WO2018144336A1 - Treatment of aqueous compositions including fines - Google Patents

Treatment of aqueous compositions including fines Download PDF

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Publication number
WO2018144336A1
WO2018144336A1 PCT/US2018/015423 US2018015423W WO2018144336A1 WO 2018144336 A1 WO2018144336 A1 WO 2018144336A1 US 2018015423 W US2018015423 W US 2018015423W WO 2018144336 A1 WO2018144336 A1 WO 2018144336A1
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WO
WIPO (PCT)
Prior art keywords
composition
salt
consolidated material
water
water soluble
Prior art date
Application number
PCT/US2018/015423
Other languages
English (en)
French (fr)
Inventor
Paul C. PAINTER
Bruce G. Miller
Aron Lupinsky
Original Assignee
Extrakt Process Solutions, Llc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Extrakt Process Solutions, Llc filed Critical Extrakt Process Solutions, Llc
Priority to CN201880009271.XA priority Critical patent/CN110462165B/zh
Priority to PE2019001506A priority patent/PE20191364A1/es
Priority to BR112019015604-6A priority patent/BR112019015604B1/pt
Priority to CA3051124A priority patent/CA3051124A1/en
Priority to AU2018216688A priority patent/AU2018216688B2/en
Priority to EA201991820A priority patent/EA201991820A1/ru
Priority to MX2019008977A priority patent/MX2019008977A/es
Publication of WO2018144336A1 publication Critical patent/WO2018144336A1/en
Priority to US16/511,787 priority patent/US12129192B2/en
Priority to ZA2019/04660A priority patent/ZA201904660B/en
Priority to CONC2019/0009139A priority patent/CO2019009139A2/es

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B1/00—Dumping solid waste
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • B09B3/30—Destroying solid waste or transforming solid waste into something useful or harmless involving mechanical treatment
    • B09B3/38—Stirring or kneading
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • B09B3/80—Destroying solid waste or transforming solid waste into something useful or harmless involving an extraction step
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B5/00—Operations not covered by a single other subclass or by a single other group in this subclass
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • C02F11/14—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents
    • C02F11/148—Combined use of inorganic and organic substances, being added in the same treatment step
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/10—Nature of the water, waste water, sewage or sludge to be treated from quarries or from mining activities
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
    • C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
    • C02F2103/365—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds from petrochemical industry (e.g. refineries)
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00—Technologies for solid waste management
    • Y02W30/50—Reuse, recycling or recovery technologies
    • Y02W30/91—Use of waste materials as fillers for mortars or concrete

Definitions

  • the present disclosure relates to dewatering and consolidation of aqueous compositions including fines such as tailings from processing ore.
  • tailings stream characterized as a sluny of particulate matter in water.
  • These tailings often contain components that are hazardous and cannot be discharged directly into rivers and streams.
  • a common practice is to store tailings in ponds, which can be very large or encompass numerous sites. For example, it has recently been estimated that Canadian oil-sands tailings ponds cover an area of about 200 square kilometers.
  • the Environmental Protection Agency has identified more than 500 ash and coal sluny ponds, mostly in the Appalachian coal mining region.
  • phosphate mining results in the production of approximately 100,000 tons a day of phosphatic clays in the form of a slurry that is also stored in ponds. It is very difficult to dewater and the phosphate industry leaves about 40% of mined land in unstable clay settling areas.
  • the processes for mining and extracting of ores of aluminum, copper, zinc, lead, gold, silver, etc. also create tailing streams.
  • fines are defined as particles having a diameter equal to or less than 44 ⁇ . They are part of a waste stream that settles much more slowly than coarse sand, leaving a layer of water with some entrained fines near the surface of the ponds. This water is reused in the bitumen extraction process. Initially, most of the fines (mainly silica and clay particles) form an intermediate layer of so-called fluid fine tailings (FFT). This fluid has a low solids content, between 1 5% and 30% and is also referred to as thin fine tailings (TFT).
  • FFT fluid fine tailings
  • MFT mature fine tailings
  • So-called impoundment ponds are used to store two types of waste from coal handling and combustion.
  • Coal ash that is a residue of combustion is one such material and include several components (fly ash, bottom ash, etc.).
  • the second type of impoundment pond for coal processing wastes stores material that is a product of coal preparation plants, where soil and rock are removed from run-of-mine coal to lower its ash content and increase its value. This is accomplished by washing.
  • this coal cleaning process produces a reject stream in the form of a sludge or slurry.
  • This slurry contains very fine coal particles together with other material (such as clays) and, as with the tailings streams mentioned above, is very difficult to dewater economically using standard methods.
  • the impoundments can be as large as 50 acres in size and contain billions of gallons of toxic sludge. This material represents both an economic cost in terms of the loss of a valuable resource (in the form of coal fines) and a major environmental hazard.
  • the Washington Post (April 24, 2013) reported that a study by the Office of Surface Mining Reclamation and Enforcement found that many sludge impoundment walls are weak and are known to leak. Historically, a number of catastrophic failures of ash and sludge ponds have occurred, resulting in significant loss of life and environmental devastation. With the coal industry in decline and mining companies filing for bankruptcy, the impoundment ponds, both those that remain in use and those that have been abandoned, are a significant and growing problem.
  • Advantages of the present disclosure include processes to dewater aqueous compositions including fines, e.g., tailings, to produce high solids content materials.
  • the process comprises treating the composition, which includes fines and process water, with a highly water soluble salt.
  • the process can include treating the composition with at least one highly water soluble salt or solution thereof and can optionally include either or both of (i) at least one polymer flocculant or solution thereof and/or (ii) optionally coarse particles, e.g., sand, to form a treated composition.
  • the treated composition can include a consolidated material in the process water, which can then advantageously be separated from the consolidated material.
  • Implementations of the process of the present disclosure include, for example, (i) treating the composition with at least one highly water soluble salt to form a treated composition including a consolidated material in the process water, (ii) treating the composition with at least one highly water soluble salt and at least one polymer flocculant to form a treated composition including a consolidated material in the process water, (iii) treating the composition with at least one highly water soluble salt and coarse particles to form a treated composition including a consolidated material in the process water, and (iv) treating the composition with at least one highly water soluble salt, at least one polymer flocculant and coarse particles to form a treated composition including a consolidated material in the process water.
  • Each of these implementations can include aqueous solutions of the salt and/or polymer flocculant to treat the composition.
  • Each of these implementations can include separating the process water from the consolidated material.
  • the consolidated material has a density greater than the process water.
  • the aqueous composition including fines can be tailings.
  • the at least one highly water soluble salt can have a solubility in water (a salt/water solubility) of at least about 5 g/100 g at 20 °C, e.g., at least about 10 g/100 g at 20 °C,
  • the at least one highly water soluble salt is a non-hydrolyzing salt.
  • the at least one highly water soluble salt can have a monovalent cation and can include an ammonium based salt, a phosphate based salt, or a sulfate based salt or combinations thereof.
  • the treated composition can have a salt-composition concentration of at least 0.5 wt% of the at least one highly water soluble salt and preferably no less than about 1 wt%, such as at least about 2 wt% and even greater than about 3 wt%, 4 wt%, 5 wt%, etc. of the at least one highly water soluble salt.
  • the at least one polymer flocculant is a polyacrylamide or co-polymer thereof.
  • the treated composition can have a polymer-composition concentrati on of the at least one polymer flocculant of no less than about 0.001 wt%, e.g., no less than about 0.003 wt%, 0.005 wt%, 0.01 wt% or 0.04 wt%.
  • the composition is treated with coarse particles, e.g., sand, at a sand to fines ratio of less than 4: 1 , e.g., between about 2.5: 1.0 to about 0.5: 1 or between about 2.25: 1 to about 0.75: 1.
  • the polymer flocculant forms high density floes, e.g., having a density greater than the process water, which facilitates separation and dewatering of the consolidated solids.
  • treating the composition can include combining the composition with a solution including the at least one highly water soluble salt and the at least one polymer flocculant.
  • treating the composition can include combining a stream of the composition, e.g., tailings, with a stream of a solution including the at least one highly water soluble salt and a separate stream of a solution including the at least one polymer flocculant.
  • treating the composition can include combining a stream of the composition, e.g., tailings, with a stream of a solution including both the at least one highly water soluble salt and the at least one polymer flocculant.
  • Coarse particles can also be added to the composition or stream thereof and/or to any or all of the solution streams.
  • the streams can be mixed inline and/or with the aid of an inline mixer.
  • treating the composition can be carried out at a temperature of no more than 50 °C, e.g., no more than about 40 °C or about 30 °C.
  • treating the composition includes using a solution of one or more highly soluble salts sourced from a natural or existing source such as seawater or a body of hypersalme water.
  • the process water can be separated from the consolidated material by any one or more of decanting, filtering, vacuuming, gravity draining, electrofilteriiig, etc. or combinations thereof.
  • separating the process water from the consolidated material can include mechanically dewatering the consolidated material, e.g., mechanically dewatering the consolidated material by a dewatering screw. Once separated, the consolidated material can be transferred for further dewatering or disposal.
  • the separated process water can include the at least one highly water soluble salt and the process can further comprise recovering at least a portion of the separated process water.
  • the process can further comprise recycling at least a portion of the recovered separated process water to treat additional tailings.
  • the process can further include purifying at least a portion of the recovered process water,
  • Yet another aspect of the present disclosure includes recovering valuable materials from the aqueous composition of fines, e.g., tailings.
  • the valuable materials can include rare earth elements (REE) associated with solids such as clays in tailings from various types of aqueous fines such as tailings stream. Therefore, in practicing certain aspects of the processes of the present disclosure and the various embodiments thereof, the aqueous compositions can further include rare earth element materials which can be recovered by treating the composition with at least one highly water soluble salt e.g., an ammonium based salt such as ammonium sulfate, to form a treated composition including REE in the process water and/or in the consolidated materials.
  • the process further includes separating the process water from the consolidated material and recovering the REE from the separated process water and/or the consolidated materials.
  • the processes of the present disclosure can consolidate the solids of the composition to produce a consolidated material having a solids content in excess of about 45% by weight, e.g., a solids content of greater than about 50% and higher than about 60%, 65%, 70% and 75% by weight.
  • the consolidated material formed in the treated composition according to certain embodiments can result in a high solids content after mixing and/or dewatering the treated composition in a short period of time.
  • the consolidated material can have a solids content of greater than about 50% and at least about 60%, 65%, 70%, 75% and 80% by weight after mixing and/ or dewatering.
  • the aqueous solution includes a highly water soluble ammonium based salt and a polymer flocculant, e.g., a water soluble polymer.
  • Embodiments include, together or individually, an aqueous solution of one or more of the highly water soluble salt(s) and having a concentration of no less than about I wt%, e.g., at least about 2 wt%, 5 wt%, 10 wt%, 20 wt%, 30 wt% and even as great as a 40 wt% or as an aqueous salt slurry.
  • the aqueous solution can also include one or more of the polymer flocculant(s) and having a concentration of no less than about 0.005 wt%, e.g. no less than about 0.01 wt%, 0.04 wt%, 0.05 wt %, 0.1 wt%, 0,2 wt%, 0.4 wt%, for example
  • Figure 1 schematically illustrates an exemplary embodiment of a process of consolidating an aqueous composition including fines and process water.
  • Figure 2 shows pictures of vials containing waste coal slurry treated according to an embodiment of the present disclosure. The pictures show coal slurry after adding an ionic solution (left), then centrifuging (middle) and after removal of supernatant solution (right).
  • Figure 3 shows pictures of the dewatered coal slurry from Figure 2 after removal from the vial (left) and subsequent hand-pressing between paper towels.
  • Figure 4 shows pictures of vials containing mature fine tailings from oil sands processing treated with an ammonium salt solution including a polyacrylamide flocculant at the concentrations indicated in the figure.
  • Figure 5 shows pictures of vials containing mature fine tailings treated with an ammonium salt and a polyacrylamide flocculant and illustrate effects of increasing salt concentration and reducing polymer concentration under the conditions tested.
  • Figure 6 shows a picture of vials containing mature fine tailings from oil sands processing treated with seawater which included varying amounts of a polyacrylamide flocculant.
  • Aqueous compositions of fines can be in the form of tailings, which are typically produced when mining and processing ores such as metal ores, e.g., aluminum, copper, zinc, lead, gold, silver, etc., phosphate ore, oil sands, etc.
  • Aqueous compositions of fines can also be produced when processing coal. For example, certain processes finely grind coal prior to combustion to more readily liberate pyrite (a sulfur based compound) and hence reduce sulfur emissions upon combustion of the ground coal. Such processes can produce fine coal particles as well as other fine mineral or mineral matter in an aqueous composition that are difficult to recapture and reuse.
  • the particulate solids in the aqueous compositions of the present disclosure can be minerals and mineral like materials, i.e., mineral matter, clays, slit, and in sizes ranging from fines to coarse solids.
  • the term fines as used herein is consistent with the Canadian oil sands classification system and means solid particles with sizes equal to or less than 44 microns ( ⁇ ). Sand is considered solid particles with sizes greater than 44 ⁇ .
  • the composition of the fines depends on the source of the materials, but generally fines are comprised mostly of silt and clay material and sometimes minerals or mineral matter, depending on the ore. Tailings can have various solids contents and various amounts of fines as its solids content.
  • the tailings treated according to embodiments of the present disclosure can include a significant amount of fines by weight (>5 wt%) as their solids content.
  • Such tailings can include at least about 10 wt%, 20 wt%, 30 wt%, 40 wt%, 50 wt%, 60 wt%, 70 wt% or higher fines as their solids content.
  • the process of the present disclosure can consolidate the solids of aqueous compositions including fines, e.g., tailings, to produce consolidated material having a solids content in excess of about 45% by weight, e.g., a solids content of greater than about 70% by weight.
  • coagulation and flocculation are often used interchangeably in the literature. As used herein, however, coagulation means particle aggregation brought about by the addition of hydrolyzing salts, whereas flocculation means particle aggregation induced by flocculating polymers. Hydrolyzing salts undergo hydrolysis when added to water to form metal hydroxides, which precipitate from the solution, trapping fines and other minerals in the coagulating mass. Hydrolyzing salts typically have low solubility in water and are used as coagulants. Aggregation induced by flocculation, in contrast, is believed to be the result of the polymer binding to the particles thereby tying the particles together into a so called floe causing aggregation of the particles.
  • an aqueous composition of fines and process water can be consolidated by treating the composition with one or more highly water soluble salt(s) or an aqueous solution thereof to destabilize and consolidate solids in the composition, e.g., to destabilize and consolidate fines in the composition.
  • the composition is tailings, e.g., a suspension of particulate solids in an aqueous liquid which include fines and process water such as tailings streams from metal extraction or a coal slurry which includes fines of coal and other matter.
  • the process includes treating the composition with the highly water soluble salt(s) or an aqueous solution thereof to form a treated composition including a consolidated material, e.g. consolidated fines, in process water.
  • the process water can then be separated from the consolidated material.
  • the consolidated material has a solids content of at least 45% by weight, e.g., a solids content of greater than about 50% and higher than about 60%, 65%, 70% and 75% by weight.
  • Salts that are useful in practicing the present disclosure include salts that are highly soluble in water.
  • a highly water soluble salt as used herein is one that has a solubility in water of greater than 2 g of salt per 100 g of water (i.e., a salt/water solubility of 2g/100g) at 20 °C.
  • the highly water soluble salt has a water solubility of at least about 5 g/ ' lOO g at 20 °C, e.g., at least about 10 g/100 g of salt/water at 20 °C.
  • the highly water soluble salts used in the processes of the present disclosure are preferably non-hydroiyzing.
  • Hydrolyzing salts undergo hydrolysis when added to water to form metal hydroxides, which precipitate from the solution. Such hydrolyzing salts are believed to form open floes with inferior solids content and cannot be readily recycled for use with additional tailings in continuous or semi-continuous processes.
  • hydrolyzing salts typically have low solubility in water and are used at elevated temperatures to ensure sufficient solubility for aggregation, which is an energy intensive process. See US 4,225,433 which discloses the use of lime as a coagulating agent at a temperature of 75 °C.
  • the highly water soluble salts are preferably not carboxylate salts since such organic acid salts tend to be more expensive than inorganic salts and can be deleterious to plant and/or animal life.
  • Highly water soluble salts that are not hydrolyzing and useful in practicing processes of the present disclosure include salts having a monovalent cation, e.g., alkali halide salts such as sodium chloride, potassium chloride; also salts with monovalent cations such as sodium nitrate, potassium nitrate, sodium and potassium phosphates, sodium and potassium sulfates, etc. are useful in practicing processes of the present disclosure.
  • alkali halide salts such as sodium chloride, potassium chloride
  • salts with monovalent cations such as sodium nitrate, potassium nitrate, sodium and potassium phosphates, sodium and potassium sulfates, etc. are useful in practicing processes of the present disclosure.
  • ammonium based salts such as ammonium acetate (NH 4 C 2 H 3 O 2 ), ammonium chloride (NH 4 CI), ammonium bromide (NH+Br), ammonium carbonate ((NH 4 ) 2 C03), ammonium bicarbonate (NH 4 HCO 3 ), ammonium nitrate (NH 4 NO 3 ), ammonium sulfate ((NH 4 ) 2 S0 4 ), ammonium hydrogen sulfate (NH 4 HSO 4 ), ammonium dihydrogen phosphate (NH 4 H 2 P0 4 ), ammonium hydrogen phosphate ((NH 4 ) 2 HP0 4 ), ammonium phosphate ((NH ⁇ PC ⁇ ), etc. Mixtures of such salts can also be used.
  • ammonium based salts such as ammonium acetate (NH 4 C 2 H 3 O 2 ), ammonium chloride (NH 4 CI), ammonium bromide (NH+Br), ammonium carbonate ((NH 4
  • Ammonium based salts are useful for practicing the present disclosure since residual ammonium based salts on the consolidated material after combining the salt with the aqueous fines, e.g., tailings, can be beneficial to plant life.
  • many of the ammonium based salts are useful as fertilizers, e.g., ammonium chloride, ammonium nitrate, ammonium sulfate, etc.
  • Many of the monovalent sulfate and phosphate salts are also useful as fertilizers.
  • the highly water soluble salt or salts used in the processes of the present disclosure can preferably be non-toxic and beneficial to plant life to aid in environmental remediation and the restoration of mine sites.
  • treating the compositions of the present disclosure with a highly water soluble salt destabilizes and consolidates solids in the composition.
  • a highly water soluble salt can include mixing the composition, which includes fines and process water, with a highly water soluble salt to consolidate the fines, and separating the process water from the consolidated fines to produce a high solids content, e.g., at least 45% by- weight.
  • the highly water soluble salt is an ammonium based salt.
  • Highly water soluble salts that can be used in practicing the present process can also include salts having multivalent cations.
  • Such salts include, for example, divalent cation salts such as calcium and magnesium cation salts, such as calcium chloride (CaCl 2 ), calcium bromide (CaBr 2 ), calcium nitrate i( ' a( ⁇ ' () ) ⁇ ).
  • the highly water soluble salts used in the processes of the present disclosure are preferably non-hydrolyzing. Many of the multivalent cation salts are hydro lyzing and thus less preferred for the reasons stated above. Moreover, experimentation with multivalent salts showed increased fouling of containers and formation of less cohesive consolidated materials as compared to highly water soluble salts having monovalent cations.
  • some multivalent salts such as FeCl 3 and Fe 2 (S0 4 ) 3
  • FeCl 3 and Fe 2 (S0 4 ) 3 are particularly corrosive and Fe 2 (S0 4 ) 3 is formed from oxidizing pyrite and results in acid mine runoff, which make such salts less preferable for use in processes of the present disclosure.
  • the salt-composition concentration of the at least one highly water soluble salt should preferably be at least 0.5 wt% and preferably no less than about 1 wt%, such as at least about 2 wt% and even at least about 3 wt%, 4 wt%, 5 wt%, etc.
  • salt-composition concentration refers to the concentration of the highly water soluble sait(s) in the treated aqueous fines, e.g., tailings, and is determined by taking the percentage of the mass of highly water soluble salt(s) divided by the combined mass of the salt(s) plus the aqueous fines and any water used to dilute the salt(s). For example, combining 1 part undiluted (i.e., neat) salt to 99 parts tailings by weight results in a salt-composition concentration of 1 wt%. Alternatively, treating tailings with an equal weight of a 2 wt% solution of the salt also results in a salt-composition concentration of 1 wt% in the treated tailings.
  • the highly water soluble salt(s) can be used to treat compositions of the present disclosure as a solid, e.g., combining the salt as a powder with the composition.
  • the salt can be used to treat as a solution, e.g., combining an aqueous salt solution with the compositions.
  • an aqueous solution of the highly water soluble salt can be prepared having a concentration of no less than about 1 wt%, e.g., greater than about 2 wt%, 5 wt%, 10 wt%, 20 wt%, 30 wt% and even as great as a 40 wt% or as an aqueous salt slurry.
  • composition and salt solution or slurry should be mixed at a ratio sufficient to destabilize the composition to cause consolidation of the solids therein.
  • the composition and the salt solution are mixed at a ratio of between 5.0: 1.0 and 1.0:5.0, e.g., mixed at a ratio between 1.5: 1.0 to 1.0: 1.5 composition to salt solution.
  • a natural source of a highly soluble salt or salts such as in a natural body of water including such salts in sufficiently high concentration such as at least about 2 wt% and even at least about 3 wt% or greater.
  • ocean or sea water can be used as a source of highly soluble salts, which can significantly improve the economics of the process under certain conditions.
  • the vast majority of seawater has a salinity of between 31 g/kg and 38 g/kg, that is, 3.1 -3.8%.
  • seawater in the world's oceans has a salinity of about 3.5% (35 g/'L, 599 mM).
  • Seawater includes of a mixture of salts, containing not only sodium cations and chlorine anions (together totaling about 85% of the dissolved salts present), but also sulfate anions and calcium, potassium and magnesium cations. There are other ions present (such as bicarbonate), but these are the mam components.
  • Another natural source of highly soluble salts that can be used as a source of highly soluble salts includes a hypersaline body of water, e.g., a hypersaline lake, pond, or reservoir.
  • a hypersaline body of water is a body of water that has a high concentration of sodium chloride and other highly soluble salts with saline levels surpassing ocean water, e.g., greater than 3.8 wt% and typically greater than about 10 wt%.
  • Such hypersaline bodies of water are located on the surface of the earth and also subsurface, which can be brought to the surface as a result of ore mining operations.
  • the solids in the composition can be consolidated such as by mixing followed by gravity sedimentation in a settling tank or by centrifugation to increase the rate of forming a consolidated material in the treated composition.
  • the consolidated material can be separated from the process water by decanting, filtering, eletrofiltration, cross-flow filtering, vacuuming, and/or by mechanical dewatering, i.e., applying an external force to the consolidated material. Once separated, the consolidated material can be transferred for further dewatering or disposal.
  • the processes of the present disclosure can also include treating aqueous fines with coarse particles, e.g., particles with sizes greater than 44 ⁇ , such as sand, to significantly increase the solids content.
  • coarse particles e.g., particles with sizes greater than 44 ⁇ , such as sand
  • sand is appropriate for aqueous fines that have solids mostly as fines, as the fine particles can sit in the voids between the coarse particles, enhancing packing and solids content. It was found, however, that for certain compositions such as coal slurry, the addition of sand was not needed to achieve a high solids content, as there were sufficient coarse particles present in the aqueous fines stream to give a high solids content material.
  • implementations of the process of the present disclosure include, for example, (i) treating the composition with at least one highly water soluble salt to form a treated composition including a consolidated material in the process water, (ii) treating the composition with at least one highly water soluble salt and at least one polymer floccuiant to form a treated composition including a consolidated material in the process water, (in) treating the composition with at least one highly water soluble salt and coarse particles to form a treated composition including a consolidated material in the process water, and (iv) treating the composition with at least one highly water soluble salt, at least one polymer floccuiant and coarse particles to form a treated composition including a consolidated material in the process water.
  • Each of these implementations can include aqueous solutions of the salt and/or polymer floccuiant to treat the composition.
  • Each of these implementations can include separating the process water from the consolidated material.
  • the consolidated material has a density greater than the process water.
  • the process water can then be readily separated from the consolidated material as, for example, by one or more of decanting, filtering, gravity draining, effectrofiltering, cross- flow filtering, vacuuming and other evaporating techniques, etc. and/or by one or more of a device for dewatering consolidated material such as a centrifuge, decanting centrifuge, dewatering screw, hydrocyelone, vacuum belt filter, filter press or pressing devices, etc.
  • the separated consolidated material can be disposed or deposited in a containment structure which allows removal of released water from the consolidated material,
  • Polymers that are useful in practicing the present disclosure include water soluble flocculating polymers such as polyacrylamides or copolymers thereof such as a nonionic polyacrylamide, an anionic polyacrylamide (APAM) such as a polyacrylamide-co-acrylic acid, and a cationic polyacrylamide (CPAM), which can contain co-monomers such as acryloxyethyitrimethyl ammonium chloride, methacryloxyethyltrimethyl ammonium chloride, dime thy ldi ally ammonium chloride (DMDAAC), etc.
  • APAM anionic polyacrylamide
  • CPAM cationic polyacrylamide
  • water soluble flocculating polymers useful for practicing the present disclosure include a polyamine, such as a polyamine or quaternized form thereof, e.g., polyacrylamide-co-dimethylaminoethylacrylate in quaternized form, a polyethyleneimine, a polydiallyldimethyl ammonium chloride, a polydicyandiamide, or their copolymers, a polyamide-co-amine, poly electrolytes such as a sulfonated polystyrenes can also be used.
  • Other water soluble polymers such as polyethylene oxide and its copolymers can also be used.
  • the polymer flocculants can be synthesized in the form of a variety of molecular weights (MW), electric charge types and charge density to suit specific requirements.
  • the flocculating polymer used in practicing processes of the present disclosure do not include use of activated polysaccharides or activated starches, i.e., polysaccharides and starches that have been heat treated, in sufficient amounts to lower the density of the floe to below the density of the process water from which they are separated.
  • activated polysaccharides and activated starches when used in sufficiently high dosages tend to form low density floes which rise to the surface of an aqueous composition, which can hinder removal of solids in large scale operations involving high solids content and can also hinder dewatering of consolidated material.
  • the amount of polymer(s) used to treat aqueous fines should preferably be sufficient to flocculate the solids in the composition and any added coarse particles, e.g., sand.
  • the amount of poiymer(s) used to treat an aqueous composition which includes fines and process such as tailings can be characterized as a concentration based on the total weight of the composition or as a dosage based on the weight percent of the solids in the composition.
  • the concentration of the one or more polymer flocculant(s) in the treated composition has a polymer-composition concentration of no less than about 0.001 wt%, e.g., no less than about 0.003 wt%, 0.005 wt% or no less than about 0.01 wt%.
  • a polymer-composition concentration of no less than about 0.001 wt%, e.g., no less than about 0.003 wt%, 0.005 wt% or no less than about 0.01 wt%.
  • polymer-composition concentration refers to the concentration of the flocculating polymer(s) in the treated composition and is determined by taking the percentage of the mass of the polymer(s) divided by the combined mass of the polymer(s) plus the composition and any water used to dissolve the polymer(s). For example, combining 1 part undiluted (i.e., neat) polymer to 9999 parts tailings by weight results in a polymer-composition concentration of 0.01 wt%. Alternatively, treating tailings with an equal weight of a 0.02 wt% solution of the polymer also results in a polymer-composition concentration of 0.01 wt%.
  • aqueous fines are treated with at least one polymer flocculant to yield a polymer- composition concentration of no less than about 0.02 wt%, such as no less than about 0.03 wt%, 0.04 wt%, 0.05 wt%, and even at least about 0.07 wt%, 0.09 wt%, 0.1 wt%, 0.2 wt%, etc.
  • the amount of poly mer flocculant can be used in greater concentrations. However, after certain high concentrations it becomes difficult to dissolve the flocculant, the solution becomes too viscous and the process is less economical.
  • the concentration of the one or more polymer flocculant(s) in the treated composition has dosage (weight of the flocculant(s) to weight of the solids in the composition, e.g., tailings) of no less than about 0.005 wt%, e.g., no less than about 0.01 wt% and preferably no less than about 0.015 wt%, 0.020 wt%, 0.025 wt%, 0.03 wt%, or 0.04 wt%.
  • the amount of polymer flocculant can be reduced if the salt-composition concentration is increased. While the reason for this effect is not clear, a very low polymer- composition concentration of no less than about 0.001 wt%, e.g. no less than about 0.003 wt%, 0.005 wt%, 0.01 wt%, 0.02 wt%, 0.03 wt%, 0.04 wt%, 0.05 wt %, for example, can achieve reasonably fast consolidation of solids in composition, e.g., tailings, if the salt-composition concentration is increased.
  • Coarse particles useful for practicing certain processes according to the present disclosure are preferably sand and when used in treating compositions the amount of such particles are preferably in a sand to fines ratio (SFR ratio) of less than 4: 1, e.g., between about 2.5: 1.0 to about 0.5: 1 or between about 2.25: 1 to about 0.75: 1.
  • SFR ratio is calculated by determining the amount of sand added to an estimated amount of solid fines in the aqueous fines on a weight basis. It is believed that the use of coarse particles facilitates packing of the consolidated fines which advantageously increases the solids content and can even form a jammed structure of consolidated solids, i.e. a structure in which generally individual particles of the consolidated solid can no longer move freely relative to other particles.
  • Treating an aqueous composition including fines and process water, e.g., tailings, with at least one highly water soluble salt and optionally with either or both of at least one polymer flocculant and/or optionally sand can be carried out in a number of ways.
  • treating the composition includes combining and/or mixing the various components.
  • the at least one salt can be added directly to the composition either as an undiluted solid in powder form or as a solution; the at least one polymer flocculant can be added directly to the composition either as an undiluted material or as a solution, and the sand can be added to the composition directly or with the salt and/or polymer or solutions thereof.
  • the salt and polymer can be combined in a single solution, with or without sand, and combined with the composition.
  • the order of combining the salt, polymer and sand to the composition can give equivalent results and optimization of the process will depend on the type of composition, and the scale and equipment used in the process.
  • an aqueous solution of one or more highly water soluble salt(s) can be prepared having a concentration of no less than about 0.5 wt% or 1 wt%, e.g., at least about 2 wt%, 3 wt%, 4 wt%, 5 wt%, 6 wt%, 7 wt%, 10 wt%, 20 wt%, 30 wt% and even as great as a 40 wt% or as an aqueous salt slurry for use in treating the composition.
  • the one or more polymer flocculant(s) can also be included in the aqueous solution of the salt(s) and can have a concentration of no less than about 0.005 wt%, e.g., no less than about 0.01 wt%, 0.04 wt%, 0.05 wt %, 0.1 wt%, 0.2 wt%, 0.4 wt%, for example.
  • the aqueous solution of the highly water soluble salt(s) and polymer flocculant(s) can be used to treat the composition and can be combined with such compositions at a ratio of between 5.0: 1.0 and 1.0:5.0, e.g., at a ratio between 1.5: 1.0 to 1.0: 1.5 of composition to aqueous solution.
  • Sand can be combined with the composition before, during, or after combining the composition with the solutions.
  • the temperature of the treated aqueous fines need not be elevated above ambient to practice the process.
  • treating the composition according to the various embodiments herein can be carried out at a temperature of no more than 50 °C, e.g., no more than about 40 °C or about 30 °C.
  • the tailings stream may already be warm or hot as a result of prior processing. The processes of the present disclosure can be applied directly to these tailings streams.
  • compositions e.g., a suspension of particulate solids in an aqueous liquid which include fines and process water
  • Treating compositions e.g., tailings, in tins manner can cause destabilization and consolidation of the solids, e.g., fines and sand, in the treated composition to form a consolidated material, which can settle under gravity relatively quickly, in the process water.
  • solids e.g., fines and sand
  • the treated compositions and/ or consolidated material can be further dewatered to further separate the process water from the consolidated material and, in some instances, further consolidate the solids.
  • the consolidated material formed in the treated compositions can be separated from the process water by any one or more of decanting, filtering, e.g., electrofiltering, cross-flow filtering, gravity draining, vacuuming and other evaporating techniques, etc. and/or by any one or more of a mechanical dewatering, i.e., applying an external force to the consolidated material, with a device for dewatering consolidated material such as by- applying a centrifuge, decanting centrifuge, dewatering screw, hydrocyclone, filter press, pressing device, etc.
  • the process water can be separated from the consolidated material by passing a stream of treated composition through a cross-flow filter, e.g., a porous or slotted pipe, which filters and dewaters the treated composition stream to separate the process water from the consolidated material. The process water can then be readily separated from the consolidated material.
  • the process water can be separated from the consolidated material by gravity draining to achieve a solids content of at least about 70% within about a month after treating the tailings, e.g., within about two weeks or within about one week of gravity draining after treating the tailings.
  • the consolidated material can be further dewatered after separating from the treated composition by depositing the separated consolidated material in a thin lift deposition.
  • the consolidated material formed in the treated compositions can advantageously have a high solids content, e.g., a solids content of greater than about 50% and at least about 60%, 65%, 70% and 75% by weight.
  • the consolidated material formed in the treated compositions according to certain embodiments can result in a high solids content after mixing and/or dewatering the treated compositions in a short period.
  • the consolidated material can have a solids content of greater than about 50% and at least about 60%, 65%, 70%, 75% and 80% by weight after mixing and/or dewatering.
  • a solids content of at least about 70 % is achieved within about one month of gravity draining after treating the composition, e.g., within about two weeks or within about one week of gravity draining after treating the composition.
  • the process includes mixing the composition with a highly water soluble salt, e.g., an ammonium based salt, a water soluble polymer, e.g., a polyacryiamide, and optionally sand, such as in a sand to fines ratio of between about 2.25: 1 to about 0.75: 1 to form a treated composition including a consolidated material having a high solids content, e.g., a solids content of greater than about 50% by weight, e.g., at least about 60%, 65%, 70 wt% or higher in less than 10 minutes, depending on the dewatering method used.
  • a highly water soluble salt e.g., an ammonium based salt
  • a water soluble polymer e.g., a polyacryiamide
  • optionally sand such as in a sand to fines ratio of between about 2.25: 1 to about 0.75: 1 to form a treated composition including a consolidated material having a high solids
  • a rare earth element as defined by IUPAC, is one of a set of seventeen chemical elements in the periodic table, specifically the fifteen lanthanides, as well as scandium and yttrium. Scandium and yttrium are considered rare earth elements because they tend to occur in the same ore deposits as the lanthanides and exhibit similar chemical properties. Many of the REE are used in electronic devices, magnets, high performance coatings.
  • Such REE include cerium (Ce), dysprosium (Dy), erbium (Er), europium (Eu), gadolinium (Gd), holmium (Ho), lanthanum (La), lutetium (Lu), neodymium (Nd), praseodymium (Pr), promethium (Pm), samarium (Sm), scandium (Sc), terbium (Tb), thulium (Tm), ytterbium (Yb) and yttrium (Y).
  • REE in aqueous fines are typically in the form of an ion or oxide.
  • zirconium can be present as zircon
  • ZrSi0 4 titanium can be present as the minerals ilmenite, leucoxene and rutile.
  • Coal ash and coal cleaning wastes contain rare earth elements. Fire cla - coal ash has unusually high concentrations of Yttrium and zirconium. Oil sands tailings also contain REE.
  • REEs absorb on the surface of clays in tailings.
  • REEs are predominately included among the solids of the tailings but can also be in the process water. Absorbed REEs can be exchanged with the highly water soluble salts of the present disclosure, e.g., ammonium based salts due to an exchange of ammonium ions for the REE ions.
  • REEs from the solids of the tailings can be obtained by leaching the solids with acid followed by- extraction and precipitation or by caustic decomposition followed by acid leaching.
  • Another aspect of processes of the present disclosure includes consolidating an aqueous composition including fines and process water, e.g., tailings, which include REE materials by treating the composition with at least one highly water soluble salt, e.g., an ammonium based salt such as ammonium sulfate, to form a treated composition including a consolidated material in process water which includes the REE materials in the process water and/or among the consolidated materials.
  • the treated composition consolidates the fines and also separates REE materials from the solids and into the process water. The process water can then be separated from the consolidated material and the REE materials can be recovered from the separated process water.
  • the REE materials can be recovered from the process water by precipitation, e.g., using oxalic acid, or extraction.
  • Other methods for recovering REE from the process water include mineral processing and physical beneficiation, deep eutectic solvents/ionic liquids extraction, acid dissolution, high temperature phase separations, use of REE selective sorbents, photophoresis, in-situ brine injection and extraction, reactive grinding, etc.
  • the treated composition consolidates the fines and REEs are among the consolidated materials. The process water can then be separated from the consolidated material.
  • the consolidated material can then be leached with acid, e.g., nitric acid, sulfuric acid, etc., followed by extraction with solvent and/or ion exchange resins and precipitated.
  • acid e.g., nitric acid, sulfuric acid, etc.
  • the consolidated material can then be treated with a caustic reagent such as sodium hydroxide to decompose certain of the materials to form hydroxides of the REEs followed by leaching in acid, e.g., HC1.
  • the composition which includes REE materials can be treated with at least one polymer f!occulant and optionally sand to form the treated composition.
  • the treated composition can have a salt-composition concentration of at least 0.5 wt% of the at least one highly water soluble salt and preferably no less than about 1 wt%, such as at least about 2 wt% and even greater than about 3 wt%, 4 wt%, 5 wt%, etc. of the at least one highly water soluble salt.
  • the process of the present disclosure allows for large scale treatment of aqueous fines in a continuous or semi -continuous process with further recovering, recycling and purifying at least a portion of the process water in the aqueous fines and optionally recovering REE materials.
  • the process water separated from an initial treated composition can advantageously include a significant amount of the one or more highly water soluble salt(s) initially used to treat the composition.
  • the separated process water includes the at least one highly water soluble salt and the process includes recovering at least a portion of the separated process water; recycling at least a portion of the recovered separated process water to treat additional aqueous fines; and/or purifying at least a portion of the recovered process water.
  • the separated process water includes REE materials salt and the process further includes recovering at least a portion of the separated process water; recycling at least a portion of the recovered separated process water to treat additional aqueous fines; recovering the REE materials and/or purifying at least a portion of the recovered process water.
  • FIG. 1 schematically illustrates such an exemplary continuous or semi- continuous process.
  • aqueous compositions including fines and process water are treated with one or more highly water soluble salt(s), and optionally one or more polymer flocculant(s) and optionally coarse particles (sand) by combining a stream of the salt(s) (101a), which can be an aqueous solution with a stream of the composition (103a).
  • the composition is a tailings composition but other aqueous fines compositions can be processed in the same manner.
  • the composition can also be treated with one or more polymer flocculant(s) by combining a stream of the flocculants(s) (102a), which can be as an aqueous solution, with the composition stream (103a).
  • the salts(s) and f!occulant(s) can be combined together as a solution to treat the tailings as a stream thereof.
  • Coarse particles (sand) can also be added to the composition or stream thereof and/or to any or all of the solution streams.
  • the solution streams of salt(s) and polymer(s) can be sourced from holding tanks
  • the streams of aqueous fines and sand can be sourced from holding tanks 103 and 105, respectively.
  • the Tailings can be sourced from an oil sands extraction operation.
  • the stream of salt(s) ( 101a) and polymer(s) ( 102a) and tailings stream (103a) are carried to mixing device 107 where a stream of sand (105a) is added and the combination mixed.
  • Mixing device 107 can be an inline mixer, a mixing tank, ribbon mixer or other mixing device that can mix streams 101a, 102a, 103a and 105a.
  • the aqueous fines are combined with the salt(s) and poiymer(s) as solutions followed by addition of sand to treat the aqueous fines.
  • the sand can be combined with the aqueous fines (105b) followed by mixing with the salt(s) and polymer(s) solutions.
  • the sand can be added as a wet or dry stream.
  • the combination of the streams in a line can cause sufficient mixing to eliminate the need for a separate mixing device, e.g., inline mixing, and the combined streams can be carried directly to a mechanical dewatering device to separate consolidated material from process water and, in some instances, to further consolidate the solids in the consolidated material.
  • the treated aqueous fines which include a consolidated material and process water, is transferred to dewatering device 109 to separate the process water from the consolidated material.
  • dewatering devices include, for example, one or more of a decanting, filtering, electrofiltering, cross-flow filtering, gravity draining, or vacuuming device or combination thereof and/or by one or more of a device for dewatering consolidated material such as a centrifuge, decanting centrifuge, dewatering screw, hydrocyclone, vacuum belt filter, filter press or pressing devices, etc, or combinations thereof.
  • the recovered process water in tank 111 includes the process water from the aqueous fines, e.g., tailings, diluted with stream 101a and thus includes residual salt(s) from the one or more highly water soluble salt(s) and can possibly include residual polymer(s) from the one or more polymer flocculant(s) as well as contaminants from the aqueous fines. If the aqueous fines include REE materials, the recovered process water in tank 111 and/or the consolidated material in 113 can also include REE materials.
  • the recovered process water in tank 11 can then be transferred to a water purifying system 115 to purify at least a portion of the recovered process water which is transferred to tank 117.
  • Water purifying systems that can be used for embodiments of the processes of the present disclosure include reverse osmosis systems, vacuum distillation systems, electrodialysis, filtration systems, etc.
  • the remaining, non-purified recovered process water is transferred to tank 119 to recover process water including the one or more highly water soluble salt(s) and highly water soluble salts that are constituents of the original aqueous fines. This remaining, non-purified recovered process water can be recycled back to the treatment process.
  • the non-purified recovered process water can be recycled back to holding tank 101 and deficiency in the concentration of the salt(s) or polymer(s) can be corrected by adding additional highly water soluble salt(s) or polymer flocculant(s) from one or more make-up tanks such as make-up containers 121 and 22.
  • the process of the present disclosure can also include recovering REE materials from recycled separated process water or from the consolidated solids.
  • the REE materials can be recovered from the process water by precipitation, e.g., using oxalic acid, or extraction.
  • REE from the process water examples include mineral processing and physical beneficiation, deep eutectic solvents/ionic liquids extraction, acid dissolution, high temperature phase separations, use of REE selective sorbents, photophoresis, in-situ brine injection and extraction, reactive grinding, etc.
  • the process of the present disclosure can also include recovering REE materials from the consolidated solids by acid leaching or caustic decomposition.
  • the process of the present disclosure can include adding an organic solvent (e.g., naphtha, kerosene or a C5-8 hydrocarbon, such as pentane, hexane, heptane, benzene, toluene, etc. or mixtures thereof) to dilute organic material included with the aqueous fines, e.g., tailings such as residual hydrocarbons, organic solvents, oil, bitumen.
  • an organic solvent e.g., naphtha, kerosene or a C5-8 hydrocarbon, such as pentane, hexane, heptane, benzene, toluene, etc. or mixtures thereof
  • organic solvent e.g., naphtha, kerosene or a C5-8 hydrocarbon, such as pentane, hexane, heptane, benzene, toluene, etc. or mixtures thereof
  • tailings such as residual hydrocarbons
  • the consolidated solids can be recovered.
  • the recovered consolidated solids can include residual highly water soluble salt(s) from the treatment of the tailings.
  • the salt used in treating the tailings are beneficial to plant life, such as an ammonium based salt or sulfate based salt or phosphate based salt
  • the residual salt can act as a fertilizer with the consolidated solids.
  • the recovered consolidated solids can include REE materials which can be separated from the consolidated solids as explained elsewhere.
  • the vial was then centrifuged for 30 seconds at 3000 rpm and the particles consolidated into a compact mass, as shown in the picture in the center of Figure 2.
  • the supernatant liquid appeared to be clear, with no visible suspended particles.
  • the compacted solids Upon removal of the liquid it was found that the compacted solids have enough cohesive strength to hold their shape when the vial was inverted, as can be seen in the picture on the right in Figure 2.
  • Table 2 Solids content of MFT treated with an equal weight of a salt/P AM solution with the addition of sand (SFR ratio 1 : 1) after centrifugation.
  • the salt-tailings concentration was about 5 wt%.
  • the salt-tailings concentration was about 2.5 wt%.
  • Table 1 reports the solids content of dried consolidated material following treating of MFT with the various salt/polymer solutions without sand. After centrifugation for just 30 seconds, the highly water soluble salts gave solids contents for the consolidated materials in a range between about 31%-37%. However, the use of highly water soluble salts having a multivalent cation such as the aluminum and ferric cations appeared to cause fouling of the vial walls and gave a less cohesive consolidated material as compared to highly water soluble salts having a monovalent cation under the tested conditions.
  • Table 2 reports the solids content of dried consolidated material following treating
  • the salt-tailings concentration in treated MFT can be achieved in a number of ways. For ease of handling in the foregoing vial tests, it was convenient to combine equal weights of salt/polymer solutions to MFT. However, smaller amounts of salt/polymer solutions with higher concentrations thereof to give the same salt-tailings concentration give equivalent results of consolidated materials.
  • Centrifuging in flat-bottomed vials is not as effective in terms of producing a high solids material as using centrifuge tubes. It should be kept in mind that for all sets of laboratory vial and tube tests, there is always solution remaining in the voids between the particles. It will be shown later that the solids content of the consolidated material can easily be increased from the 46%-58% range by simply draining or the use of mechanical dewatering methods known to the art, such as filter presses, belt filters, cross-flow filtering, dewatering sand screws, decanting centrifuges, hydrocy clones, etc.
  • salt-tailings concentrations in excess of 0.5 wt% and preferably no less than about 1% should be used to achieve reasonably fast consolidation of the solids in the tailings.
  • a degree of consolidation of the fines/sand mixture is obtained at polymer-tailings concentrations as low as 0.01 wt% for relatively short processing times, superior results are obtained at polymer-tailings concentrations of 0.05% and higher.
  • the top set of vials in Figure 4 shows results obtained by adding 5 g of a 2 wt% ammonium sulfate ((NH 4 ) 2 S0 4 ) solution containing PAM to 5 g of MFT. Sand was also added to give a sand-to- fines ratio of 1 : 1 (i.e., 1.5 g of sand was added). The amount of PAM in the solutions was varied between 0.1% (by weight) and 0.02% (by weight). The bottom set of vials show what is observed when a 1 wt% of the ammonium sulfate was used. The vials were centrifuged at 3000 rpm for 30 seconds to accelerate settling.
  • a 2 wt% ammonium sulfate ((NH 4 ) 2 S0 4 ) solution containing PAM
  • Sand was also added to give a sand-to- fines ratio of 1 : 1 (i.e., 1.5 g of sand was added).
  • Figure 4 was determined by drying, i.e., the centrifuged consolidated material was separated from its supernatant liquid, the wet mass weighed, dried and reweighed to determine a solids content.
  • the solids content of the consolidated materials for the sets of vials are summarized in Table 3.
  • Table 3 The solids content of centrifuged ammonium sulfate/PAM treated MFT as determined by separating and drying consolidated material.
  • Treating MFT with an equal weight of the (NH4) 2 S0 4 / polymer solutions resulted in a salt-tailings concentration of about 1 wt% for each of vials A4- E4, and for vial A4, a polymer-tailings concentration of about 0.05 wt% PAM, for vial B4 a polymer-tailings concentration of about 0.04 wt% PAM, for vial C4 a polymer-tailings concentration of about 0.03 wt% PAM, for vial D4 a polymer-tailings concentration of about 0.02 wt% PAM, and for vial E4 a polymer-tailings concentration of about 0.01% PAM.
  • the solids content was very variable, reflecting the problems with segregation of coarse and fine particles in the consolidated materials in these experiments.
  • solutions of seawater (sourced from the U.S. eastern shore of the Atlantic Ocean) were prepared with various concentrations of a nonionic polyacrylamide (available from SNF as FA920) between 0.1% (by weight) and 0,02% (by weight).
  • the concentration of highly soluble salts in the seawater is believed to be greater than 3 wt%.
  • the seawater-polymer solutions were used to treat MFT from oil sands processing.
  • An equal amount of seawater -polymer solution was used to treat MFT (about 5 g of seawater -polymer solution to about 5 g of MFT) in a vial.
  • the treated mixtures were first stirred and then the vials were centnfuged at 3000 rpm for 30 seconds to accelerate settling.
  • the results are shown in the picture of Figure 6. From left to right, the seawater used to treat the MFT included about 0.1 wt%, 0.08 wt%, 0.06 wt%, 0.04 wt% and 0.02 wt% of the polymer flocculant, respectively.

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CN113094880A (zh) * 2021-03-29 2021-07-09 广州中国科学院先进技术研究所 膜蒸馏物料浓缩动态能耗计算方法、电子设备及计算机可读存储介质
WO2021207564A1 (en) * 2020-04-09 2021-10-14 Extrakt Process Solutions, Llc Water management system for ore mining operation
CN114011589A (zh) * 2021-11-01 2022-02-08 安徽汉华工贸有限责任公司 基于二甲基二烯丙基氯化铵与聚丙烯酰胺煤泥水处理工艺
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