WO2008025088A1 - Coal flotation method - Google Patents
Coal flotation method Download PDFInfo
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- WO2008025088A1 WO2008025088A1 PCT/AU2007/001268 AU2007001268W WO2008025088A1 WO 2008025088 A1 WO2008025088 A1 WO 2008025088A1 AU 2007001268 W AU2007001268 W AU 2007001268W WO 2008025088 A1 WO2008025088 A1 WO 2008025088A1
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- WIPO (PCT)
- Prior art keywords
- stream
- flotation
- particles
- feed
- separator
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Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D1/00—Flotation
- B03D1/02—Froth-flotation processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
- B03B9/00—General arrangement of separating plant, e.g. flow sheets
- B03B9/005—General arrangement of separating plant, e.g. flow sheets specially adapted for coal
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D3/00—Differential sedimentation
- B03D3/02—Coagulation
- B03D3/04—Coagulation assisted by vibrations
Definitions
- the present invention relates to a method and apparatus for producing carbonaceous material which has an increased propensity to be separated in a flotation cell.
- Coal is an increasingly valuable resource due to its relative abundance and the depletion and loss of other natural energy resources such as petroleum, natural gas, oil shale and tar sands. As coal, along with other energy sources, has become more valuable, there has been a greater imperative to efficiently extract our available coal reserves.
- An important element of increasing the carbonaceous yield from coal deposits is to reduce the amount of carbonaceous material in the tailings stream of coal extraction plants.
- Froth flotation separation techniques are used to separate a slurry of particulate matter into a lighter hydrophobic portion and a heavier hydrophilic portion.
- air is introduced into the liquid slurry of particulate matter through a porous cell bottom or hollow impeller shaft, thereby producing a surface froth.
- a sparger device is used to form bubbles from shearing energy applied to input air.
- an apparatus for the separation of carbonaceous material from inorganic matter including:
- a first flotation cell for processing a feed stream of carbonaceous material to produce an overflow product stream and an underflow stream;
- a separation means for separating a further processing stream from the underflow stream; and a mechanical processing means for mechanically working the further processing stream to produce the flotation stream, the flotation stream providing a recycle stream for combination with the feedstream to the first flotation cell or a feed stream to a second flotation cell.
- the flotation cell typically includes a liquid and a means for creating the froth phase on which floats carbonaceous rich material up to the surface of the liquid.
- the over flow stream from the flotation cell includes carbonaceous rich material which is removed from the cell.
- An underflow stream includes material which could not be floated under the conditions in the flotation cell.
- the apparatus is advantageously used to process a carbonaceous material which contains material of a size, density and/or hydrophobicity distribution which is not conducive to efficient flotation cell processing (i.e. low carbon yield).
- Feed streams comprising carbonaceous matter may include material such as coal particulates in middlings streams from upstream separation operations.
- carbonaceous material from tailings dams may form the basis for the feed stream.
- the feed stream for the first flotation cell is derived from a source stream and is combined with the flotation stream and fed to the first flotation cell.
- the separation means which is preferably a sieve screen or other type of separator that separates particles on the basis of particle size, separates over size particles or particles larger than a particular size.
- These oversized particles constitute the further processing stream which are mechanically processed to reduce there size and then recycled as the flotation stream for combination with the feed stream to the first flotation cell.
- the l mechanically worked further processing stream is separated to remove undersized or fine particles prior to being recycled as the flotation stream.
- the underflow from the first flotation cell is separated to produce a further processing stream, as above which in turn is mechanically processed to reduce the particle size.
- the resulting flotation stream is passed to a second flotation cell to undergo a flotation process.
- the feed stream to the first flotation cell is derived from a source stream.
- the flotation conditions in the first flotation cell and the second flotation cell may be the same or different depending on the quality and nature of the coal to be recovered.
- the overflow from the second flotation cell may be combined with the overflow from the first flotation cell to form the product stream.
- the flotation cell will typically have an optimum particle size range for the transfer of hydrophobic carbonaceous material into the froth phase, with the size range being dependent upon the particle density.
- the mechanical processing means eg. grinding or attrition
- the mechanical processing means is able to reduce the large particles into the optimum particle size range, with the reduction in the particle size resulting in the liberation of inorganic material within the particles. With the liberation of the denser inorganic material, the proportion of lower density material (equating to cleaner coal) increases.
- Carbonaceous material such as coal
- excess fines eg. less than 75 ⁇ m
- this portion of the feed stream or underflow stream is preferably separated and mechanical processed to liberate inorganic material from the composite particles; reduce the particles to a more optimal particle size for flotation removal; and remove the hydrophilic outer layer from the coal to produce a more hydrophobic particle.
- the apparatus of the invention includes a separating means, prior to the mechanical processing means to separate a carbonaceous stream from a second separation means or the underflow stream by size and/or density to form a further processing stream.
- This step preferably removes the high ash content material and finer particle material that does not easily float.
- the flotation yield being the ratio of the mass of carbon in the outlet stream to the mass of carbon in the feed stream.
- the further processing stream which contains the oversize material is then mechanically processed.
- the stream preferably has a higher proportion of particles between 75 ⁇ m and 300 ⁇ m than the further processing stream. More preferably, the flotation stream has a higher proportion of particles between 100 ⁇ m and 250 ⁇ m than the underflow stream. The applicant has found that by mechanically working the particles in the further processing stream, the preferred particle range of the recycle stream may be achieved.
- the flotation stream is less dense than the tailing or underflow stream.
- the flotation stream preferably has a specific gravity of 1.25 to 2.4, more preferably 1.25 to 1.6 and most preferably 1.25 to 1.4.
- the apparatus may further include a density separating means to remove the denser particles from the flotation stream.
- the propensity of the material in the flotation stream to be transferred into the froth phase may also be enhanced through increasing the hydrophobic nature of the flotation stream.
- the rate of flotation of particles depends on their frequency of collision with bubbles and on the efficiencies of collision, attachment and stability between particles and bubbles. Most flotation machines produce maximum flotation for particles of optimum intermediate size with flotation decreasing for particle sizes each side of this optimum.
- the lower flotation of fine and coarser particles results mainly from their lower collision efficiency and lower stability efficiency (in the high turbulence of the flotation cell), respectively with bubbles.
- this maximum in flotation shifts to larger or smaller particle sizes for minerals of lower or higher density.
- the flotation of particles increases with the hydrophobicity of the mineral surface (increase in bubble-particle attachment efficiency). Coal is naturally hydrophobic.
- collectors such as surfactants or oil may be added to further increase this hydrophobicity, especially if the coal is oxidised which increases the number of hydrophilic surface hydroxide groups.
- the decrease in mineral hydrophobicity may also be the result of precipitation of metal hydroxides from solution on the mineral surface.
- Coating of the valuable minerals with hydrophilic gangue minerals such as silicates may also decrease surface hydrophobicity and therefore propensity of the particles to float.
- the mechanical processing means is used in the invention to not only reduce the particle size of the material to form the flotation stream but also remove the surface layer.
- a stirred mill may be used to remove the surface layer through grinding attrition. In the process particle surfaces are abraded by applying intense shear and frictional forces between the grinding elements and particles. Whereas stirred mills have been traditionally used to reduce particles below 40 ⁇ m, the applicant has found that a stirred mill may be used to decrease the particle size and enhance the hydrophobic nature of the oversize material in the recycle stream to produce particles within the preferred particle size range (75 ⁇ m to 300 ⁇ m).
- the mechanical processing means may include a grinder (eg. ball or rod mill) for reducing the mean particle size of the further processing stream and liberate inorganic ash material; and an attritioner for increasing the hydrophobic nature of the recycle stream.
- a grinder eg. ball or rod mill
- an attritioner for increasing the hydrophobic nature of the recycle stream.
- the mechanical processing means may include two stirred or tumble mills may operate in series.
- the first stirred mill is set up to attrition the hydrophilic surface layer and the second stirred mill set up to reduce the particle size of the underflow stream.
- the product of the first (and second) stirred mill(s) may be separated by size and or density, with the coarser material (> 300 ⁇ m) feed into the second stirred mill, and the ultra-fine ( ⁇ 75 ⁇ m) material feed into a tailings stream.
- the 75 ⁇ m to 300 ⁇ m fraction is fed into the flotation stream with its increased hydrophilic nature increasing its propensity to transfer into the froth phase and hence into the high carbonaceous product stream.
- the second stirred or tumble mill operates to reduce the particle size to within the preferred particle size distribution.
- Preferably at least 80% of the output of the second stirred mill has a particle size of less than 300 ⁇ m.
- the output of the second mill is also fed into the recycle stream with its enhanced particle and density distribution increasing its propensity to transfer into the froth phase and hence into the high carbonaceous product stream.
- the process parameters e.g. solids volume concentration, grinding media/particle ratio, specific energy input, circumferential speed and grinding media filling ratio
- one stirred mill may be set up to maximise the flotation yield through both attrition and comminution of the oversized material in the underflow stream.
- the process parameters of the stirred mill are such that ultra-fine particulate production is minimised.
- the net weight proportion of ultra-fine particles after mechanical processing is less than 30%, more preferably, less than 25%, even more preferably less than 20%.
- the mechanical processing means may also be applied to other underflow, tailing or waste streams, such that the processed tailings may feed into the flotation tank.
- the tailings from gravity and/or size separators eg. screens, teetered bed separators or spirals
- an apparatus for the separation of carbonaceous material including
- a first flotation cell for processing a feed stream of carbonaceous material
- a separation means for separating a source stream into an undersize stream for flotation and a further processing stream
- a mechanical processing means for processing the further processing stream to produce a flotation stream, wherein the flotation stream is combined with the undersize stream for flotation from the separation means to provide the feedstream to the first flotation cell.
- the separator or separation means maybe at least a first separator and a second separator.
- the source stream which may have been subjected to earlier processing or separation is provided to the second separator.
- the further processing stream is preferably the middlings stream from the first separator which is mechanically processed in the mechanical processing means to form the flotation stream.
- the flotation stream is then fed with the undersized material from the second separator into the first flotation cell.
- the overflow from the first flotation cell is then added to the product stream.
- the underflow stream may be combined with the tailings stream.
- the feed stream preferably includes the underflow stream of a flotation cell.
- a method for attritioning/grinding a feed stream including the steps of:
- the low ash portion in comparison to the feed stream, has at least one characteristic selected from group consisting of :
- the target particle size range is preferably 63 ⁇ m to 500 ⁇ m, more preferably 75 ⁇ m to 500 ⁇ m, more preferably 63 ⁇ m to 300 ⁇ m and even more preferably 75 ⁇ m to 300 ⁇ m.
- FIGS. 1a to 1d are schematic diagrams of various flotation methods for recovering carbonaceous material in accordance to several embodiments of the present invention.
- Figure 2 is a graph of the partition number versus particle size of carbonaceous material for a conventional flotation cell.
- Figure 3 is a graph of the regrinding sizing results for different grinding times and grinding media using the stirred mill of Figure 3a & b.
- Figure 4 is a graph comparing the cumulative yield (%) versus the cumulative ash (%) for unground and ground material from the flotation underflow stream.
- Figure 5 is a particle size distribution of a flotation feed sample and a particle size distribution of a flotation feed sample subjected to sonication for 1 minute.
- Figure 6 is a backscattered electron image of a carbonaceous sample from the flotation feed sample of Figure 6.
- Figure 7 is a graph of the flotation concentrates and tail fractions of the flotation feed sample of Figure 6.
- Figure 8 is a graph of the flotation concentrates and tail fractions of the flotation feed sample subjected to sonication for 1 minute of Figure 6.
- Figure 9 is a table summarising the testwork results in Example 3.
- Figure 10 is a graph of the size distribution of coal tailings after milling after milling with balls, pebbles or rods.
- Figure 11 is a graph of the size distribution of coal tailing after milling with cycles or balls.
- the flotation process of one embodiment of the present invention includes a first flotation cell 10.
- the flotation cell may be one of a variety of mechanically agitated and/or microbubble flotation cells available, including the "Microcel" tall vessel column in which air is admitted separately from the feed. Alternatively, 'shallow columns', with short retention times, in which air is admitted with the feed, such as the Jameson and Ekof type columns, may also be used.
- the feed stream typically comprises a mixture of carbonaceous and composite carbonaceous/inorganic material from upstream separation processes such as spirals, teetered bed separators, reflux classifiers, coarse rejects and even the reprocessing of tailings from tailing dams.
- the carbonaceous material is subjected to a flotation process resulting in an overflow stream 11 and an underflow 12.
- the underflow which typically contain lumps of carbonaceous material higher in ash or otherwise denser than the material which floated is passed to a size separator 13 such as sieve screens where fine material 14, 15 removed to a tailings stream 15.
- the oversize material which forms the further processing stream 16 is passed to a mechanical processing means which in this case is a stirred mill 17 where the material is size reduced made more suitable for flotation.
- the fine fraction of the mechanically processed material is removed in a size separator or the density separator and the flotation stream 19 combined with the feedstream 9 and fed into the first flotation cell 10.
- a feedstream 21 is fed into the first flotation cell 20.
- the underflow 22 is fed to a size separator 23 separates oversized material for further processing 24 and undersized material passes to a tailings stream.
- the further processing stream 24 is fed to a mechanical processing device which is an attrition/milling device 25 before being fed as flotation stream 26 to a second flotation cell 27 where a concentrate 28 is floated and the underflow sent to tailings. This concentrate 28 is combined with overflow 29 from the first flotation cell 20 to produce the product stream.
- Figure 1c is similar to that of Figure 1c? except the underflow 31 from first flotation cell 30 being separated in separator 32 and further processed stream 33 is fed to mechanical processing means 33.
- mechanical processing means is an attrition milling device 34.
- the flotation stream 35 is fed directly back to be combined with feed stream.36 to the first flotation cell 30.
- Figure 1d relates to a process configuration in which a middlings stream is mechanically worked, with the product of the mechanical working forming part of the feed stream to the first.
- a series of separators 41 , 42, 43 separate a feed stream by size.
- the primary separator produces an undersize stream 44 which is fed to a second separator 42.
- the second separator produces an undersize fraction 45 which is fed to the first flotation cell 40.
- the oversize fraction 46 from the second separator 42 is fed to a third separator 43 which produces a middling fraction 47, a product fraction 48 and a purge stream 49.
- the middling stream 47 is passed to a mechanical processing means which is an attrition milling device 50 to produce the flotation stream 51.
- the flotation stream is added with the undersize feed stream 45 to the flotation cell 40 to undergo a flotation process.
- the product stream 52 is taken off as the overflow and the underflow is sent to tailings.
- an optimal particle size range for a conventional flotation cell is in the range of 63 ⁇ m to 300 ⁇ m.
- a mechanical processing means and the flotation stream a wider range of particle sizes may be effectively processed by the flotation cell.
- larger particle sizes of up to 500 ⁇ m or above may be effectively processed, with the relatively low recovery rate of carbonaceous material during the first pass through the flotation cell compensated by higher recovery rates of the mechanically processed material fed into the flotation cell from the flotation stream.
- the underflow stream may include a separation means before and/or after the mechanical processing means, to enable the preferred particle size and/or density distribution to enter the mechanical processing means and/or the downstream flotation stream.
- the separation means may include spirals, teetered bed separators, reflux classifiers and may also include a preceding classification stage (eg. cyclone).
- the preferred particle size range is between 63 ⁇ m to 300 ⁇ m, with a density range corresponding to the cleaner coal fractions ( Figure 2).
- Clean coal has been classified as particles having a relative density range or specific gravity of 1.25 to 1.4, semi-clean coal 1.4 to 1.6, bony coal 1.6 to 2.4 and mineral stone > 2.4.
- Reagents are added to the flotation cell to aid the particles to more readily float (collectors) and to create the froth phase which keeps the floated particles suspended on the top of the flotation medium, thus allowing these particulates to be removed in the outlet (high carbonaceous material).
- Collector reagents are typically oil based products such as diesel.
- the coal which is lipophilic attaches to the surface of the oil droplets and floats upwardly along with the oil droplet utilising their buoyancy and hydrophilic nature.
- the mechanical reprocessing of the underflow material or material of a particular size increases the hydrophobic nature of coal coated with a hydrophilic outer layer (eg. oxidised organic material or inorganic material, such as clay).
- a hydrophilic outer layer eg. oxidised organic material or inorganic material, such as clay.
- the mechanical processing means is preferably a stirred or tumble mill, although other grinding/crushing equipment (eg. fluidised bed or high pressure griding rolls) may be used.
- a benefit of the stirred or tumble mill is that it grinds/attritions the coal particles under a liquid environment, thus minimising the extent of oxidation of the coal particle's surface.
- the re-oxidation of the coal's surface will increase the coal's affinity to water and hence lead to lower separation efficiency of the flotation cell.
- the cooling effect of the liquid eg. water medium
- the combination of a non- oxidising milling environment and short lag time ensures the hydrophobicity of the coal particles in the flotation steam is maximised.
- the fluid media may also include a gaseous fluid, such as carbon dioxide or other non- oxidising gas.
- a gaseous fluid such as carbon dioxide or other non- oxidising gas.
- carbon dioxide may be particularly advantageous when a fluidised bed is used to attrition/grind the underflow stream.
- the attrition process involves the collision of particles which result in shear and frictional stresses between the colliding particles.
- crushing or grinding forces reduce the particle size through multiple fractures in the particle due to the higher compressive forces applied to the particle.
- Attrition may be advantageously employed to not only remove the fine impurity layer on the coal surface, but to fracture the particle along a weakened stress line. These weakened stress lines are more likely to coincide with the interface to inorganic matter. Therefore, the use of attrition may effectively liberate inorganic ash impurities. Also, as particle size reduction is able to occur with more gentle forces (lower energy costs), less fines are produced and hence greater carbonaceous yields may be achieved.
- the stirred mill may be used to increase the propensity of the carbonaceous material to be transferred into the froth phase by:
- the relative size distribution of the grinding/attrition media to the feed of the stirred or tumble mill is an important parameter to control. If a cleaning process is required, then the particle size distribution is preferably similar to the particle's size distribution of the carbonaceous material. Similarly, if a particle size reduction process is required the mean size of the grinding media is preferably increased.
- the attritioning media are the particulates from the underflow stream, the collisions of the carbonaceous material able to clean their own surfaces and reduce the mean particle size of the underflow stream.
- a stirred mill was developed to grind the samples of middling material.
- Crushed river rock was used as the grinding media in the mill.
- the river rock was screened to give approximately 1mm to 4.75mm and 4.75mm to 8mm size fractions. Combinations of these two fractions were used in several grinding tests to investigate the effect of media size and grinding time. Results from these tests are detailed in Figure 3.
- the grinding procedure involved placing a proportion of the river rock and required water in the mill container, turning on the stirrer then adding the middling sample, remainder of the water and enough river rock to give the surface of the grinding mass the appearance of a donut.
- Typical river rock charge was about 80Og, water about 200ml and middlings mass around about 20Og.
- the mixed media charge had the largest effect on coarse particle size reduction so this charge was used for subsequent flotation work.
- Results for the flotation testwork are detailed in Figure 4. Three lots of approximately 20Og (wet) were re-ground using the mixed media charge and a grind time of approximately 30s to produce approximately 50Og (dry) for a flotation test.
- the flotation cell size was 5L so 50Og of material was required to give approximately 10% solids in the flotation cell.
- the 100% cumulative yield sample points represents the quality of the feed material used in the flotation test.
- the flotation test procedure consisted of adding the middlings material to the flotation cell, adding enough tap water to fill the cell to 5L, conditioning for one minute with the impeller on, adding frother (eg. methyl iso-butyl carbinol (MIBC)) and conditioning for 30s then adding collector (eg. diesel) and conditioning for one minute before turning the air on. Timed concentrates were collected for 10s, 40s, 3min and 10min to enable yield- ash curves to be generated.
- frother eg. methyl iso-butyl carbinol (MIBC)
- collector eg. diesel
- Example 2 Samples (PD3X) from the flotation feed stream were assessed for the affect of 1 minute of sonication (sound wave energy which is defined for the purposes of this invention as being a subset of mechanical processing) on flotation performance. As illustrated in Figure 5, the sample subjected to sonication of 1 minute had an increased fines level. As illustrated in Figure 6, a portion of the coal particles are covered with clay particles. The introduction of sound wave energy to vibrate (mechanical processing) the clay particles free from the coal particles has resulted in an increase in particle sizes below 5 ⁇ m.
- 1 minute of sonication sound wave energy which is defined for the purposes of this invention as being a subset of mechanical processing
- the proportion of higher particle size material in the underflow stream from the untreated sample indicates that there would be benefits in removing the hydrophilic layer from the underflow stream and recycling this material into the flotation cell feed.
- Tests were performed to evaluate the suitability of using tumbling or stirred mills to effectively reduce the size of coal tailing particulates to between 75 ⁇ m to 300 ⁇ m, without an excessive increase in ultra-fine material ( ⁇ 75 ⁇ m).
- the feed material had an ultra-fine ( ⁇ 75 ⁇ m content of 1 % (2.8% in second campaign), with 80wt% of the particles being 702 ⁇ m or less (662 ⁇ m in second campaign).
- the largest feed material was about 1.5mm, with about 99 wt% of the feed material being 1mm or less.
- Figure 9 is a table which summarises the results of the testwork. Effect of grinding media
- the shape and the density of the grinding media may have an effect on the coal tailings grinding performance. Pebbles are advantageous over steel balls in coal grinding due to their lower density and therefore, reduced breakage force. A lower breakage force is considered to produce fewer fines.
- the density of the steel balls are 7.8-8 grams/cm 3 compared to a density of pebbles of about 2.5 grams/cm 3 . Therefore, to avoid excessive fines formation, the density of the griding media is preferably no greater than 3 grams/cm 3 and more preferably no greater than 2.5 grams/cm 3 .
- the ratio of the griding media size to the P80 size is preferably at least 10 and more preferably at least 20.
- stream encompasses continuous, non-continuous, solids, semi-solids, slurries, gases and any other solid / liquid / gas mixture.
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Abstract
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Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
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AU2007291959A AU2007291959A1 (en) | 2006-08-30 | 2007-08-30 | Coal flotation method |
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AU2006904725 | 2006-08-30 | ||
AU2006904725A AU2006904725A0 (en) | 2006-08-30 | Coal flotation method |
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Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2009026612A1 (en) * | 2007-08-28 | 2009-03-05 | Xstrata Technology Pty Ltd | Method for improving flotation cell performance |
CN103240168A (en) * | 2013-05-08 | 2013-08-14 | 中国矿业大学 | Grading separation and dehydration method for high-ash difficult-separation coal slime |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0057577B1 (en) * | 1981-01-29 | 1986-05-07 | The Standard Oil Company | Method for the beneficiation, liquefaction and recovery of coal and other solid carbonaceous materials and beneficiated coal products |
EP0066066B1 (en) * | 1981-05-28 | 1987-08-05 | The Standard Oil Company | Beneficiated coal, coal mixtures and processes for the production thereof and an arrangement for producing a beneficiated coal product |
US4828686A (en) * | 1987-06-05 | 1989-05-09 | University Of Utah | Chemical conditioning of fine coal for improved flotation and pyrite rejection |
-
2007
- 2007-08-30 WO PCT/AU2007/001268 patent/WO2008025088A1/en active Application Filing
- 2007-08-30 AU AU2007291959A patent/AU2007291959A1/en not_active Abandoned
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0057577B1 (en) * | 1981-01-29 | 1986-05-07 | The Standard Oil Company | Method for the beneficiation, liquefaction and recovery of coal and other solid carbonaceous materials and beneficiated coal products |
EP0066066B1 (en) * | 1981-05-28 | 1987-08-05 | The Standard Oil Company | Beneficiated coal, coal mixtures and processes for the production thereof and an arrangement for producing a beneficiated coal product |
US4828686A (en) * | 1987-06-05 | 1989-05-09 | University Of Utah | Chemical conditioning of fine coal for improved flotation and pyrite rejection |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2009026612A1 (en) * | 2007-08-28 | 2009-03-05 | Xstrata Technology Pty Ltd | Method for improving flotation cell performance |
AU2008291673B2 (en) * | 2007-08-28 | 2012-07-19 | Xstrata Technology Pty Ltd | Method for improving flotation cell performance |
US8881911B2 (en) | 2007-08-28 | 2014-11-11 | Xstrata Technology Pty Ltd. | Method for improving flotation cell performance |
CN103240168A (en) * | 2013-05-08 | 2013-08-14 | 中国矿业大学 | Grading separation and dehydration method for high-ash difficult-separation coal slime |
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