CA2018155A1 - Alumina crystal growth additive - Google Patents
Alumina crystal growth additiveInfo
- Publication number
- CA2018155A1 CA2018155A1 CA002018155A CA2018155A CA2018155A1 CA 2018155 A1 CA2018155 A1 CA 2018155A1 CA 002018155 A CA002018155 A CA 002018155A CA 2018155 A CA2018155 A CA 2018155A CA 2018155 A1 CA2018155 A1 CA 2018155A1
- Authority
- CA
- Canada
- Prior art keywords
- alumina trihydrate
- bayer process
- ppm
- pregnant
- liquor
- 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.)
- Abandoned
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
- C01F7/14—Aluminium oxide or hydroxide from alkali metal aluminates
- C01F7/144—Aluminium oxide or hydroxide from alkali metal aluminates from aqueous aluminate solutions by precipitation due to cooling, e.g. as part of the Bayer process
- C01F7/145—Aluminium oxide or hydroxide from alkali metal aluminates from aqueous aluminate solutions by precipitation due to cooling, e.g. as part of the Bayer process characterised by the use of a crystal growth modifying agent other than aluminium hydroxide seed
Abstract
ABSTRACT
A method of modifying crystal structure of alumina trihydrate crystallizing from saturated Bayer liquors, which method includes the treatment of the saturated Bayer liquors with a crystal modifying amount of a polysaccharide, preferably a dextran.
A method of modifying crystal structure of alumina trihydrate crystallizing from saturated Bayer liquors, which method includes the treatment of the saturated Bayer liquors with a crystal modifying amount of a polysaccharide, preferably a dextran.
Description
2~1~1S5 I~TROD~CTION
This invention is concerned with treatment of Bayer process pregnant liquor, sometimes referred to as Bayer process green liquor, from which aluminum values are precipitated as alumina trihydrates.
In the Bayer process for bauxite ore beneficiation, crystallization and precipitation of solubilized alumina trihydrate values from causticized sodium aluminate liquors, referred to herein as Bayer process liquor, is a critical step toward the economic recovery of aluminum values. Bayer process operators optimize their precipitation method so as to produce the greatest possible yield from the Bayer process liquors, while trying to achieve a given crystal size or crystal size distribution. It is desirable in most instances to obtain relatively large crystal sizes since this is beneficial in subsequent processing steps required to produce alumina, alumina products, and/or aluminum metals. Production is often limited by processing conditions under which the crystallization and precipitation steps are conducted. These processing conditions vary from one plant to the next and include, but are not limited to, temperature profiles, seed charge, seed crystal surface area, liquor loading, liquor purity, and the like. My invention -~
appears to function to achieve increased average crystal size irrespective of the various processing conditions which may be ~r, present.
It is extremely well known that organic impurities in the Bayer process liquors, which impurities are normally derived from organics present in the bauxite ore or derived therefrom, can have devastating effects on Bayer process crystallization practises. These organics can include humate chemicals or umate-derived che=icals sucù as sodium oxalate and the like.
~1 ~ lS5 ,,, It would, therefore, be an advance in the art if technology could be developed to enhance the crystallization process even in the presence of humates, oxalates, and other impurities.
This has been accomplished with the instant invention. The instant invention involves th addition of certain additives prior to or simultaneously with the addition of seed crystals to ¦ enhance the production of alumina trihydrate precipitates from ¦ pregnant Bayer process liquors. The instant invention has been ¦ found to work even in the presence of certain impurities such as -~
¦ humates and oxalates, and the practise of the invention leads to ¦ the formation of higher particle size alumina trihydrate crystals. This phenomenon is observed irrespective of the ¦ operating plant criteria in regards to Bayer liquor quality, ¦ loading, purities, temperature of operation, time for recoverin~
¦ alumina trihydrate crystallites, seeding media and/or concentration and/or particle size, and the like. The instant ¦ invention also avoids the addition of insoluble hydrocarbons, an ¦ addition which is made in a commercially important technique j ¦ currently practised to achieve alumina trihydrate crystal growth in the Bayer process.
~, PRIOR PRAC~I5E~ -¦ A number of techniques have been demonstrated in the art and in prior publications and patents to achieve similar phenomenon ¦ achieved by the practise of the instant invention. For example, ¦ Owen et al., U.S. Patent 4,737,352, have demonstrated a method ¦ and composition for producing coarse alumina trihydrate crystal ¦ in the Bayer process pregnant liquor by adding thereto an oil in ¦ which is clissolved certain surfactants. This adds hydrocarbons ¦ to the precipitated alumina trihydrate.
201~3~5S
Roe et al., U.S. Patent 4,608,237, add polyacrylic acid having a molecular weight in excess of one million and containing at least fifty mole percent acrylic acid monomer to pregnant Bayer process liquors to control the negative effects of sodium i oxalate on the crystallization of alumina trihydrate from the Bayer process liquors. This technique is not commercially competitive with the Owen et al. process above.
Keeney, U.S. Patent 4,472,2~0, teaches a method of remo~ing certain anionic polymers and acidic organic impurities from aqueous trona solutions prior to the crystallization of tronas, thereby improving crystal formation of the trona solution. The preferred polymers Keeney uses in his trona crystallization process are nitrogen-containing cationic polymers and the purpose is to eliminate contaminants thought to be interfering with crystallization of trona. Of course, trona is not alumina trihydrate. Each of the patents above, U.S. Patent 4,737,352, U.S. Patent 4,608,237, and U.S. Patent 4,472,280, are incorporated herein by reference.
None of the above references teach or anticipate or make obvious the invention to be described below.
'' ~
TH~ INVENTION
I have discovered an improved method of producing an improved, large crystalline sized, alumina trihydrate crystal by crystallization from a hot, caustic pregnant Bayer process liquor, which improved alumina trihydrate crystals have a reduced content of crystallites having a crystal size below -325 mesh;
also reduced percentage of crystallites below 40 microns; and which improved method comprises treating the hot, caustic pregnant liquor, after red mud separation and after any final settling, centrifugation, or filtration step, if any such step is ' '' l .~
~` Z(~18155 employed to remove suspended red mud residues from the pregnant liquor, but prior to or simultaneously with the seeding of the pregnant caustic Bayer process liquors, with an effective crystal-modifying amount of a linear polysaccharide having a degree of branching less than five weight percent of the total weight of the polysaccharide added. My method is preferably practised with a linear polysaccharide having a weight average molecular weight r~nging between about 50,000 to about ;~
40,000,000, which linear polysaccharide is added to the pregnant `~
Bayer liquors in a concentration ranging between about 0.1 ppm to about 1000 ppm based on the total weight of the caustic pregnant Bayer process liquor being so treated. -~
-';`,,.-' TH~ LINEAR PO~Y8ACCHARIDE
The linear polysaccharide useful in my invention can be any linear polysaccharide which has a degree of branching less than about five weight percent of the total weight of the ~-polysaccharide. Preferably this polysaccharide is derived from ~
hydrolyzed starches or from polymerized anhydroglucose-based ~-units so that the polysaccharides have a weight average molecular weight ranging between about 50,000 to about 40,000,000.
Preferably the weight average molecular weight that is useful in my invention ranges between about 100,000 to about 35,000,000, and most preferably ranges between about 500,000 to about 25,000,000. However, the linear polysaccharides which are use~ul in the invention can have molecular weight below 500,000 or above 25,000,000.
Branching of the anhydroglucose units can occur when these units are obtained from certain starches or other natural products ancl the branching is primarily that achieved through a 1,3 branching location on the anhydroglucose unit. The primary `
~tructure of the anhydroglucose units and the polysaccharide polymers useful in this invention is given by Formula I.
FOR~ULA I
~ r~ r~ r~ r HO ~ HO ~ J HO ~ HO
OH OH OH OH
However, branching can exist, up to about five percent (-5%), and can be illustrated by the structures in Formula II below. ~:
FORMULA II
A primary source of the anhydroglucose polysaccharide units useful in this invention are from dextrans which have a :;-preponderance of ~ 1-6 linked anhydroglucose units ~sometimes ~:
referred to as anhydroglucopyranose units). As an example, the dextran products supplied by a company, Pharmachem, Inc., are ~-.
6 :::
~''' ~"
21~lB155 :!
useful in the instant invention. Pharmachem's products are derived from a native polymer produced by the bacterium ~-~euconostoc mesenteroides, strain NRRL B-512 F. This bacterium can be cultured on an industrial scale and used to induce the synthesis o~ an extra-cellular enzyme, dextransucrase, which in turn are mixed with sucrose sources and catalyse the transfer of the glucose moiety of the sucrose disaccharide raw material onto ~-a growing polysaccharide polymer chain. The dextrans produced in this manner have wide ranges of molecular weights.
Dextrans can also be produced by the roasting of corn or potato starches and/or by the hydrolysis of corn starches or other starch materials to produce various fractions having different molecular weight characteristics, different branching characteristics, and the like, which fractions may be recovered from the reaction media either by alcohol precipitation or by other techniques such as temperature gradient precipitation.
The polysaccharides most useful in the instant invention are those which are essentially linear and consist of approximately ~ -95 percent of ~ 1,6 linked glucopyranose units, but can include up to about five (S) percent ~ 1,3 linked glucopyranose monomer units. These side-chains are preferably usually no more than l -2 glucose units in length. However, dextrans or other polysaccharides having slightly higher branching or increased side-chain length can still be useful in the invention. At very high molecular weights and high degree of branching these materials may be water insoluble, though still swellable. ~:
The amount of dextrans or other polysaccharide materials added which effectively modifies crystal growth and crystal ;~
structure of the alumina trihydrates in the precipitation step of the Bayer process can be as little as 0.1 ppm, based on the total weight of the Bayer liquors being treated, and can be as high as -- 2~ SS
500 ~ 1000 ppm on the same basis. A preferred concentration range would be between about 0.5 ppm to about 200 ppm and a most preferred concentration range would be between about 1.0 ppm to about 50 ppm polysaccharide, based on the total weight of the Bayer liquor being treated. The polysaccharide can be added as a solution or a suspension, but is preferably added as a solution which contains at least 0.1 weight percent dissolved polysaccharide, preferably at least 0.5 weight percent dissolved v polysaccharides. The solutions or suspensions used are preferably water solutions, preferably having a pH ranging between about 4.oto about 12Ø The polysaccharide concentrations effective in modifying the crystals, which concentrations are listed above as from about 0.1 to about 1000 ppm, are based on active concentrations of what would be a solid, neat polysaccharide material, which material is preferably a dextran which may be added as a solution or suspension in neutral to basic pH water to the hot pregnant caustic Bayer liquors.
Best performance is observed when the polysaccharides are dissolved in the hot pregnant liquors prior to cooling and precipitation.
The molecular weights above are weight average molecular weights which may be obtained from light-scattering data. These molecular weights may also be verified by viscosity measurements of the dextran solutions.
Dextran solutions have been used in the Bayer liquor process in the past. However, their use has been primarily as a flocculant aid such as in red mud settling and as a flocculant ~;
for alumina trihydrate after seeding and cooling of pregnant liquor and after alumina trihydrate crystallization. However, the instant invention has never been anticipated or taught in the prior use of dextrans as floccula~ion aids. Prior use of ZOlB155 dextrans in the crystallization step have been to add the dextran materials after the seeding and crystallization step has begun and either nearly completed or totally completed. The dextrans in this flocculation use act merely as a flocc~lant, or ~
flocculating agent, to separate and increase the rate o~ - .
separation of the formed alumina trihydrate crystals from the :.-spent Bayer liquor process. Use in this manner has no real affect on crystal size and does not show crystal modification as ~:
does the use of dextrans in the method of this invention.
To demonstrate my invention the following examples are provided:
.:' 2XAMPLE~ :~:
Synthetic green liquor, (also referred to as pregnant Bayer ~liquors) saturated with alumina trihydrate values, is prepared in the laboratory by dissolving alumina trihydrate in hot caustic.
Preferably the tempexature of the hot caustic is between about :~
110 C. to about 120 C., with a preferred temperature ranging between about 112 C. to about 117 C~ Our tests were performed at 115 C. After the alumina trihydrate is dissolved to a level .
equal to its saturation value at this temperature, any reagents `
to be tested and mixed into the solution are added and dissolved therein. ~ .
After the addition of the test reagents, an alumina trihydrate ~eed obtained from an operating Bayer process plant, is added in appropriate quantities and the resulting slurry is :
agitated ancl cooled to a temperature of about 65 C. in a period of approximately sixteen (16) to eighteen (18) hours, thereby precipitating the alumina trihydrate from the pregnant synthetic :~
green liqu~r. Particle size distribution is determined on the Z01~1 55 precipitate recovered to determine the coarsening effect caused by the test reagents of this invention.
Table I and Graph I show that the addition of the linear polysaccharides of this invention in the precipitation stage, prior to seeding the pregnant synthetic green liquors, lowers the percent of alumina trihydrate precipitate having a particle size less than -325 mesh, corresponding to approximately a particle size less than 40 microns, relative to a blank precipitate obtained from the same synthetic green liquor absent any crystal modi~ying treatment. Also, the data presented demonstrates the fact that the linear polysaccharides, that is the dextrans, which are used in these experiments, provides an improved result over the results of an oil/surfactant formulation which would be covered by the claims of Owen et al., U.S. 4,737,352.
In a second set of experiments, 500 ppm of a sodium humate was added to the synthetic green pregnant liquor prior to the addition of the crystal-modifying linear polysaccharide reagents of this invention. This was an attempt to simulate process conditions where bauxlte ores are digested which ores contain organic matter producing these kinds of humate impurities during the digestion step of the Bayer process. Table II and Graph II
demonstrate the results obtained and again show that the addition of the linear polysaccharides of this invention give a coarser precipitate than that obtained with either no treatment or treatment with a product which would be covered by the Owen et al. patent, U.S. 4,737,352, which has been incorporated herein by reference. `
Table ]:II gives results obtained from a test run on an actual Bayer process plant pregnant green liquor. Once again, even in the presence of the naturally occurring impurities whlch included not only humate, but also oxalate salts, the dextran 2(; 1~3~5S
. ..
used according to the instant invention obtained a coarser ~ ; :
alumina trihydrate precipitate than available with no treatment.
. ~
The improved alumina trihydrate crystals recovered from the precipitation step can have.an average crystal size at least one percent higher than the crystal size obtained in . :~.
the absence of dextran.
.~ ' .; ' ' ~:: . :, : - , .. ~ ~,. .: :.: .
,- ,~, ~:-:::: :;: ..;
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., -~,~ `,' "'...'.
: ~ - :. ::
~::: :. . ~
~: :: ' ' :: ~: :, .:
.:; ~ . .. .
'''"''', ''~ `' .
Z~1~15ti ~,,.
~:
TA~B ~
EVALUATION OF DExTnAN IN ALUMINA PRECIPITATION
% PRECIPITATE LESS T~AN A GIVEN PARTICLE SIZE
NO HUMATE ADDED
....
OIL/ OIL/
SIZE BLAN~ DEXT~AN DEXT~N DEXTR~N SURFACTANT SURFACTANT
1 ppm)~5 ppm)~20 ppm)~20 ppm)(50 ppm) 300.0100.0100.0100.0 100.0 100.0 100.0 : 212.0100.0100.0100.0 100.0 100.0 100.0 150.0100.0100.098.2 99.7 100.0 100.0 :
106.096.587.9 79.0 77.7 85.5 82.2 75.0 76.963.2 52.4 48.8 55.6 52.3 53.0 43.033.5 24.0 23.2 29.1 27.2 ~:.
38.0 23.618.5 15.6 13.2 17.7 17.6 ~: 27.0 18.413.9 13.7 11.6 15.6 16.3 ~
19.0 17.313.2 13.2 10.~ 14.7 14.6 -.
13.0 15.110.4 11.9 8.6 13.1 13.3 :
9.4 10.0 7.8 8.9 6.9 10.3 11.0 6.6 6.1 4.6 5.3 3.9 6.0 6.5 4.7 2.7 1.4 2.1 1.5 2.5 2.6 :~ ,'~
'~'~
~ ~ ~s taught Owen et al., U.S. Patent 4,737,352 ~ ~
: ~ . :
~, , ' ''``'.''.'' '''"~
~, 201t3155 , . TA~B~II
EVALUA$ION OF DEXTRAN IN ALUMINA PRECIPITATION
% PRECIPITAT2 LESS THAN A GIVEN PARTIC~E SIZE
.' SIZE BLANX DEXTRANDEXTRANSURFACTANT SURFACTANT
~) (5 ppm~~20 ppm) (20 ppm) (50 ppm) ;
. 300.0 100.0 100.0100.0 100.0 100.0 212.0 100.0 100.0100.0 100.0 100.0 150.0 100.0 100.099.9 100.0 loo.0 106.0 99.8 91.1 ~6.4 95.1 93.8 ..
75.0 88.1 68.7 61.8 79.9 75.8 ..
53.0 60.6 36.1 27.9 49.3 43.7 38.0 33.7 16.9 10.2 25.2 20.6 .. :
27.0 16.6 9.5 5.4 13.6 12.
19.0 ll.9 8.0 3.9 10.1 9.9 .
13.0 9.5 6.2 2.6 8.4 7.9 9.4 6.4 4.0 1.1 5.9 5.4 .~
~ 6.6 3.5 2.2 0.6 3.2 2.7 :~.`
: 4.7 1.0 0.4 0.2 0.9 0.7 .. ~
~;
. -~ As taught owen et al ., U. S. Patent 4, 737, 352 ~ ~
~:~ .
~ ~
~
''''' .'~
:
,~
2~ 31SS
TA}3~æ I I X
EVALUATION OP DEXTRAN IN ALUMINA PRECIPITATION
IN PLANT LIQUOR
.
Dose Precipitate Size Product fppm) f% less than 106 ~) Blank - 55 --Oil/Surfactant 50 48 . .
Dextran 5 49 . ~ ''"' ~ ~ As taught Owen et al., U.s. Patent 4,737,352 . , : ,'' ,;
~' .
''"' 201~1155 TEIE FIGUR~S
The figures I and II demonstrate the improved overall effect of dextrans relative to both measured particle size and number of particles (or crystals) having a particular size. Figure I is a ~:
humate free experiment, while Figure II is purposely contaminated with humate. ;
The dextrans used in the! above experiments are materials identified as C-2P, manufactured by Pharmachem Corporation, and having a weight average molecular weight ranging between about :~
5,000,000 to about 40,000,000. These dextrans are manufactured ~`.
by the procedures listed above using bacterial strains and raw ~:
sucrose, although other dextrans having the characteristics :~
described above are also expected to function as crystal :~
modifiers and crystal size enhancers. ~
It is important to the practise of this invention that the ~ ~:
improved method of producing the improved and coarser alumina trihydrate crystals from the alumina trihydrate precipitation step of any Bayer process, which process is operated to produce :~
alumina trihydrate crystals from bauxite ores, include a method that comprises treating hot caustic pregnant Bayer process liquors after red mud separation and any final liquid-solid separation or other removal or polishing step designed to remove very small particle red mud materials, for example the use of specially designed filters to remove very finely suspended iron oxide particles from pregnant Bayer liquors prior to the ~
precipitation step, and prior to or simultaneously with the - :
seeding of 1:hese pregnant liquors.
However, it is feasible that, if filters are used prior to crystalliza1:ion, a working and effective crystal modifying amount of dextrans could be supplied to the crystallizers by overdosing prior to filtration and allowing the amount of overdosed dextrans Z/~lB155 to pass through thP filters to provide crystal modifying effects.
This would be an alternative means of practising my invention, but is not a preferred means.
The preferred instant process involves the addition of effective crystal-modifying and crystal size increasing amounts -~
of linear polysaccharides, preferably linear dextrans having a weight average molecular weight ranging between about 500,000 to about 40,000,000, most preferably between 5,000,000 to 40,000,000. The addition of our dextrans is preferred to be after red mud separation and final red mud residue removal steps, if any, but prior to or simultaneous with the addition of the alumina trihydrate seeds, or any other seeding materials, which -;~
seed crystals are used for the purpose of beginning the crystallization of alumina trihydrate from pregnant or green Bayer process liquors as these liquors are cooled. The normal process involves, after seeding, the cooling of the green or pregnant Bayer process liquors from temperatures of approximately 115 C., + 10 C., to temperatures of approximately 65~ C., + 5 C. (or below, some processors go as low as 50 C.), and collecting the precipitated alumina trihydrates on precipitation trays. Although, as taught above, dextrans have been used to enhance the flocculation of alumina trihydrate precipitates, their previous use involved the addition after the seeding, cooling, and crystallization step and did not obtain crystal modification as in the instant process. Therefore, no effect on ultimate crystal size was observed by their use. I have discovered that by modifying the location and the amount of dextrans used in this crystallization step and, most preferably, by adding the dextrans to the hot pregnant liquors immediately before seed:ing or simultaneously with the addition of the seed, but after final filtration and removal of all red mud materials, 7~0~t~155 .
I can effect, in a positive way, the crystal size and shape of :~.
the alumina trihydrate recovered from the Bayer process. The effective amount of these preferred dextrans used in the process described above, including that process which adds dextrans to hot caustic pregnant Bayer process liquors after the red mud separation step, but prior to or simultaneously with the seeding :~
of the hot pregnant liquors, ranges between approximately 0.1 ppm ~
to about 1000 ppm, and is preferably between about 0.5 ppm ~nd ~:
about 500 ppm, and most preferably from 1 to about 100 ppm dextran based on a total weight of Bayer process liquor. -Havin escribed my invention I claim:
~;
This invention is concerned with treatment of Bayer process pregnant liquor, sometimes referred to as Bayer process green liquor, from which aluminum values are precipitated as alumina trihydrates.
In the Bayer process for bauxite ore beneficiation, crystallization and precipitation of solubilized alumina trihydrate values from causticized sodium aluminate liquors, referred to herein as Bayer process liquor, is a critical step toward the economic recovery of aluminum values. Bayer process operators optimize their precipitation method so as to produce the greatest possible yield from the Bayer process liquors, while trying to achieve a given crystal size or crystal size distribution. It is desirable in most instances to obtain relatively large crystal sizes since this is beneficial in subsequent processing steps required to produce alumina, alumina products, and/or aluminum metals. Production is often limited by processing conditions under which the crystallization and precipitation steps are conducted. These processing conditions vary from one plant to the next and include, but are not limited to, temperature profiles, seed charge, seed crystal surface area, liquor loading, liquor purity, and the like. My invention -~
appears to function to achieve increased average crystal size irrespective of the various processing conditions which may be ~r, present.
It is extremely well known that organic impurities in the Bayer process liquors, which impurities are normally derived from organics present in the bauxite ore or derived therefrom, can have devastating effects on Bayer process crystallization practises. These organics can include humate chemicals or umate-derived che=icals sucù as sodium oxalate and the like.
~1 ~ lS5 ,,, It would, therefore, be an advance in the art if technology could be developed to enhance the crystallization process even in the presence of humates, oxalates, and other impurities.
This has been accomplished with the instant invention. The instant invention involves th addition of certain additives prior to or simultaneously with the addition of seed crystals to ¦ enhance the production of alumina trihydrate precipitates from ¦ pregnant Bayer process liquors. The instant invention has been ¦ found to work even in the presence of certain impurities such as -~
¦ humates and oxalates, and the practise of the invention leads to ¦ the formation of higher particle size alumina trihydrate crystals. This phenomenon is observed irrespective of the ¦ operating plant criteria in regards to Bayer liquor quality, ¦ loading, purities, temperature of operation, time for recoverin~
¦ alumina trihydrate crystallites, seeding media and/or concentration and/or particle size, and the like. The instant ¦ invention also avoids the addition of insoluble hydrocarbons, an ¦ addition which is made in a commercially important technique j ¦ currently practised to achieve alumina trihydrate crystal growth in the Bayer process.
~, PRIOR PRAC~I5E~ -¦ A number of techniques have been demonstrated in the art and in prior publications and patents to achieve similar phenomenon ¦ achieved by the practise of the instant invention. For example, ¦ Owen et al., U.S. Patent 4,737,352, have demonstrated a method ¦ and composition for producing coarse alumina trihydrate crystal ¦ in the Bayer process pregnant liquor by adding thereto an oil in ¦ which is clissolved certain surfactants. This adds hydrocarbons ¦ to the precipitated alumina trihydrate.
201~3~5S
Roe et al., U.S. Patent 4,608,237, add polyacrylic acid having a molecular weight in excess of one million and containing at least fifty mole percent acrylic acid monomer to pregnant Bayer process liquors to control the negative effects of sodium i oxalate on the crystallization of alumina trihydrate from the Bayer process liquors. This technique is not commercially competitive with the Owen et al. process above.
Keeney, U.S. Patent 4,472,2~0, teaches a method of remo~ing certain anionic polymers and acidic organic impurities from aqueous trona solutions prior to the crystallization of tronas, thereby improving crystal formation of the trona solution. The preferred polymers Keeney uses in his trona crystallization process are nitrogen-containing cationic polymers and the purpose is to eliminate contaminants thought to be interfering with crystallization of trona. Of course, trona is not alumina trihydrate. Each of the patents above, U.S. Patent 4,737,352, U.S. Patent 4,608,237, and U.S. Patent 4,472,280, are incorporated herein by reference.
None of the above references teach or anticipate or make obvious the invention to be described below.
'' ~
TH~ INVENTION
I have discovered an improved method of producing an improved, large crystalline sized, alumina trihydrate crystal by crystallization from a hot, caustic pregnant Bayer process liquor, which improved alumina trihydrate crystals have a reduced content of crystallites having a crystal size below -325 mesh;
also reduced percentage of crystallites below 40 microns; and which improved method comprises treating the hot, caustic pregnant liquor, after red mud separation and after any final settling, centrifugation, or filtration step, if any such step is ' '' l .~
~` Z(~18155 employed to remove suspended red mud residues from the pregnant liquor, but prior to or simultaneously with the seeding of the pregnant caustic Bayer process liquors, with an effective crystal-modifying amount of a linear polysaccharide having a degree of branching less than five weight percent of the total weight of the polysaccharide added. My method is preferably practised with a linear polysaccharide having a weight average molecular weight r~nging between about 50,000 to about ;~
40,000,000, which linear polysaccharide is added to the pregnant `~
Bayer liquors in a concentration ranging between about 0.1 ppm to about 1000 ppm based on the total weight of the caustic pregnant Bayer process liquor being so treated. -~
-';`,,.-' TH~ LINEAR PO~Y8ACCHARIDE
The linear polysaccharide useful in my invention can be any linear polysaccharide which has a degree of branching less than about five weight percent of the total weight of the ~-polysaccharide. Preferably this polysaccharide is derived from ~
hydrolyzed starches or from polymerized anhydroglucose-based ~-units so that the polysaccharides have a weight average molecular weight ranging between about 50,000 to about 40,000,000.
Preferably the weight average molecular weight that is useful in my invention ranges between about 100,000 to about 35,000,000, and most preferably ranges between about 500,000 to about 25,000,000. However, the linear polysaccharides which are use~ul in the invention can have molecular weight below 500,000 or above 25,000,000.
Branching of the anhydroglucose units can occur when these units are obtained from certain starches or other natural products ancl the branching is primarily that achieved through a 1,3 branching location on the anhydroglucose unit. The primary `
~tructure of the anhydroglucose units and the polysaccharide polymers useful in this invention is given by Formula I.
FOR~ULA I
~ r~ r~ r~ r HO ~ HO ~ J HO ~ HO
OH OH OH OH
However, branching can exist, up to about five percent (-5%), and can be illustrated by the structures in Formula II below. ~:
FORMULA II
A primary source of the anhydroglucose polysaccharide units useful in this invention are from dextrans which have a :;-preponderance of ~ 1-6 linked anhydroglucose units ~sometimes ~:
referred to as anhydroglucopyranose units). As an example, the dextran products supplied by a company, Pharmachem, Inc., are ~-.
6 :::
~''' ~"
21~lB155 :!
useful in the instant invention. Pharmachem's products are derived from a native polymer produced by the bacterium ~-~euconostoc mesenteroides, strain NRRL B-512 F. This bacterium can be cultured on an industrial scale and used to induce the synthesis o~ an extra-cellular enzyme, dextransucrase, which in turn are mixed with sucrose sources and catalyse the transfer of the glucose moiety of the sucrose disaccharide raw material onto ~-a growing polysaccharide polymer chain. The dextrans produced in this manner have wide ranges of molecular weights.
Dextrans can also be produced by the roasting of corn or potato starches and/or by the hydrolysis of corn starches or other starch materials to produce various fractions having different molecular weight characteristics, different branching characteristics, and the like, which fractions may be recovered from the reaction media either by alcohol precipitation or by other techniques such as temperature gradient precipitation.
The polysaccharides most useful in the instant invention are those which are essentially linear and consist of approximately ~ -95 percent of ~ 1,6 linked glucopyranose units, but can include up to about five (S) percent ~ 1,3 linked glucopyranose monomer units. These side-chains are preferably usually no more than l -2 glucose units in length. However, dextrans or other polysaccharides having slightly higher branching or increased side-chain length can still be useful in the invention. At very high molecular weights and high degree of branching these materials may be water insoluble, though still swellable. ~:
The amount of dextrans or other polysaccharide materials added which effectively modifies crystal growth and crystal ;~
structure of the alumina trihydrates in the precipitation step of the Bayer process can be as little as 0.1 ppm, based on the total weight of the Bayer liquors being treated, and can be as high as -- 2~ SS
500 ~ 1000 ppm on the same basis. A preferred concentration range would be between about 0.5 ppm to about 200 ppm and a most preferred concentration range would be between about 1.0 ppm to about 50 ppm polysaccharide, based on the total weight of the Bayer liquor being treated. The polysaccharide can be added as a solution or a suspension, but is preferably added as a solution which contains at least 0.1 weight percent dissolved polysaccharide, preferably at least 0.5 weight percent dissolved v polysaccharides. The solutions or suspensions used are preferably water solutions, preferably having a pH ranging between about 4.oto about 12Ø The polysaccharide concentrations effective in modifying the crystals, which concentrations are listed above as from about 0.1 to about 1000 ppm, are based on active concentrations of what would be a solid, neat polysaccharide material, which material is preferably a dextran which may be added as a solution or suspension in neutral to basic pH water to the hot pregnant caustic Bayer liquors.
Best performance is observed when the polysaccharides are dissolved in the hot pregnant liquors prior to cooling and precipitation.
The molecular weights above are weight average molecular weights which may be obtained from light-scattering data. These molecular weights may also be verified by viscosity measurements of the dextran solutions.
Dextran solutions have been used in the Bayer liquor process in the past. However, their use has been primarily as a flocculant aid such as in red mud settling and as a flocculant ~;
for alumina trihydrate after seeding and cooling of pregnant liquor and after alumina trihydrate crystallization. However, the instant invention has never been anticipated or taught in the prior use of dextrans as floccula~ion aids. Prior use of ZOlB155 dextrans in the crystallization step have been to add the dextran materials after the seeding and crystallization step has begun and either nearly completed or totally completed. The dextrans in this flocculation use act merely as a flocc~lant, or ~
flocculating agent, to separate and increase the rate o~ - .
separation of the formed alumina trihydrate crystals from the :.-spent Bayer liquor process. Use in this manner has no real affect on crystal size and does not show crystal modification as ~:
does the use of dextrans in the method of this invention.
To demonstrate my invention the following examples are provided:
.:' 2XAMPLE~ :~:
Synthetic green liquor, (also referred to as pregnant Bayer ~liquors) saturated with alumina trihydrate values, is prepared in the laboratory by dissolving alumina trihydrate in hot caustic.
Preferably the tempexature of the hot caustic is between about :~
110 C. to about 120 C., with a preferred temperature ranging between about 112 C. to about 117 C~ Our tests were performed at 115 C. After the alumina trihydrate is dissolved to a level .
equal to its saturation value at this temperature, any reagents `
to be tested and mixed into the solution are added and dissolved therein. ~ .
After the addition of the test reagents, an alumina trihydrate ~eed obtained from an operating Bayer process plant, is added in appropriate quantities and the resulting slurry is :
agitated ancl cooled to a temperature of about 65 C. in a period of approximately sixteen (16) to eighteen (18) hours, thereby precipitating the alumina trihydrate from the pregnant synthetic :~
green liqu~r. Particle size distribution is determined on the Z01~1 55 precipitate recovered to determine the coarsening effect caused by the test reagents of this invention.
Table I and Graph I show that the addition of the linear polysaccharides of this invention in the precipitation stage, prior to seeding the pregnant synthetic green liquors, lowers the percent of alumina trihydrate precipitate having a particle size less than -325 mesh, corresponding to approximately a particle size less than 40 microns, relative to a blank precipitate obtained from the same synthetic green liquor absent any crystal modi~ying treatment. Also, the data presented demonstrates the fact that the linear polysaccharides, that is the dextrans, which are used in these experiments, provides an improved result over the results of an oil/surfactant formulation which would be covered by the claims of Owen et al., U.S. 4,737,352.
In a second set of experiments, 500 ppm of a sodium humate was added to the synthetic green pregnant liquor prior to the addition of the crystal-modifying linear polysaccharide reagents of this invention. This was an attempt to simulate process conditions where bauxlte ores are digested which ores contain organic matter producing these kinds of humate impurities during the digestion step of the Bayer process. Table II and Graph II
demonstrate the results obtained and again show that the addition of the linear polysaccharides of this invention give a coarser precipitate than that obtained with either no treatment or treatment with a product which would be covered by the Owen et al. patent, U.S. 4,737,352, which has been incorporated herein by reference. `
Table ]:II gives results obtained from a test run on an actual Bayer process plant pregnant green liquor. Once again, even in the presence of the naturally occurring impurities whlch included not only humate, but also oxalate salts, the dextran 2(; 1~3~5S
. ..
used according to the instant invention obtained a coarser ~ ; :
alumina trihydrate precipitate than available with no treatment.
. ~
The improved alumina trihydrate crystals recovered from the precipitation step can have.an average crystal size at least one percent higher than the crystal size obtained in . :~.
the absence of dextran.
.~ ' .; ' ' ~:: . :, : - , .. ~ ~,. .: :.: .
,- ,~, ~:-:::: :;: ..;
:. . ' ' :. .: :., ..~ . .; .
., -~,~ `,' "'...'.
: ~ - :. ::
~::: :. . ~
~: :: ' ' :: ~: :, .:
.:; ~ . .. .
'''"''', ''~ `' .
Z~1~15ti ~,,.
~:
TA~B ~
EVALUATION OF DExTnAN IN ALUMINA PRECIPITATION
% PRECIPITATE LESS T~AN A GIVEN PARTICLE SIZE
NO HUMATE ADDED
....
OIL/ OIL/
SIZE BLAN~ DEXT~AN DEXT~N DEXTR~N SURFACTANT SURFACTANT
1 ppm)~5 ppm)~20 ppm)~20 ppm)(50 ppm) 300.0100.0100.0100.0 100.0 100.0 100.0 : 212.0100.0100.0100.0 100.0 100.0 100.0 150.0100.0100.098.2 99.7 100.0 100.0 :
106.096.587.9 79.0 77.7 85.5 82.2 75.0 76.963.2 52.4 48.8 55.6 52.3 53.0 43.033.5 24.0 23.2 29.1 27.2 ~:.
38.0 23.618.5 15.6 13.2 17.7 17.6 ~: 27.0 18.413.9 13.7 11.6 15.6 16.3 ~
19.0 17.313.2 13.2 10.~ 14.7 14.6 -.
13.0 15.110.4 11.9 8.6 13.1 13.3 :
9.4 10.0 7.8 8.9 6.9 10.3 11.0 6.6 6.1 4.6 5.3 3.9 6.0 6.5 4.7 2.7 1.4 2.1 1.5 2.5 2.6 :~ ,'~
'~'~
~ ~ ~s taught Owen et al., U.S. Patent 4,737,352 ~ ~
: ~ . :
~, , ' ''``'.''.'' '''"~
~, 201t3155 , . TA~B~II
EVALUA$ION OF DEXTRAN IN ALUMINA PRECIPITATION
% PRECIPITAT2 LESS THAN A GIVEN PARTIC~E SIZE
.' SIZE BLANX DEXTRANDEXTRANSURFACTANT SURFACTANT
~) (5 ppm~~20 ppm) (20 ppm) (50 ppm) ;
. 300.0 100.0 100.0100.0 100.0 100.0 212.0 100.0 100.0100.0 100.0 100.0 150.0 100.0 100.099.9 100.0 loo.0 106.0 99.8 91.1 ~6.4 95.1 93.8 ..
75.0 88.1 68.7 61.8 79.9 75.8 ..
53.0 60.6 36.1 27.9 49.3 43.7 38.0 33.7 16.9 10.2 25.2 20.6 .. :
27.0 16.6 9.5 5.4 13.6 12.
19.0 ll.9 8.0 3.9 10.1 9.9 .
13.0 9.5 6.2 2.6 8.4 7.9 9.4 6.4 4.0 1.1 5.9 5.4 .~
~ 6.6 3.5 2.2 0.6 3.2 2.7 :~.`
: 4.7 1.0 0.4 0.2 0.9 0.7 .. ~
~;
. -~ As taught owen et al ., U. S. Patent 4, 737, 352 ~ ~
~:~ .
~ ~
~
''''' .'~
:
,~
2~ 31SS
TA}3~æ I I X
EVALUATION OP DEXTRAN IN ALUMINA PRECIPITATION
IN PLANT LIQUOR
.
Dose Precipitate Size Product fppm) f% less than 106 ~) Blank - 55 --Oil/Surfactant 50 48 . .
Dextran 5 49 . ~ ''"' ~ ~ As taught Owen et al., U.s. Patent 4,737,352 . , : ,'' ,;
~' .
''"' 201~1155 TEIE FIGUR~S
The figures I and II demonstrate the improved overall effect of dextrans relative to both measured particle size and number of particles (or crystals) having a particular size. Figure I is a ~:
humate free experiment, while Figure II is purposely contaminated with humate. ;
The dextrans used in the! above experiments are materials identified as C-2P, manufactured by Pharmachem Corporation, and having a weight average molecular weight ranging between about :~
5,000,000 to about 40,000,000. These dextrans are manufactured ~`.
by the procedures listed above using bacterial strains and raw ~:
sucrose, although other dextrans having the characteristics :~
described above are also expected to function as crystal :~
modifiers and crystal size enhancers. ~
It is important to the practise of this invention that the ~ ~:
improved method of producing the improved and coarser alumina trihydrate crystals from the alumina trihydrate precipitation step of any Bayer process, which process is operated to produce :~
alumina trihydrate crystals from bauxite ores, include a method that comprises treating hot caustic pregnant Bayer process liquors after red mud separation and any final liquid-solid separation or other removal or polishing step designed to remove very small particle red mud materials, for example the use of specially designed filters to remove very finely suspended iron oxide particles from pregnant Bayer liquors prior to the ~
precipitation step, and prior to or simultaneously with the - :
seeding of 1:hese pregnant liquors.
However, it is feasible that, if filters are used prior to crystalliza1:ion, a working and effective crystal modifying amount of dextrans could be supplied to the crystallizers by overdosing prior to filtration and allowing the amount of overdosed dextrans Z/~lB155 to pass through thP filters to provide crystal modifying effects.
This would be an alternative means of practising my invention, but is not a preferred means.
The preferred instant process involves the addition of effective crystal-modifying and crystal size increasing amounts -~
of linear polysaccharides, preferably linear dextrans having a weight average molecular weight ranging between about 500,000 to about 40,000,000, most preferably between 5,000,000 to 40,000,000. The addition of our dextrans is preferred to be after red mud separation and final red mud residue removal steps, if any, but prior to or simultaneous with the addition of the alumina trihydrate seeds, or any other seeding materials, which -;~
seed crystals are used for the purpose of beginning the crystallization of alumina trihydrate from pregnant or green Bayer process liquors as these liquors are cooled. The normal process involves, after seeding, the cooling of the green or pregnant Bayer process liquors from temperatures of approximately 115 C., + 10 C., to temperatures of approximately 65~ C., + 5 C. (or below, some processors go as low as 50 C.), and collecting the precipitated alumina trihydrates on precipitation trays. Although, as taught above, dextrans have been used to enhance the flocculation of alumina trihydrate precipitates, their previous use involved the addition after the seeding, cooling, and crystallization step and did not obtain crystal modification as in the instant process. Therefore, no effect on ultimate crystal size was observed by their use. I have discovered that by modifying the location and the amount of dextrans used in this crystallization step and, most preferably, by adding the dextrans to the hot pregnant liquors immediately before seed:ing or simultaneously with the addition of the seed, but after final filtration and removal of all red mud materials, 7~0~t~155 .
I can effect, in a positive way, the crystal size and shape of :~.
the alumina trihydrate recovered from the Bayer process. The effective amount of these preferred dextrans used in the process described above, including that process which adds dextrans to hot caustic pregnant Bayer process liquors after the red mud separation step, but prior to or simultaneously with the seeding :~
of the hot pregnant liquors, ranges between approximately 0.1 ppm ~
to about 1000 ppm, and is preferably between about 0.5 ppm ~nd ~:
about 500 ppm, and most preferably from 1 to about 100 ppm dextran based on a total weight of Bayer process liquor. -Havin escribed my invention I claim:
~;
Claims (7)
- Claim 1. An improved method of producing improved alumina trihydrate crystals by crystallization from a hot, caustic pregnant Bayer process liquor, which improved alumina trihydrate crystals have a reduced content of crystallites having a crystal size below -325 mesh, which method comprises treating the hot caustic pregnant Bayer process liquor, after red mud separation, and after any final solid-liquid separation step which removes suspended red mud residues, but prior to crystallization of alumina trihydrate, with an effective crystal modifying amount of a linear polysaccharide having a degree of branching less than five weight percent of the total weight of the polysaccharide.
- Claim 2. The method of Claim 1 wherein the linear polysaccharide has a weight average molecular weight ranging between about 50,000 to about 40,000,000.
- Claim 3. The method of Claim 1 or Claim 2 wherein the effective crystal modifying amount of polysaccharide ranges between about 0.1 ppm to about 1000 ppm, based on the total weight of the caustic Bayer process liquor.
- Claim 4. An improved method of producing improved alumina trihydrate crystals in the alumina trihydrate precipitation step of a Bayer process operating to produce alumina trihydrate crystals from bauxite ores, which method comprises treating caustic pregnant Bayer process liquor; after red mud separation, but prior to, or simultaneously with, seeding the pregnant liquors; with an effective crystal modifying amount of dextran having a weight average molecular weight ranging between about 50,000 to about 40,000,000.
- Claim 5. The method of Claim 4 wherein the dextran is added to the pregnant Bayer process liquor at a concentration ranging between about 0.1 ppm to about 500 ppm, based on the total weight of liquor.
- Claim 6. The method of Claim 4 or Claim 5 wherein the improved alumina trihydrate crystals recovered from the precipitation step have an average crystal size at least one percent higher than the crystal size obtained in the absence of dextran.
- Claim 7. The method of Claim 4 or Claim 5 wherein the improved alumina trihydrate crystals are recovered from a humate contaminated green Bayer Process liquor.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US475,622 | 1990-02-06 | ||
| US07/475,622 US5106599A (en) | 1990-02-06 | 1990-02-06 | Alumina crystal growth additive |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2018155A1 true CA2018155A1 (en) | 1991-08-06 |
Family
ID=23888404
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002018155A Abandoned CA2018155A1 (en) | 1990-02-06 | 1990-06-04 | Alumina crystal growth additive |
Country Status (3)
| Country | Link |
|---|---|
| US (1) | US5106599A (en) |
| AU (1) | AU633181B2 (en) |
| CA (1) | CA2018155A1 (en) |
Families Citing this family (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE4039053A1 (en) * | 1990-12-07 | 1992-06-11 | Henkel Kgaa | POLYGLYCERINE IN THE BAYER PROCESS |
| DE69308777T2 (en) * | 1992-12-14 | 1997-07-31 | Nalco Chemical Co | Change of trihydrate crystals in the Bayer process |
| US6293973B1 (en) | 1996-10-11 | 2001-09-25 | Nalco Chemical Company | Method of controlling oxalate precipitation in bayer process liquor |
| US8971913B2 (en) * | 2003-06-27 | 2015-03-03 | Qualcomm Incorporated | Method and apparatus for wireless network hybrid positioning |
| US7976820B2 (en) * | 2005-06-23 | 2011-07-12 | Nalco Company | Composition and method for improved aluminum hydroxide production |
| US9284625B2 (en) * | 2007-11-20 | 2016-03-15 | Nalco Company | Use of polyols as scale control reagents in the mining processes |
| US8282689B2 (en) | 2009-07-01 | 2012-10-09 | Nalco Company | Composition and method for enhancing the production of crystal agglomerates from a precipitation liquor |
| US8252266B2 (en) | 2010-08-09 | 2012-08-28 | Nalco Company | Recovery of alumina trihydrate during the bayer process using scleroglucan |
| US9102995B2 (en) | 2010-08-09 | 2015-08-11 | Nalco Company | Cross-linked ethylsulfonated dihydroxypropyl cellulose |
| US8298508B2 (en) | 2010-08-09 | 2012-10-30 | Nalco Company | Recovery of alumina trihydrate during the bayer process using cross-linked polysaccharides |
| US9199855B2 (en) | 2010-08-09 | 2015-12-01 | Nalco Company | Chemical treatment to improve red mud separation and washing in the bayer process |
| US9187337B2 (en) | 2010-09-06 | 2015-11-17 | Alcoa Of Australia Limited | Method of increasing the stability of a Bayer process liquor |
| US8920768B2 (en) | 2013-03-14 | 2014-12-30 | Ecolab Usa Inc. | Crystallization aids for bayer aluminum hydroxide |
| US9592456B2 (en) | 2015-02-11 | 2017-03-14 | Ecolab Usa Inc. | Methods for enhancing production of aluminum hydroxide in an aluminum hydroxide production process |
| US10427950B2 (en) | 2015-12-04 | 2019-10-01 | Ecolab Usa Inc. | Recovery of mining processing product using boronic acid-containing polymers |
| US10259721B2 (en) * | 2016-09-09 | 2019-04-16 | Cytec Industries Inc. | Oil free crystal growth modifiers for the bayer process |
| AU2018339457B2 (en) | 2017-09-26 | 2023-11-09 | Ecolab Usa Inc. | Methods and compositions for bauxite beneficiation |
| CN112299461B (en) * | 2020-11-08 | 2023-03-24 | 湖南诺兰蒂尔环保科技有限公司 | Device and process for removing oxalate in sodium aluminate solution |
Family Cites Families (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2734796A (en) * | 1956-02-14 | Composition comprising stable solid sodium aluminate | ||
| US2345139A (en) * | 1942-06-13 | 1944-03-28 | Martin Archworth | Geneva drive |
| US3085853A (en) * | 1958-12-23 | 1963-04-16 | Dow Chemical Co | Method of employing dextrans |
| US3142637A (en) * | 1961-01-31 | 1964-07-28 | Reynolds Metals Co | Flocculating agent and process for digested bauxite slurries |
| US3197289A (en) * | 1961-12-11 | 1965-07-27 | Nopco Chem Co | Modification of zinc hydrosulfite crystals by use of high molecular weight colloidal materials |
| US3390959A (en) * | 1965-04-30 | 1968-07-02 | Nalco Chemical Co | Process of making alumina |
| US3445187A (en) * | 1966-05-25 | 1969-05-20 | Nalco Chemical Co | Process for separation of red mud from dissolved alumina |
| GB1350389A (en) * | 1970-08-26 | 1974-04-18 | Atomic Energy Authority Uk | Processes for precipitating metal compounds |
| US3937748A (en) * | 1973-06-01 | 1976-02-10 | Petro-Tex Chemical Corporation | Oxidative dehydrogenation using gel precipitated catalyst preparation |
| JPS603005B2 (en) * | 1978-05-08 | 1985-01-25 | 住友アルミニウム製錬株式会社 | Method for separating precipitated aluminum hydroxide from sodium aluminate solution |
| US4263261A (en) * | 1978-12-21 | 1981-04-21 | Sumitomo Aluminium Smelting Company, Limited | Method for the removal of impurities from sodium aluminate solution |
| US4678585A (en) * | 1981-12-30 | 1987-07-07 | American Cyanamid Company | Process for alumina recovery |
| US4608237A (en) * | 1985-04-24 | 1986-08-26 | Nalco Chemical Company | Use of polymers in alumina precipitation in the Bayer process of bauxite beneficiation |
| US4822593A (en) * | 1986-12-11 | 1989-04-18 | Aluminum Company Of America | Control of form of crystal precipitation of aluminum hydroxide using cosolvents and varying caustic concentration |
| US4737352A (en) * | 1987-04-09 | 1988-04-12 | Nalco Chemical Company | Use of surfactants in alumina precipitation in the bayer process |
| US4839060A (en) * | 1987-04-28 | 1989-06-13 | Suncor, Inc. | Methylated starch compositions and their use as flocculating agents for mineral wastes, such as bauxite residues |
| GB8824176D0 (en) * | 1988-10-14 | 1988-11-23 | Allied Colloids Ltd | Recovery of alumina from bauxite |
-
1990
- 1990-02-06 US US07/475,622 patent/US5106599A/en not_active Expired - Lifetime
- 1990-06-04 CA CA002018155A patent/CA2018155A1/en not_active Abandoned
-
1991
- 1991-02-18 AU AU71158/91A patent/AU633181B2/en not_active Ceased
Also Published As
| Publication number | Publication date |
|---|---|
| AU7115891A (en) | 1991-08-08 |
| AU633181B2 (en) | 1993-01-21 |
| US5106599A (en) | 1992-04-21 |
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