EP1066114A4 - Production et recuperation commandees d'agglomerats de fines de charbon - Google Patents

Production et recuperation commandees d'agglomerats de fines de charbon

Info

Publication number
EP1066114A4
EP1066114A4 EP98952419A EP98952419A EP1066114A4 EP 1066114 A4 EP1066114 A4 EP 1066114A4 EP 98952419 A EP98952419 A EP 98952419A EP 98952419 A EP98952419 A EP 98952419A EP 1066114 A4 EP1066114 A4 EP 1066114A4
Authority
EP
European Patent Office
Prior art keywords
slurry
coal
oil
water
process according
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP98952419A
Other languages
German (de)
English (en)
Other versions
EP1066114A1 (fr
Inventor
Ian Clarence Hoare
James Clifton Donnelly
Allan Bruce Waugh
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
SELECTIVE OIL AGGLOMERATION PROCESS Pty Ltd
SELECTIVE OIL AGGLOMERATION PR
Original Assignee
SELECTIVE OIL AGGLOMERATION PROCESS Pty Ltd
SELECTIVE OIL AGGLOMERATION PR
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from AUPP0145A external-priority patent/AUPP014597A0/en
Priority claimed from AUPP5186A external-priority patent/AUPP518698A0/en
Application filed by SELECTIVE OIL AGGLOMERATION PROCESS Pty Ltd, SELECTIVE OIL AGGLOMERATION PR filed Critical SELECTIVE OIL AGGLOMERATION PROCESS Pty Ltd
Publication of EP1066114A1 publication Critical patent/EP1066114A1/fr
Publication of EP1066114A4 publication Critical patent/EP1066114A4/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/01—Separation of suspended solid particles from liquids by sedimentation using flocculating agents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/24—Feed or discharge mechanisms for settling tanks
    • B01D21/2405—Feed mechanisms for settling tanks
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/30—Control equipment
    • B01D21/302—Active control mechanisms with external energy, e.g. with solenoid valve
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/30—Control equipment
    • B01D21/32—Density control of clear liquid or sediment, e.g. optical control ; Control of physical properties
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/30—Control equipment
    • B01D21/34—Controlling the feed distribution; Controlling the liquid level ; Control of process parameters
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/26—Separation of sediment aided by centrifugal force or centripetal force
    • B01D21/262—Separation of sediment aided by centrifugal force or centripetal force by using a centrifuge
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/26—Separation of sediment aided by centrifugal force or centripetal force
    • B01D21/267—Separation of sediment aided by centrifugal force or centripetal force by using a cyclone

Definitions

  • the present invention relates to a process for recovery of fine coal agglomerates and more particularly relates to a process for recovery of such agglomerates utilising a
  • control system including means to monitor the concentration of fine coal in a coal/water/mineral slurry to facilitate controlled delivery of an optimum quantity of an agglomeration agent such as an oil based emulsion used in the recovery process thereby preventing over use of the agent and obviating the need for agglomeration agent recovery as a result of its over use.
  • an agglomeration agent such as an oil based emulsion used in the recovery process
  • coal agglomerates are separated from the mineral matter by screening, filtration or flotation.
  • the process flow demonstrate the simplicity of the design
  • the semi-commercial plant treated feed material in which the average feed ash ran at about 40% Oil was added in the form of an emulsion produced by using an ultrasonic sound
  • This material when treated with oil at an addition rate of 7- 8%> (dry feed basis) produced an agglomerated product of 79% ash at a yield representing 60% of the feed
  • the agglomerated product was amenable to handling and has been stockpiled for periods of 8 months without oxidation
  • the tailing ash was typically in the 80-85 % range and settled rapidly to produce an extremely clear supematant liquid in contrast to the feed material which settled slowly and left a stable grey layer in the supematant liquid
  • This process did not however, include a system for the controlled feeding rate of oil emulsion determined by measurement of coal concentration in the coal/waste slurry.
  • Aglofloat process is an advanced spherical agglomeration and flotation process
  • a first run-of-mine coal is crushed to pass 600 ⁇ m and slurried with re-cycled water
  • Crude oil is mixed with diesel fuel to form a bridging oil
  • the coal slurry and bridging oil are then combined in a high shear mixer where coal and oil form micro- agglomerates about 212 ⁇ m in size
  • the micro-agglomerates are separated from coal mineral matter and refuse in a flotation cell, and then washed and separated from
  • agglomerates are enlarged to about 850-335 ⁇ m
  • hydroseparator is removed and discarded as plant reject
  • the process is capable of beneficiating high-ash and high-sulphur bituminous coals An Illinois No 6 coal with
  • FIG. 2 uses heptane selectively to agglomerate hydrophobic organic coal
  • based asphalt binder is subsequently added toassist in enlarging product agglomerates to more manageable 6 4mm to 9 5mm spherical pellets H ⁇ drophilic inorganic ash-forming and pyritic sulphur mineral matter is rejected, leaving a virtualh coal-free refuse
  • the agglomerated coal product is then stripped of the heptane bridging liquid b ⁇ contact with steam Steam stripping is used to recover the heptane because heptane and steam form an azcotrope which has a boiling point (79 20C) lower than either heptane or watci alone (98'C and lOO'C.
  • the present invention in one form seeks to ameliorate the problems of the know n processes examples of which arc described above providing a process for the ⁇ eco ⁇ e ⁇ of fine coal agglomerates utilising a s ⁇ stcm for accuratch controlling deliver) of an agglomerating agent such as an oil emulsion responsive to measurement of parameters of a coal/water/mincial slum to prevent over use of and the need to recover that agent
  • an agglomerating agent such as an oil emulsion responsive to measurement of parameters of a coal/water/mincial slum to prevent over use of and the need to recover that agent
  • the present invention further piovides an economic coal recovers process utilising an agglomerating agent such as low cost oils and a laser cut screen for separating the coal agglomerates and also comprising probes which monitor condition parameters of a coal/w ater/mincral slum to thercb) control the addition of those oils
  • the invention further a nuclear monitoring s ⁇ stem for determining the actual amount of coal in the coal/water/mineral slum mixture and computer control of the agglomerating agent quant ⁇ t ⁇ required for rccove ⁇ , of fine coal from the mixture
  • a first probe will measure the total solids and a second piobc the quantity of dirt In a t ⁇ p ⁇ cal slum there might be 20-30% solids and 70-80% is fine coal, alternative!) there might be 2%-50% solids of which 5%-60%of said solids is mineral matter
  • all of the agglomerating agent ill be used, obviating the need for the added step of oil recover)' as occurred in certain of the prior art processes
  • the oil consumption rate according to the process of the invention has been leduced to a level such that oil recover)' is not nccessarv to achieve commercial viabiht) of the process
  • Selective oil agglomeration according to the present invention includes the following advantages over com entional froth flotation for the economic recover) of fine coal a) thickener underflow slum as feed can be used with solids concentration of 15-30% weight compared to 5 - 10% for froth flotation, thus, volumetric feed
  • the present invention comprises, a process for the separation of
  • said first reservoir from an infeed line, a second reservoir for receiving and holding an emulsion comprising an oil, water
  • a pump operably connected to said second reservoir
  • first and second reservoirs are in communication with a mixing tank which receives said coal/water/mineral slurry from said first reservoir and said oil emulsion from said second reservoir,
  • a primary separator in communication with said mixing tank, and a vibrating screen separator in communication with said primary separator and/or the high shear mixing tank, the process further comprising,control means in communication with at least one sensor in said first reservoir, and said pump in communication with said second
  • control means also in communication with said coal/water/mineral
  • control means controlling said pump responsive to a signal/s
  • control means comprises a computer processor programmed to receive signals from said sensor/s which preferabh comprise probes immersed in said coal/water/mincral slum and which detect the concentration of coal fines whereupon said processor actuates the pump on said second reservoir responsive to data determined bv said piobes relating to the condition of the slum facilitate feeding into said mixing tank of a predetermined amount of emulsion from said second rcscn oir
  • slurn from said first reservoir is delucred to a mixci b) means of a pump or an overflow conduit
  • the present invention comprises, a process for separation of fine coal from a coal/water/mineral slurn .
  • the process comprising an infeed line which delivers a coal/water/mincral slurn into a fust lescivou .
  • a second reservoir for icceiung and holding an oil emulsion and including a deliver) pump m communication therewith.
  • a mixing reservoir in/communication with said first and second reservoirs, control means including at least one sensing probe in contact with said coal/watcr/mmcial slum foi monitoring parameters of said coal/water/mincral slum whilst in said infeed line and/or in said first reservoir.
  • control means controls the deliver) of said oil emulsion via said pump to said mixing rcseivoir responsive to measurement of the parameters, including the concentration of fine coal of the coal/watcr/mineral slur in the first reservoir said pioccss thercb * s obviating the need for oil recover)
  • the present invention comprises. an oil agglomeration process for separation of fine coal from a coal/watcr/mmeral slum using an agglomerating agent such as an oil emulsion characteiised in that the process includes computerised control mcanswhich controls the deliver) of said oil emulsion from an oil emulsion holding tank to a feed holding tank holding said coal/water/mincral slurn at a rate determined by measured parameters of said coal/w atcr/mincral slum, thereb) preventing over use of said agent in said process and obviating the ncedfor agent recover)
  • an oil agglomeration process for separation of fine coal from a coal/watcr/mmeral slum using an agglomerating agent such as an oil emulsion characteiised in that the process includes computerised control mcanswhich controls the deliver) of said oil emulsion from an oil emulsion holding tank to a feed holding tank holding said
  • the present invention comprises, an oil agglomeration process for the separation and recovery of fine coal agglomerates from a slurry, the process including
  • sensing means in direct or indirect communication with said slurry for detecting predetermined parameters relating to the condition of said slurry, means in communication with the sensing means responsive to an instantaneous
  • condition parameters so as to minimise use of the agglomerating agent but maximise fine coal recovery for a predetermined quantity of
  • the process including a slurry from which fine coal is to be recovered, sensing means for detecting predetermined parameters relating to the condition of said
  • At least one signal processing assembly responsive to a reading of said parameters in direct
  • said signal processing assembly for controlling/regulating the delivery of an agglomerating agent into the slurry at a rate or in a quantity determined by said
  • condition parameters so as to minimise use of the agglomerating agent but maximise
  • a control system for regulating the coal slurry feed rate and solids concentration in an agglomeration process for the recovery of fine coal from said slurry comprising, a central processor, at least one remote sensor for measuring the condition parameters or ingredients of said coal/water/mineral slurry, means linking said remote sensor/s to said central processor for transmission to said central processor of data measured by said at least one sensor, means connecting the central processor to a variable speed pump which regulates the delivery rate of an agglomerating agent to a coal slurry reservoir prior to a mixing tank
  • a control system for regulating the delivery of an agglomerating agent into a coal/water/mineralslurry in an oil agglomeration process for the recovery of fine coal from said slurry, the control system comprising, a central processor, at least one remote sensor for measuring the condition parameters or ingredients of said coal/water/mineral slurry, means linking said remote sensor/s to said central processor for transmission to said central processor of data relating to the condition of
  • An assembly for controlling the delivery of an agglomerating agent to a slurry from which fine coal is to be recovered comprising, at least one probe in contact with said slurry, a signal processing unit in communication with said at least one probe and which receives and processes data from said at least one piobe i elating to the condition of said slurry,
  • PLC programmable logic computer
  • said pump is responsive to an input from said PLC thereby
  • the present invention comprises, a control sv stem for regulating the deliver) of an oil emulsion into a coal/water/mincral slurn in an oil agglomeration process for the recover) of fine coal the s ⁇ stctn comprising, a central processor. at least one remote sensor for measuring the condition and/oi constituents of said coal/water/mincral slum .
  • control means comprises a computer processorand a programmable logic computer each instructed b) software which processes data recen ed from a first sensing probe or probes in an infeed line which delivers the coal/water/mincral slurn and at least a second piobe in a feed holding tank foi said coal/w atei /mineral shu .
  • the programmable logic computer regulates the deliver) of the oil emulsion b) actuating a variable drive deliver) pump attached to or remote from said oil emulsion holding tank according to measured parameters of said coal/water/mincral slurn The measured parameters of the coal/w ater/mmeral slurn which control the actnit)
  • a mixing tank including at least one high shear agitator. substantial!) vertical baffles, an air distributor, an inlet and an outlet. wherein said baffles create an optimum level of turbulence to maximise contact between coal particles and oil droplets resulting in oil coating of the particles
  • the high shear agitators have a geometry which facilitates a combination of axial and radial flow to allow optimum mixing within the tank whilst maintaining sufficient residence time and high shear to achieve coal-oil interaction
  • the present invention comprises a filter for separating bulk liquid and minerals from coal having an aperture of between 200 - 50 ⁇ m with open area between 10% - 20%
  • Figure 1 shows schematic layout of a control assembly including probes linked to a signal processing computer and a PLC
  • Figure 2 shows an analysis graph of Solids versus Time
  • Figure 3 shows a schematic layout of a selective oil agglomeration coal recovery process according to a preferred embodiment of the invention
  • Figure 4 shows a table of typical data produced by a run carried out on the pilot plant referred in figure 3 ,
  • Figure 5 shows a summary of results from an oil agglomeration coal recovery plant
  • This system includes a recovery process for reuse of heptane mixed with the coal agglomerates in the agglomeration circuit.
  • This arrangement does not however teach the controlled injection of an emulsion obviating the need for an oil recovery process to ensure economic viability.
  • Such a system will now be described with reference to figure 1.
  • FIG 1 there is shown a general schematic layout of a control assembly for use in controlling the recovery of fine coal from a slurry.
  • Control assembly 1 comprises an infeed pipe 2 which delivers a slurry containing water, fine coal and other mineral matter to a holding tank 3.
  • tank 3 includes a receiving reservoir
  • Tank 3 includes a discharge assembly which comprises a delivery pipe 7 and control valve 8 which regulates delivery of the slurry to the agglomeration process .
  • Overflow reservoir 5 includes overflow pipe 9 which joins delivery pipe 7.
  • Tank 3 has a wall 3a which is designed to maintain slurry level above the probe detecting areas.
  • Control assembly 1 futher comprises probes 10 and 1 1 each sealed within a housing which are used to determine the ash content of the slurry.
  • Probe 1 1 measures a density parameter of the slurry and probe 10 the mineral content. The probes allow on line determination of the ash of the slurry and subsequent continuous and instantaneous determinationof the coal content of the feed.
  • the probes are in communication with a personal computer based signal processing unit 12 which receives and processes data from the probes relating to condition parameters of the slurry.
  • Signal processing unit 12 is linked to a programmable logic computer (PLC) 13 which itself is in communication with a density guage 14 via interface 13a and flow meter 15 via interface 13b located in feed pipe 2.
  • PLC programmable logic computer
  • An output of counts per second is sent to unit 12 (which could include a 486 chip processor or higher ) whereupon its software determines the solids data for the slurry
  • PLC 13 receives data regarding the slurry and responsive to condition parameters of the slurry operates pump 16 which is driven by variable speed drive motor 17 thereby controlling delivery of an agglomerating agent such as an oil emulsion in the agglomeration process for fine coal recovery.
  • the agglomerating agent may also comprise oil only or a mixture of oil and water with additives to enhance dispersion of oil in water.
  • the oil must be capable of being finely dispersed in water and this is generally more difficult without surfactants in oils of increasing viscosity.
  • Most mineral oils derived from the oil refining process would be suitable, typically ranging from light oils such as dieseline to heavy fuel oils such as fractionator bottoms and reprocessed waste mineral oils. Vegetable oils could also be used. Energy sources and receivers of the probes are sealed within a housing (not shown ) immersed in the slurry.
  • probes used may be a Cs density probe and a
  • Density probe 1 1 which provides a determination of solids and has a source that generates a gamma ray through the slurry to a receiver to determine the slurry density
  • Probe 10 uses a plutonium source to generate X-rays into
  • the density is determined by passing the slurry across the path of the gamma ray and the mineral content is determined by generating X-rays through a window into the
  • the probes are calibrated they continuously and instantaneously monitor in that signals are continuously delivered to the signal processing unit for analysis
  • Counts per second values obtained are sent to processing unit 12 for analysis and thus determination of ash content
  • An algorithm in the associated software determines oil or emulsion requirements based on coal content
  • the variable drive motor 17 is then instructed to allow supply of oil or emulsion by the dosing pump at a prescribed rate
  • the accuracy of the probe processing depends upon measuring the same slurry at the same time i e close together
  • probes may be installed in a feed box a feed tank or sampling loop
  • probes may be installed in a sampling loop on the Selective Oil Agglomeration Process (SOAP) reject stream to continuously measure the processrecovery rates
  • SOAP Selective Oil Agglomeration Process
  • the PLC interacting systems include in the associated software specifically designed algorithms to, convert the density and mineral content probe signals to ash content of the slurry and then, convert ash content to mass of carbonaceous material in the slurry and then , determine the coal mass and flow rate which is then used to determine the required mass flow of agglomerating agent which as a consequence, signals the appropriate speed to run the agglomerating agent variable speed pump motor
  • FIG 2 there is shown a graph of Solids versus Time
  • the analyser probes provide an instantaneous readout of kilograms of coal, kilograms of mineral and kilograms of total solids
  • the data presented in the graph was collected over an 18 hour operating period of the SOAP plant in May 1998
  • the output from the probes is interpolated by a computer algorithm, which is used to control the on line addition of oil or an oil/water emulsion to a coal slurry
  • Oil pump rate responds via a variable frequency drive to the changes in coal content of the slurry, on a continuous basis, providing an accurately controlled correct addition to the slurry
  • the probes are preferably installed in a large heavy guage steel containment vessel that is used as the slurry feed reservoir 3
  • Output signals from the density and X-ray probes are sent to the computer via two interfaced cards that control pulse height, pulse shape position and amplification
  • the computer can display such information as the
  • FIG 3 there is shown a general schematic layout of a process for recovery of fine coal agglomerates according to a preferred embodiment of the invention
  • the process requires a source of slurry from which fine coal is to be extracted
  • the slurry is held in thickener tank 30 which includes slurry discharge line 3 1 in communication with pump 32 which itself is in communication with an infeed line 33 which terminates at feed holding tank 34.
  • Infeed line 33 includes a flow meter (not shown) as previously described with reference to figure 1 and delivers a coal/water/mineral slurry into feed holding tank 34.
  • Holding tank 34 includes a discharge or overflow 34a which takes any overflow to tailings sump 46.
  • the coal water slurry inside feed holding tank 34 is delivered via feed pump 35 to a high shear mixer 38.
  • Feed line 36 downstream of pump 35 includes in line mixer 37.
  • the process further comprises emulsion mixer 40 which receives a mixture of oil, water and surfactant to form an oil based emulsion.
  • Emulsion mixer 40 further comprises feed line 41 terminating at pump 42. Pump 42 is joined on its downstream side delivery line 43 enabling communication between emulsion mixing tank 40 and high shear mixer 38.
  • the process further comprises a signal processing computer 50 which is directly or indirectly linked to at least feed holding tank 34 via probes 54 &
  • PLC Computer 50 includes an interface 57 and 58 allowing signal communication with a flow meter and density guage in feed line 33 as the coal/water/mineral slurry travels therealong. This enables the computer to meter the flow rate of the coal/water/mineral slurry which is infed into feed holding tank 34.
  • Computer 50 comprises interfaces 52 and 53 which terminate in probes 54 and
  • Measuring gauges are used to measure the quantity of coal fines in the coal/water/mineral slurry in feed holding tank
  • the state of the slurry is converted to a signal which inputs into the computer 50 which controls a loop to adjust the flow emanating from pump 42 via interface 56.
  • the quantity and /or flow of emulsion delivered from tank 40 may be controlled so that an appropriate amount of emulsion to achieve maximum coal recovery without wastage is delivered to high shear mixer 38.
  • the probes used in this process are commercially available but have not previously been used in combination in the above described manner in fine coal recovery to effect controlled delivery of an oil emulsion.
  • Pump 42 is preferably variable drive so that its speed can be adjusted according to the predetermined amount of oil required in high shear mixer 38 in response to readings received by computer 50.
  • coal/water/mineral slurry and emulsion from emulsion mixing tank 40 are mixed in high shear mixing tank 38 by means of special agitator 38a including baffles (not shown).
  • the coal/water/emulsion mixer is allowed to agglomerate whereupon the agglomerated fines gravitate into primary separator 39.
  • Computer 50 is instructed by software which actuates the emulsion pump 42 to deliver the required dose of emulsion into the high shear mixer 38 as the coal/water/mineral slurry is continually infed. Flow of the coal/water/mineral slurry is monitored using a standard flow meter gauge located near the entry to the feed holding tank which is electronically linked to the computer 50.
  • the blend of emulsion/coal/water is mixed for several minutes.
  • a second high shear mixing tank (not shown) which receives overflow from high shear mixer 38 can also be used to increase the residence time for high shear agitation
  • Underflow from high shear mixing tank 38 is directed gravitationally into primary separator 39 which may either be a settling tank having no agitation or having a water washing cyclone or spirals.
  • High shear mixer 38 further includes an overflow assembly allowing overflow from the high shear mixing tank 38 to be directed to laser-cut vibrating screen separator 39.
  • Separator 39 is adapted with an overflow 39a which enables overflow from the primary separator to be directed to laser cut dewatering screen 45.
  • the emulsion is preferably made up of water and oil with the addition of a small amount of surfactant sufficient to maintain a stable emulsion
  • the coal particle size can vary from 500 ⁇ m to sub micron size
  • the dosage of emulsion is critical for the successful recovery of the maximum quantity of coal and as previously indicated is important for the overall economics of the process If emulsion is used efficiently operating costs can be reduced to a minimum Furthermore, the process being computer controlled allows the system to operate without a hands on operator Good coal agglomerates can only be formed with correct emulsion dosage and are required for high recoveries on the screen To achieve the correct dosage it is vital that the mass flow of coal to the plant is known and hence the need for on line monitoring gauges which provide information for the computer to actuate variable speed pump 42
  • the mixing tank must have at least one high shear agitator, and vertical baffles to create maximum turbulence and hence giving greatest contact between coal particles and oil droplets resulting in oil coating of the particles
  • the tank must also have a quiet zone whereby the oil coating particle may be allowed to collide and grow in agglomerate size
  • the tank should also be fitted with an air distributor to promote agglomerate growth and to form a coal agglomerate floating mat This floating mat of coal product should be able to overflow the mixing tank and report to the separating screen for dewatering
  • the mixing tank should also contain an outlet by which the underflow and/or the smaller agglomerates can pass into a primary separator for further treatment
  • the high shear agitator/s must have a blade geometry such that a combination of axial and radial flow are created to allow good mixing within the body of the tank while maintaining sufficient residence time and high shear to achieve coal-oil interaction
  • Re agitator diameter to tank diameter ratio should be in the range 1 2 to 1 8 and have a power rating number between 0 5 and 10
  • the mixing tank should have provisions for introduction of the nucleonic gauges and inlet lines for the coal/water/mineral slurry and emulsion These two inlets should be in close proximity to each other or preferably mixed prior to entry into the tank
  • the product from the overflow of the mixing tank and the primary separator requires dewatering via a screen or filter While the coal product is agglomerated to larger sizes and floats on the mineral/water slurry, the mineral particles are still fine and can be sub-micron in size
  • To separate the bulk liquid from the coal it is necessary to use a fine screen with a maximum "open area" This has been achieved b ⁇ incorporating spcciall) cut screens using laser techniques
  • the screen should have an aperture of between 200-50 ⁇ m with open area between 20% - 10% To aid separation these screens c been mounted in vibrating screen deck units and the laser cut screen special!' mounted to transfer the vibrations over the whole screen deck Without these special screens, adequate dewatering would not be achieved
  • the first module prepares, stores and delivers oil emulsion at a controlled rate depending upon feed slurr) density, flow rate and coal contents
  • the second module is involved in slurn' mixing, fine coal agglomerate formation separation and dewatering processes and the third module is involved in bulk oil storage
  • a pilot plant full) automated and provided with instrumentation and variable speed controls on pumps and mixers permit process variation while continuoush measuring and recording operating parameters
  • the product gravitates to a collection belt below the structure while the tailings stream is directed to a suitable disposal circuit
  • a tailings thickener underflow is provided as feed to the pilot plant
  • the feed vanes in solids concentration during the testing period in the range 10 - 25 % b) weight and ash level in the range of 20 - 25 % Combustible recover) from the pilot plant was found under normal circumstances to be in the lange 75 90% while an oil loadings of 8 - 10% based on dry product tonnes was required
  • the product generated was low in ash (less than 1 %).
  • An automatic valve opens and allows slurry from the tailings thickener disposal line to flow to the SOAP plant
  • a pump installed in the feed line controls feed to the plant, while slurry, excess to the plants requirements, is directed to the SOAP plant tailings sump.
  • a constant flow of slurry feed and an automatically controlled quantity of oil is delivered to the high shear mixing process.
  • the speed of the fixed displacement oil dosing pump is controlled by an algorithm programmed into the PLC that takes into account the current operational parameters of flow rate to the process and oil loading, as well as slurry properties such as density and ash
  • the high frequency screening process is, under normal operating circumstances, capable of producing a product higher than expected
  • Ke factors in the success of the Sclectne Oil Agglomeration Process are - unique utilisation of the feed flow ctei. densitomctcr. and ash gauge to icgulate emulsion dosing in accordance with the coal content of the slurry, not the total solids content The influence of mineral matter content is thus discounted - Highh efficient high shear mixing pioccss that ensures oil consumption is minimised and all the emulsified oil fed to the process is effective in forming and growing agglomerates, development of emulsion chcmistn that allows low value and waste oils to be used in thepiocess. adaption of laser cut fine apeituic scieen decks on a high frcqucnc) screen to dewater thcagglomcrated coal and separate the mineral matter from the agglomerates

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Treatment Of Sludge (AREA)

Abstract

L'invention concerne un procédé d'agglomération à l'huile, destiné à la séparation et récupération d'agglomérats de fines de charbon, à partir d'une boue. Ce procédé comprend une source de boue à partir de laquelle il faut récupérer les fines de charbon, des moyens de détection en communication directe ou indirecte avec cette boue et destinés à détecter des paramètres déterminés se rapportant à l'état de cette boue, des moyens communiquant avec les moyens de détection et sensibles à une valeur ou des valeurs instantanée(s) mesurée(s) desdits paramètres, et il est caractérisé en ce que les moyens sensibles auxdits paramètres commandent/régulent l'apport d'un agent d'agglomération dans la boue, à un débit, ou selon une quantité, déterminé par au moins l'un desdits paramètres, de manière à minimiser l'utilisation de cet agent d'agglomération et à maximiser la récupération des fines de charbon pour une quantité déterminée de l'agent, la récupération dudit agent n'étant alors plus nécessaire.
EP98952419A 1997-11-03 1998-11-03 Production et recuperation commandees d'agglomerats de fines de charbon Withdrawn EP1066114A4 (fr)

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
AUPP0145A AUPP014597A0 (en) 1997-11-03 1997-11-03 Controlled production and recovery of fine-coal agglomerates
AUPP014597 1997-11-03
AUPP5186A AUPP518698A0 (en) 1998-08-10 1998-08-10 Controlled production and recovery of fine-coal agglomerates
AUPP518698 1998-08-10
PCT/AU1998/000910 WO1999022871A1 (fr) 1997-11-03 1998-11-03 Production et recuperation commandees d'agglomerats de fines de charbon

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EP1066114A1 EP1066114A1 (fr) 2001-01-10
EP1066114A4 true EP1066114A4 (fr) 2001-07-25

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RU2012150389A (ru) * 2011-11-25 2014-06-10 Рвтх Аахен Способ и устройство для снижения потерь ценных компонентов при обогащении минерального сырья
AU2013280162B2 (en) * 2012-06-21 2016-06-16 Suncor Energy Inc. Dispersion and conditioning techniques for thick fine tailings dewatering operations
CN103071583B (zh) * 2013-01-28 2016-01-13 中国煤炭进出口公司 一种重介选煤中重介质密度的控制方法及系统
CN103995498A (zh) * 2013-07-18 2014-08-20 俞元洪 一种用于泥浆脱水固化施工装置的控制系统
WO2015066275A1 (fr) * 2013-10-30 2015-05-07 Flsmidth A/S Automatisation de conditionnement de matière première
CN105233530B (zh) * 2015-09-24 2017-02-01 安徽理工大学 一种煤泥水深度澄清系统及其处理工艺
CN113713968A (zh) * 2021-08-30 2021-11-30 东北大学 一种微细粒铁矿物团聚体结构特征原位在线表征方法

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WO1999022871A1 (fr) 1999-05-14
EP1066114A1 (fr) 2001-01-10
CN1346297A (zh) 2002-04-24

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