner emission.
Preferably, the step that increased the vapour content in calciner emission reclaim heat from Bayer process calciner emission before comprises:
At least a portion calciner emission is transported to separator, so that dehumidification air-flow and rich vapoury air-flow to be provided.
Accompanying drawing explanation
Below in conjunction with the drawings and specific embodiments, introduce the present invention, wherein:
Fig. 1 is the schematic flow sheet that the method according to this invention is shown;
Fig. 2 is the schematic flow sheet illustrating according to the method for first embodiment of the invention;
Fig. 3 is the schematic flow sheet illustrating according to the method for second embodiment of the invention;
Fig. 4 is the schematic flow sheet illustrating according to the method for third embodiment of the invention;
Fig. 5 is the schematic flow sheet illustrating according to the method for four embodiment of the invention;
Fig. 6 is the schematic flow sheet illustrating according to the method for fifth embodiment of the invention; And
Fig. 7 is the schematic flow sheet illustrating according to the method for sixth embodiment of the invention.
Specific embodiment
It will be appreciated by those skilled in the art that content of the present invention described herein can change and revise, and be not limited to introduced certain content.Should be appreciated that and the present invention includes all this variations and modification.The present invention also comprise all institutes of mentioning individually or jointly in description or pointing out in steps, feature, composition and compound, and any and all combination of step or feature or any two or more.
In Fig. 1, provide the old process figure how using according to the inventive method is shown.
According to the present invention, by wet calciner emission 12 feed, to solution-air contactor 14, it directly contacts cooling water flow 16 there.The latent heat reclaiming is passed to cooling water flow 16, thereby by cooling water flow 16 heating, at least a portion steam of warm and humid waste gas 12 condenses into aqueous water, thereby produces the waste gas 18 of cooling basic dehumidification and warm current 20 from warm and humid waste gas 12.
Solution-air contactor 14 is used to increase the coefficient of overall heat transmission and the mass transfer rate of solution-air contact, and utilizes cooling water flow 16 and 12 work of warm and humid calciner emission.Owing to increasing the coefficient of overall heat transmission of solution-air contact and the device 22 of mass transfer rate, may be thermal sensitivity, its may be cooling by it before to solution-air contactor 14 by warm and humid calciner emission 12 feed.
Most stream of warm water 20 is discharged from solution-air contactor 14, and passes to falling film evaporator 24 via water pump 26.
Provide the falling film evaporator 24 that comprises housing parts (not shown) and pipe section (not shown) to concentrate Bayer process waste liquid 28.The stream of warm water 20 that enters falling film evaporator 24 housing parts as thermal source for indirect, therefore from entering evaporation water the steam of Bayer process waste liquid 28 as liquid film through pipe section.Concentrated Bayer process waste liquid 30 is discharged from falling film evaporator 28.After leaving falling film evaporator 24, stream of warm water 20 circulates again as cooling water circulation stream 32.
After leaving falling film evaporator 24, part circulating cooling current 32 loop back cooling water flow 16, and remaining circulating cooling current 32 parts 34 are collected.
The Bayer process waste liquid 28 of heating institute feed, and the steam of generation 36 is transported to condenser 38.
The concentrated Bayer process waste liquid 30 of a part is got back to liquid line 40, and second portion 42 circulations of concentrated Bayer process waste liquid 30 are gone back, and mixes with Bayer process waste liquid 28 before entering falling film evaporator 24.
Think and provide various parameters for example flow velocity, fluid type and temperature except the supplier to necessary, can complete the installation of implementing the required multiple device of the present invention factory used for building by skilled craftsman, and only need a small amount of investment.For member, implement the necessary assembly of the present invention, need to provide specific process data by suitable device fabrication business.An example of the process data of one of applicant gas-firing in the calcining furnace of western australia oil plant provides as follows.
Waste gas streams is approximately: nitrogen 110t/hr, oxygen 6t/hr, carbon dioxide 20t/hr, water 90t/hr, amount to 226t/hr.
Under atmospheric pressure, 165 ℃ of temperature, 83 ℃ of dew points.
With waste gas described in water-quenching, to be cooled to its dew point before gas enters tower.
Enter the water of tower:
62 ℃, the about 2200kL/hr of flow velocity.
The desired properties of tower:
64 ℃ of combustion gas dew points, discharge 81 ℃ of coolant-temperature gages.
The design of evaporimeter needs the information of the physical property of pending Bayer process waste liquid, comprises solution composition, density, viscosity, thermal capacitance, thermal conductivity, steam pressure.
Think that above-mentioned information is enough to make manufacturers design to go out suitable tower, packed tower (Australian Rhine Rhur Pty Co., Ltd for example, tower diameter, filler type, packed height and pressure drop), tray tower (Australian Lisbon Engineering Pty Co., Ltd, design, tower height degree and the pressure drop of tower diameter, dish quantity, dish) and fluidisation turbine towers (Britain Fluid Technologies Co., Ltd, tower diameter, turbine types, static state and fluidized packing material height and pressure drop).
Any those skilled in the art can pass through design manual or technical literature, or heat transfer unit (HTU) (falling film evaporator and steam condenser) described in the heat exchanger designs of any standard of providing of any vaporising device manufacturer (GEA Kestner, the Bertrams Salt Plants of Winterthur City,Switzerland of France).
By in conjunction with based on Chemical Engineering basic principle be present in the expensive database of internal model in Bayer device operation, Bayer process performance and thermodynamic data, Bayer process working experience and based on ASPEN Plus
tM, the software flow graph model of physical property prepackage element in the simulation of ASPEN technology company software process and prior art, comprise performance and the operation of the device based on himself of Bayer process, can design, evaluate and improve embodiments of the present invention.
Should be appreciated that the following numerical value relevant with flow velocity and temperature is that used model and embodiment is peculiar, and be subject to the impact of the parameter of input model.For example, waste gas forms and temperature will affect temperature and the flow velocity in downstream.
Should be appreciated that the position of using the inventive method, particularly lead to the position of suitable radiator (for example, for process for cooling provides water), can affect many steps of the method.
In Fig. 2, the method that according to the present invention the first real mode concentrates Bayer process waste liquid is shown.The method of Fig. 1 and Fig. 2 is substantially similar, and identical Reference numeral represents identical step and feature.Can expect, this embodiment is by for providing for example place of large-scale chilled(cooling) water supply (CWS) of suitable radiator.
In the present embodiment, calciner emission 12 quenches by the water spray 50 of the common about 50-150kL/hr of direct contact, so as before feeding solution-air contactor 14 cooling warm and humid calciner emission 12.
The cooling dehumidification waste gas 18 of discharging from solution-air contactor 14 by gas heater 52 heating, to promote its buoyancy.Gas heater 52 can be by for example direct a small amount of natural gas and the air in burner exhaust stream 18, or by come indirect (need to about 10GJ/hr heat) to carry out work with current, hot gas or hot water heat exchanger.
Approximately 83 ℃ of the stream of warm water of discharging from solution-air contactor 14, and be pumped to falling film evaporator 24, the about 70t/hr of steam 36 that Bayer process waste liquid feed 28 produces there, and in the interior collection of water cooled condenser 54.
In Fig. 3, the method that concentrates Bayer process waste liquid according to second embodiment of the invention is shown.Fig. 1,2 substantially similar with 3 method, identical Reference numeral represents identical step and feature.
Present embodiment is designed to reclaim maybe can not obtain for the place of the cooling enough water supplies of technique at the water that need to increase waste gas implement.This embodiment has also been introduced the example that carrys out the cooling heat from calcining furnace with aluminium oxide.
In this embodiment, the stream of warm water 20 of discharging from solution-air contactor 14 be delivered to two falling film evaporators 24 first before 62, by the used heat 60 from calcining furnace, be heated to approximately 84 ℃.In calcining furnace, in the process of cooling aluminium oxide, obtain used heat 60.Should be appreciated that and can obtain described heat from other source 64 or the other places of Bayer pipeline.
The falling film evaporator 62,66 of two operated in series connection is provided, and the first stage 62 is approximately higher 10 ℃ than the operating temperature of second stage 66.The condensation flash-off steam 68 of first stage 62, with suitable temperature (usually above approximately 60 ℃), with wing fan formula aerial cooler 70 indirect condensings, reduces for the cooling water consumption of technique, therefore improves the clean yield of water.The condensation flash-off steam 72 of the second falling film evaporator 66 is the interior condensation of water cooled condenser 74 (being usually less than 60 ℃).
Enter the flow of hot water 61 of the first falling film evaporator 62 housing parts as the moisture of the thermal source indirect Bayer process waste liquid 28 that also thereby evaporation enters by pipe section as liquid film.Concentrated Bayer process waste liquid 76 leaves the first falling film evaporator 62, and enters the pipe section of the second falling film evaporator 66.
Flow of hot water 61, after leaving the first falling film evaporator 62, enters the housing parts 78 of the second falling film evaporator 66, and as the moisture of thermal source indirect and evaporation and concentration Bayer process waste liquid 76.
Concentrated Bayer process waste liquid 80 leaves the second falling film evaporator 66.
Part recirculation cooling water stream 82, after leaving the second falling film evaporator 66, loops back cooling water flow 16, and the remainder 34 of recirculation cooling water stream 82 is collected simultaneously.
In Fig. 4, the method that concentrates Bayer process waste liquid according to third embodiment of the invention is shown.Fig. 1,2,3 substantially similar with 4 method, identical Reference numeral represents identical step and feature.
This embodiment is designed to need to increase evaporation capacity and further reduce the place enforcement of evaporating required workshop steam.This embodiment has also been introduced the example that carrys out the cooling heat from calcining furnace with aluminium oxide.
The 3rd embodiment and the second embodiment difference are to replace wing fan formula aerial cooler 70 with mechanical steam recompression device 90, to improve the heat that enters the second falling film evaporator 66.
In Fig. 5, the method that concentrates Bayer process waste liquid according to four embodiment of the invention is shown.Fig. 1,2,3,4 substantially similar with 5 method, identical Reference numeral represents identical step and feature.
In this embodiment, a part 100 gas coming through separators 102 of waste gas 12, at least peel off a part of water vapour, and the osmotic flow 104 of steam and dehydration gas is provided ooze residual current 106.Osmotic flow 104 combines with the air-flow part 107 of bypass gases separator 102, to provide air-flow to have the air-flow 108 that steam increases, thereby has improved dew point.Improved the temperature of the current 20 that leave solution-air contactor 104.
It will be understood by those skilled in the art that embodiment described herein, except special instruction, can change and revise.
In an example of this embodiment, at 165 ℃, hot wet calciner emission 100 enters barrier film gas separator 102 with the flow velocity of 141t/hr, comprise for example Nafion of Du Pont separator, produce the vapor permeation stream 104 of 54.5t/hr, and the dehydration gas of 86.5t/hr and 160 ℃ ooze residual current 106.The osmotic flow 104 of steam provides air-flow 108 in conjunction with the wet calciner emission stream of heat 107 flow velocitys with about 61t/hr, and wherein water vapour content approximately 69%.Under about 106kPa, before feed gas-liquid-liquid contactor 14, combined airflow 108 is quenched by the spraying 50 of the common about 50Kl/hr of direct contact.Stream of warm water 20 is left solution-air contactor 14 at approximately 88 ℃, and enters falling film evaporator 24, produces the evaporative air 36 of about 77t/hr in the waste liquid feed 28 of about 2303t/hr.
Leave the cooling dehumidification waste gas 18 of solution-air contactor in conjunction with the exhausting waste gas 113 that residual current 106 produces 129t/hr that oozes of dehydration gas, approximately 50 ℃ of its dew points, approximately 129 ℃ of temperature, are enough to disperse.
In Fig. 6, the method that concentrates Bayer process waste liquid according to fifth embodiment of the invention is shown.Fig. 1,2,3,4,5 substantially similar with 6 method, identical Reference numeral represents identical step and feature.
The 5th embodiment and the 4th embodiment difference are through before falling film evaporator 34, the stream of warm water 20 of discharging from solution-air contactor 14 with used heat 60 heating of calcining furnace.
An example of this embodiment is that the heat of use aluminium oxide cooler 60 is increased to 90.5 ℃ by the temperature of leaving the stream of warm water 20 of solution-air contactor 14, enters stream of warm water 61 generations of falling film evaporator 24 more than the evaporative air 36 of 80t/hr.
In Fig. 7, the method that concentrates Bayer process waste liquid according to sixth embodiment of the invention is shown.Fig. 1,2,3,4,5,6 substantially similar with 7 method, identical Reference numeral represents identical step and feature.
Conventionally under approximately 165 ℃ and atmospheric pressure, the wet calciner emission 12 of heat of the about 202t/hr of flow velocity enters airair heat exchanger 110, there the cooling dehumidification waste gas 18 of its mediate contact.Can expect, at approximately 64 ℃, flow velocity is about to the reinforced airair heat exchanger 110 of cooling dehumidification waste gas of 139t/hr.
In airair heat exchanger 110, from the wet calciner emission 12 of heat, reclaim a part of sensible heat, thereby the wet calciner emission 12 of heat is cooling, approximately 125 ℃ form warm and humid calciner emission 112 streams.
Cooling dehumidification waste gas 18, obtaining sensible heat from the wet calciner emission 12 of heat, is heated to approximately 135 ℃, then as wet calciner emission 114 streams of heat, with 139t/hr, is discharged into atmosphere.
The wet calciner emission 12 of heat is contacted with the waste gas 18 of cooling dehumidification, thereby by 18 heating of the waste gas of cooling dehumidification, substantially improved its buoyancy, when waste gas plume is discharged into atmosphere, can suitably disperse it.
Flow velocity with 202t/hr leaves the warm and humid calciner emission 112 after airair heat exchanger 110, before feeding in raw material to solution-air contactor 14, spraying 50 by the common about 100kL/hr of direct contact is quenched, and at contactor 14 places, it directly contacts cooling water flow 16 with the charging rate of about 1800t/hr with the temperature of approximately 62 ℃.The latent heat reclaiming from warm and humid calciner emission 112 passes to cooling water flow 16, the degree of water that is in a liquid state thereby heating cooling water flow 16 to the steam that makes the warm and humid calciner emission 112 of at least a portion condenses, thus produce cooling dehumidification waste gas 18 and stream of warm water 20.
A large amount of stream of warm water 20 are left solution-air contactor 14 with the flow velocity of about 1864t/hr, and enter falling film evaporator 24 by water pump 26.
Stream of warm water 20 enters the housing parts of falling film evaporator 24, the about 1864t/hr of flow velocity, and concentrated Bayer process waste liquid 30 is discharged from falling film evaporator 24.After leaving falling film evaporator 24, stream of warm water circulates again as cooling water circulation stream 32.
Claims (23)
1. a method for concentrated Bayer process waste liquid, the method comprising the steps of:
By Bayer process calciner emission directly being contacted with water and heating this water, from Bayer process calciner emission, reclaim heat;
The heat that at least a portion is reclaimed is applied to Bayer process waste liquid; And
Transpiring moisture from Bayer process waste liquid, thereby concentrated Bayer process waste liquid.
2. the method for concentrated Bayer process waste liquid according to claim 1, wherein, the step that the heat that at least a portion is reclaimed is applied to Bayer process waste liquid comprises Bayer process waste liquid contact with the water through heating, thereby heats also cooling this water of Bayer process waste liquid.
3. the method for concentrated Bayer process waste liquid according to claim 2, wherein the method comprising the steps of:
Bayer process calciner emission is contacted with cooling water, thereby reclaim heat from Bayer process calciner emission, and heating water;
By more Bayer process waste liquid is contacted with the water through heating, the heat that at least a portion is reclaimed is applied to this more Bayer process waste liquid, thereby heats this more Bayer process waste liquid cooling described water; And
Transpiring moisture from this more Bayer process waste liquid, thereby concentrated this more Bayer process waste liquid.
4. according to the method for the concentrated Bayer process waste liquid described in the claims 1, wherein, calciner emission directly contacts with water in convection type solution-air contactor.
5. according to the method for the concentrated Bayer process waste liquid described in the claims 1, thereby the step that wherein calciner emission is contacted to heating water with water comprises step:
The hot calciner emission that contains steam is contacted with cooling water, thereby be cooled at least a portion steam to condense into the degree of aqueous water calciner emission, thereby produce cooling dehumidification calciner emission and warm water.
6. the method for concentrated Bayer process waste liquid according to claim 5, wherein, the method also comprises step:
Heating promotes its dispersion through cooling dehumidification waste gas to improve its buoyancy.
7. the method for concentrated Bayer process waste liquid according to claim 6, wherein, heats through cooling dehumidification waste gas and promotes the step of disperseing to improve its buoyancy, comprising:
By directly contacting with thermal source or mediate contact is heated this through cooling dehumidification waste gas.
8. according to the method for the concentrated Bayer process waste liquid described in the claims 1, wherein, calciner emission is directly contacted from Bayer process calciner emission and reclaims heat with water, thereby the step of heating water comprises:
At atmospheric pressure or approach under atmospheric pressure the step that calciner emission is contacted with water.
9. the method for concentrated Bayer process waste liquid according to claim 5, wherein, by hot calciner emission with before cooling water contacts, the method comprising the steps of:
Hot calciner emission is contacted with cooling dehumidification calciner emission, thereby by cooling dehumidification calciner emission heating.
10. the method for concentrated Bayer process waste liquid according to claim 1, wherein, the step that calciner emission is directly contacted with water is realized by solution-air contactor arrangement.
The method of 11. concentrated Bayer process waste liquids according to claim 10, wherein, described solution-air contactor arrangement comprises tray tower, structured packing tower, random packed tower, fluidized packing material tower, the tower solution-air contactor of spray tower and rank.
The method of 12. concentrated Bayer process waste liquids according to claim 10, wherein, comprises for improving the heat transfer of solution-air contact and the device of mass transfer rate for realizing the solution-air contactor arrangement of the inventive method.
The method of 13. concentrated Bayer process waste liquids according to claim 10, wherein, the method comprises:
In solution-air contactor, before calciner emission is contacted with water,
Reduce the step of calciner emission temperature.
The method of 14. concentrated Bayer process waste liquids according to claim 13, wherein, the step that reduces calciner emission temperature comprises:
In solution-air contactor, before calciner emission is contacted with water,
Make calciner emission directly contact the step of a part of water.
The method of 15. concentrated Bayer process waste liquids according to claim 2, wherein, contacts Bayer process waste liquid and the water through heating to heat the step of Bayer process waste liquid, and comprise and make the mediate contact of Bayer process waste liquid through the water of heating, thus heating Bayer process waste liquid.
The method of 16. concentrated Bayer process waste liquids according to claim 15, wherein, make the mediate contact of Bayer process waste liquid through the water of heating by vertical tube falling liquid film, horizontal tube falling liquid film, vertically rise film, autoclave boiler or adding pressure type calciner plant and realize.
The method of 17. concentrated Bayer process waste liquids according to claim 16, wherein, the mediate contact of Bayer process waste liquid is realized by the falling film evaporator with shell-side and pipe side through the water of heating, and the method comprising the steps of:
Water through heating is introduced to the shell-side of falling film evaporator;
Bayer process waste liquid is introduced to the pipe side of falling film evaporator;
Thereby heating Bayer process waste liquid, and cooling water.
The method of 18. concentrated Bayer process waste liquids according to claim 15, wherein, provides more than one device to heat Bayer process waste liquid.
19. according to the method for the concentrated Bayer process waste liquid described in the claims 1, comprises step:
The moisture of evaporation condenses from Bayer process waste liquid.
20. according to the method for the concentrated Bayer process waste liquid described in the claims 1, and wherein the method also comprises:
The step further water through heating being heated.
21. according to the method for the concentrated Bayer process waste liquid described in the claims 1, and wherein the method also comprises step:
Reclaim the step of heat from Bayer process calciner emission before, improve the water vapour content of calciner emission.
The method of 22. concentrated Bayer process waste liquids according to claim 21, wherein,
The step that improved the water vapour content of calciner emission before the step that reclaims heat from Bayer process calciner emission comprises:
Make at least a portion calciner emission enter separator, so that dehydration air-flow and rich vapoury air-flow to be provided.
23. according to the method for the concentrated Bayer process waste liquid described in the claims 1, wherein repeats the step of described method, so that continuous technique to be provided.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AU2006905250A AU2006905250A0 (en) | 2006-09-22 | Method of Concentrating a Bayer Process Liquor | |
| AU2006905250 | 2006-09-22 | ||
| PCT/AU2007/001407 WO2008034196A1 (en) | 2006-09-22 | 2007-09-21 | Method of concentrating a bayer process liquor |
Publications (2)
| Publication Number | Publication Date |
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| CN101563137A CN101563137A (en) | 2009-10-21 |
| CN101563137B true CN101563137B (en) | 2014-03-26 |
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| CN200780035168.4A Active CN101563137B (en) | 2006-09-22 | 2007-09-21 | Method of concentrating a bayer process liquor |
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| Country | Link |
|---|---|
| CN (1) | CN101563137B (en) |
| AU (2) | AU2007299598B2 (en) |
| WO (1) | WO2008034196A1 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| AU2009225953B2 (en) * | 2008-03-18 | 2013-11-21 | Alcoa Of Australia Limited | Method of concentrating a Bayer process liquor |
| CN108529657A (en) * | 2018-04-18 | 2018-09-14 | 太原理工大学 | Multi-effect evaporating device and technique applied to alumina refinery |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0335707A3 (en) * | 1988-03-30 | 1991-07-03 | Alcan International Limited | Method for transferring heat between process liquor streams |
| CN1519520A (en) * | 2003-02-07 | 2004-08-11 | ʸ����ҵ��ʽ���� | Absorbing cold/hot water heater |
| WO2005077830A1 (en) * | 2004-02-16 | 2005-08-25 | Alcoa Of Australia Limited | Treatment of alkaline bayer process residues |
| CN1864812A (en) * | 2006-04-24 | 2006-11-22 | 南京大学 | A nitric oxides (NOX) waste pollution control in industrial process and resource reclaiming method |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU3297995A (en) * | 1994-09-30 | 1996-04-18 | Alcoa Of Australia Limited | Process for the removal of sodium oxalate |
| AUPP531498A0 (en) * | 1998-08-17 | 1998-09-10 | Comalco Aluminium Limited | Feed processing for improved alumina process performance |
| AUPP624198A0 (en) * | 1998-09-30 | 1998-10-22 | Comalco Aluminium Limited | Feed processing for improved alumina process performance |
-
2007
- 2007-09-21 WO PCT/AU2007/001407 patent/WO2008034196A1/en active Application Filing
- 2007-09-21 AU AU2007299598A patent/AU2007299598B2/en active Active
- 2007-09-21 CN CN200780035168.4A patent/CN101563137B/en active Active
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0335707A3 (en) * | 1988-03-30 | 1991-07-03 | Alcan International Limited | Method for transferring heat between process liquor streams |
| CN1519520A (en) * | 2003-02-07 | 2004-08-11 | ʸ����ҵ��ʽ���� | Absorbing cold/hot water heater |
| WO2005077830A1 (en) * | 2004-02-16 | 2005-08-25 | Alcoa Of Australia Limited | Treatment of alkaline bayer process residues |
| CN1864812A (en) * | 2006-04-24 | 2006-11-22 | 南京大学 | A nitric oxides (NOX) waste pollution control in industrial process and resource reclaiming method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101563137A (en) | 2009-10-21 |
| WO2008034196A1 (en) | 2008-03-27 |
| AU2007299598B2 (en) | 2010-11-18 |
| AU2011100201A4 (en) | 2011-03-17 |
| AU2007299598A1 (en) | 2008-03-27 |
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