AU632090B2 - Mineral separator - Google Patents

Description

6't320 0

AUSTRALIA

Patents Act COMPLETE SPECIFICATION

(ORIGINAL)

Class Int. Class Application Number: Lodged: Complete Specification Lodged: Accepted: Published: Priority Related Art: o 0 0 00 0 .0 00 APPLICANT'S REF.: C.A.P. of PJ 2715 Name(s) of Applicant(s): NEIL ROBERT ALLEN 9 P'1. LTO., E X.C'1 SJ1G' jt.r1) 000 0 0 :Address(es) of Applicant(s): 0 7 LAWRY HEIGHTS, ST. HELENS, TASMANIA 7216,

AUSTRALIA

1-7/A'SQ6( l aPyiRoaod, 3"-Ii gal TeS 1t0IC 1; jjv 1 (vc a LO+ KC% I U kJO 04.

0 0 0 Actual Inventor(s): NEIL ROBERT ALLEN Address for Service is: -PHlILIPS;ORMONE-ANDF-T-Z-P-AT-R-GK--.

-Pat-ent-and-T-rade--Mark-Attorneys- Mlbourne-Austraia--3O-- ~u~AriUi1YUCA Complete Specification for the invention entitled: ,19. CA .'R-4ON j 'L I "MINERAL SEPARATOR" The following statement is a full description of this invention, including the best method of performing it kno04? 1 applicant(s): P19/3/84 MINERAL SEPARATOR This invention relates to a mineral separator and more specifically to a hydromechanical mineral separator wherein differences in specific gravity of minerals in a slurry are utilized for separating those minerals. The invention will be described with reference to a separator for separating gold from a slurry or pulp, but it is to be understood that the invention has wider application.

Various hydromechanical separators are known, and these include spiral separators, table concentrators and the like.

Generally these separators are of large and complex construction making them expensive to install and operate, and thus are unsuitable for smaller operations.

o°°o Another problem with prior art hydromechanical oo. separators is that they frequently require large flowrates of 0 0 water or other separating liquid to operate efficiently and such flowrates are not always readily available. Some 0 0 0o o separators are unsuitable to separate a wide range of particle 0oo 0°s- sizes and for this reason are either unsuitable for separating some minerals, or only separate out a certain fraction of the desired mineral. This is unsatisfactory where the mineral being separated is of high value such as gold.

0o0 An object of this invention is to provide a mineral o o'o separator which is of relatively simple construction, is easily operated and operates efficiently.

separator comprising an elongate separator tube arrangedo be mounted with its axis substantially vertical, sai geparator SOo.oe tube having a generally cylindrical narrow eter central portion, a larger diameter upper portii, and a larger diameter lower portion, an operatin iquid inlet into said lower portion and an operating id outlet from said upper portion, a slurry inlet int aid upper portion, and a tapered transition section betw said lower portion and said central portion, said tape transition section having a small angle of coni-Aty, aid separator being operable by passing operatin iquid between said fluid inlet and said fluid outl at a rate such that heavier particles in a slurry 2 17 k According to the invention there is provided a mineral separator comprising an elongate separator tube arranged to be mounted with its axis substantially vertical, said separator tube including a relatively narrow central portion having a generally cylindrical inner wall, a relatively broad upper chamber and a relatively broad lower chamber, an inlet for operating fluid in said lower chamber and an outlet for operating fluid in said upper chamber, a slurry inlet in said upper chamber, and a transition section between said lower chamber and said central portion, said transition section having a relatively small angle of conicity for providing a gradual transition between said lower chamber and said inner wall, said separator being operable by passing 0 15 operating fluid between said fluid inlet and said fluid outlet at a rate such that relatively heavier particles in a slurry introduced into said slurry inlet will pass down a said separator tube in a boundary layer adjacent said S0 inner wall and counter current to said operating fluid, 20 and relatively lighter particles in said slurry will pass s oon out of said separator tube through said fluid outlet.

00 It is preferred that the transition section has a 0 half-cone angle of between 0.50 and 50. It is also preferred that there is a tapered upper transition section 25 between the upper end of the central portion and the upper 0 0 chamber. The upper chamber may itself be cone shaped.

o The upper chamber of the separator may have an 0 axially aligned truncated cone shaped guide plate mounted therein for guiding slurry introduced into the upper chamber radially outwardly towards the inner wall of the separator, openings being provided between the base of the guide plate and the inner wall of the separator tube to permit slurry to pass from the upper chamber into the central portion.

A further feature of the invention is the provision of a central rod axially aligned and supported within the central portion. The lower and/or upper ends of the rod may be tapered and the lower end of the rod is preferably S 39 3 suspended at or near the lower end of the central portion. Means may be provided for electrically or magnetically charging the rod, or the rod may be formed from magnetic materials.

A preferred embodiment of the invention is described in detail in the following passages of the specification which refer to the accompanying drawings. The drawings, however, are merely illustrative of how the invention might be put into effect, so that the specific form and arrangement of the various features as shown is not be understood as limiting on the invention.

In the drawings: Figure 1 is a cross-sectional side view of a separator according to the invention, Figure 2 is an enlarged cross-sectional side view of 0 the lower chamber of the separator shown in Figure 1, o o Figure 3 is an enlarged cross-sectioial side view of the upper chamber of the separator shown in Figure 1, 00 Figure 4 is a cross-sectional plan view along line IV-IV shown in Figure 1, Figure 5 is a diagrammatic side view of two A ao separators according to the invention connected together in series, and SFigure 6 is a perspective view of a bank of separators operating as a separator system.

p In the embodiment of the invention shown in the p a 0drawings the separator tube 1 is formed as an elongate tubular member 2 which is vertically mounted in use by any suitable mounting frame or the like (not shown) The separator tube 1 has a relatively large diameter upper chamber 3, a narrow diameter central portion 4, and a relatively large diameter lower chamber 5. A liquid inlet 6 is provided into the lower chamber 5, and a liquid outlet 7 is provided from the upper chamber 3. The upper chamber 3 has an open upper end 8 to provide an inlet for slurry or other material to be separated 0 A central rod 9 is suspended axially within the central portion 4. A guide plate 30 is mounted in the upper portion to guide -16said fluid being passed through a aesc ;4irl hteavier density mineralwilfl slurry material towards the inner wrall 11 of the separator tube i. Baffle plates are provided in the lower chamber and separated material is collected in collection means 12 provided at the lowermost end of the tube 1.

It is to be understood that the various components depicted in the drawings are not drawn to scale or in proportion, and dimensions and angles are drawn enlarged where necessary to facilitate description.

The separator tube operates to separate out the heaviest fraction of a particulate slurry introduced into the tube through the slurry inlet 8. An operating liquid J such as water is passed through the separator tube from the liquid inlet 6 to the liquid outlet 7. The rate at which the liquid is passed through the tube 1 is selected so that the heaviest fraction of the particulate material is able to pass down the tube under the influence of gravity whilst the lighter particles are carried upwardly o to pass out of the tube through outlet 7 as tailings with the operating liquid. The system operates substantially o 20 in accordance with Stokes's Law: 2 v 2gr (P Po) o :9 where v is the velocity of the particle relative to the 25 operating fluid, g is gravitational acceleration, Sr is the radius of the particle, °0000 °n is the dynamic viscosity, p is the density of the particle, and PO is the density of the liquid.

The system will only operate where Reynolds number is less than 0.2. It will be appreciated that Stokes's Law provides only an approximation to particle flow performance since the particles in practice will not be spherical.

Separation takes place in a boundary layer just adjacent the wall of the central portion 4. The various components of the separator tube 1 will now be described 39 -1 RA

M

T2' in greater detail.

Turning to Figure 2 of the drawings, the central portion 4 of the tube 1 is connected to the lower portion by a :tower transition section 13. The lower transition section 13 provides a gradual transition or taper between the relatively narrow diameter central portion 4 and the larger diameter lower chamber 5. Preferably the transition section is comprised of two sections, an upper part 14 and a lower part 15. The upper part 14 has a very gradual taper which may have a half-cone angle of between say 0.50 and 30. The lower part 15 may have a slightly greater half-cone angle say of between 1.50 and In the preferred arrangement the upper part extends for a length of about 100 mm at a half-cone angle of 1.50 and the lower part extends for a length of about 200 mm at a half cone angle of 2 In use, small particles will tend to dislodge from the inner wall 11 of the tube wherever they encounter turbulence or high flow rates. Accordingly, at the S 20 transition section 13 it is desirable to only gradually expand the diameter of the tube to thereby ensure that turbulence in this region is minimal. Fluid flowing up 0.ooothe tube will flow relatively slowly in the transition section 13 sinco the diameter in that section is greater oo 25 than the diameter in the central portion 4. Thus, the combined effect of the lower flowrate and the gradual increase in diameter will tend to hold the particles S° against the inner wall 11 as the particles move down the wall into the lower transition section 13 under influence of gravity.

The lower end 16 of the central rod 9 has a tapered 39 5a

T

configuration, tapering towards a point at its end 17. The end 17 is preferably located at the interface between the lower end of the central portion 4 and the upper end of the transition section 13. The effect of the taper is that in the lowermost region 18 of the central portion the cross-sectional area of the flow passage is greater than in the parts of the flow passage above the taper. Thus, the velocity of flow in this lowermost region 18 will be lower, and accordingly there will be a greater tendency for the particles to adhere to the inner wall 11 as the transition section begins. Also, the itapered configuration of the rod 9 ensures that flow of fluid in this lowermost region 18 is maintained as laminar flow.

The rod 9 is preferably held in position at its lower end by a Sj wire spider 20. In one arrangement which has been tested the I central portion had an internal diameter of 19 mm, the rod had Sa diameter of 12.5 mm, the upper transition part 14 was 100 mm i long and increased the diameter of the tube from 19 to 24 mm, i and the lower transition part 15 was 200 mm long and increased the tube diamete from 24 mm to 36 mm.

The lower 4 p l 5, in the region of the liquid inlet 6 preferably has a series of baffles 22 mounted therein for inducing laminar flow in the liquid in that region and ensuring the liquid passes into the transition section 13 and i the central portion 4 as laminar flow. The baffles 22 may take any convenient form, but it is envisaged that a series of vertically aligned baffle plates 23 radially spaced around the 5 will serve as a satisfactory flow guide and j baffle arrangement. For a tube having a transition section 13 with dimensions as set out in the preceding paragraph the lowerfP.z-. 5 in the region of the fluid inlet 6 will preferably have a diameter of about 150 mm.

The uppe *o 3 is depicted in detail in Figure 3 of I CN-\C~aQ\ the drawings. As shown, the upper ;=ig 3 is formed by a substantially truncated cone shaped body 25 having its upper end 8 open to receive slurry or other particulate matter for separation. The lower most end 26 of the body 25 is connected to the central portion by an upper transition section 27 which has a small taper angle. The half-cone angle of the upper 39 transition section 27 is preferably between 10 and 50. In -o 1 6 one example arrangement the upper transition section 27 was 36 mm at its upper end and 19 mm at its lower end. Thus, the wall 28 of the body 25 tapers convergently to meet the upper end of the upper transition section 27. The angle of taper of the upper transition section 27 is small so that a minimum of turbulence is created by liquid passing through this region of the tube 1.

A truncated cone shaped guide plate 30 is located in the upper portion towards the lower part of the body 25. The lower edge 31 of the guide plate 30 flares radially outwardly to form a flange 32 which engages the tube 1 at about the middle of the upper transition section 27. A plurality of openings 33 are provided in the flange 32. The guide plate "o tapers convergently in a direction away from the central portion 4. The guide plate 30 serves as a baffle to calm the l'quid flow in tne annular space 34 between the guide plate and the inner wall 35 of the body 25. Thus, slurry deposited o in the body 25 through opening 8 will settle evenly in the space 34 and will then discharge slowly and evenly through the openings 33. The openings 33 will be configured to restrict the rate at which particles enter the upper transition section and thereby prevent minerals or other particles to be o separated surging down one side of the central portion 4.

It should also be noted that the tapered configuration a of the guide plate 30 will result in a slightly restricted outlet opening 36 being formed at the truncated upper end 37 of the guide plate. The outlet opening preferably has a diameter less than that of the central portion 4. Liquid S passing up the tube 1 in use will create a fountain like localized turbulent region above this outlet opening 36 thereby tending to disperse particles suspended in the liquid within the body 25. The result of this dispertion will be that heavier particles will tend to settle first in the annular space 34 thereby providing an initial separating action for the material being separated, concentrating the heavier particles at the base of the annular space 34.

The upper end 40 of the central rod 9 will also preferably be tapered to minimise turbulence in this upper 39 region. The rod 9 will preferably commence tapering at the KA 7 lower end of the upper transition section 27. The rod 9 may be supported at its upper end 40 by vanes 41 which radiate outwardly to connect the rod 9 to the wall 11 of the tube i, and also serve to guide the flow of fluid in the upper region of the tube i. An e*ectrical conductor 43 is connected to the upper end 40 of the rod for electrically charging the rod if required.

In addition, a charging screen 45 may be mounted above the guide plate 30 for optionally charging particles in the fluid. The screen 45 may also serve to evenly disperse particles deposited in the upper portion through opening 8.

o 0 The central rod 9 may be utilized to apply a magnetic, o o o electromagnetic or electrostatic force to zome particles in preference to others. Thus, the rod 9 may be solid metallic, 0 0 o insulated metallic or composite with metallic or 000 o electromagnetic elements. An electrical conductor 46 is °00 attached to the upper end 40 of the control rod and that ooon conductor is also connected to the charging screen 45. The conductor 45 is connected to circuit means (not shown) for providing the necessary charge to the screen 45 and/or rod 9 S o as required.

The region 50 of the separator tube below the liquid inlet 6 is preferably used to collect separated particles and 00 0 ao funnel those particles into a suitable container 12. The lower region 50 may be funnel shaped (as shown), the outlet i from the funnel leading to the container through a suitable i! tube 51. It is preferred that the container 12 is removable 'I from the separator 1 in order that separated concentrate can j be removed from the separator from time to time without interrupting the operation of the separator.

In use, a liquid, which will generally be water although other liquids could be used, will be passed through the separator from the inlet 6 to the outlet 7. The rate at which liquid is passed through the system will depend on a range of factors and in particular as the system will basically be operating in accordance with Stokes's Law, initial operating parameters can be selected as determined by that Law. It is clear that it is important to accurately size the particles 39 being separated since different flow rates will optimally be KA 8selected for different particle sizes. Flow rate will also be dependent on the relative densities of the material being separated and the operating liquid. Also, flow rate will be selected according to the separation efficiency required and the rate of separation required.

When the separators are used to separate heavier density mineral particles from lighter density mineral particles the separator will operate substantially as follows. In the separator, the mineral particles are allowed to fall freely against a rising liquid current in the central portion 4 of the tube 1. As a first approximation, the idea is that the 0 *0 upward velocity of the liquid is set a little less than the 0 0 0 terminal velocity of the denser mineral, but greater than the S terminal velocity of the less dense mineral. Thus, the denser o 0 mineral will descend while the less dense mineral, of similar 00o size, is prevented from falling.

0 When there is liquid flow, and in particular laminar flow, through a pipe, there will exist a fluid velocity gradient between the walls of the pipe and the centre. The velocity changes will tend to be parabol-c, with the velocity S 11 at the walls zero. The region close to the walls of the pipe where the velocity changes rapidly away from the walls is termed the boundary layer. A particle descending a vertically aligned pipe against a liquid flow experiences a velocity "slope" which forces it against the walls of the tube, towards K the boundary layer, into a region of lower upward liquid K velocity.

As the particles are effectively in motion through a I liquid where the velocity of the liquid is faster past one side of the particle than it is towards the other side of the particle, the particles also experience a sideways force towards the centre of the tube and away from the walls. This is known as the Bernoulli effect. Turbulence around the irregularly shaped mineral particles destroys much of this effect, but it does assist in separation by tending to force less dense minerals radially inwardly into the faster flow region in the tube and they are then returned by the liquid flow up the tube. However, for the denser particles, the 39 Bernoulli effect is less than the flow gradient effect and the KA 9 I_ XII-~L L~I-III- particles remain against or mo- owards the wall 11 of the tube.

Each irregularly shaped descending particle carries with it a region of local turbulence, which extends for several diameters around it and which causes a local disruption of the laminar flow in the tube which extends for many diameters behind it. From observation it would seem that a separation between particles of about 20 diameters allows a reasonably laminar flow to be maintained if water is the liquid used for separation. Thus, descending particles should maintain an average separation of about 20 diameters for separation to o0 operate efficiently.

oo, 0 te 0Generally, prior to being separated, an ore containing S° the desired mineral will be crushed and ground to a particle o size which will suit the separator. Thereafter the crushed 0oo000 S material will be sized using suitable screens. The crushing and screening will be done using well known techniques.

It,.

In order to produce good separation of denser from less II dense partciles, it is also necessary for the particles to be I 20 screened to size ranges such that the terminal velocity of the smallest denser particles is at least 10% greater than the terminal velocity of the largest less dense particles. The upward flow in the separator is then set to prevent the less dense particles from descending. The combined influence of ii the Bernoulli effect, the boundary layer effect, and the mineral irregularity in shape, results in an arrangement in t which the liquid velocity up the tube is optimally very close to, but slightly less than, the calculated terminal velocity of the denser mineral.

i 30 For example, if particles are sized between 100 and 150 Itmicrons, then 100 micron gold (with a terminal velocity of 9.8 cm/sec) could be separated from 150 micron galena (with terminal velocity of 8.1 cm/sec) if the liquid velocity in the tube is set to about 9 cm/sec.

On the other hand, 100 micron galena (with a terminal velocity of 3.6 cm/sec) could not be separated from 150 micron barite (with a terminal velocity of 4.9 cm/sec). In this case the screening would have to be closer (say between 100 and 120 39 microns).

KA r~lr The following separation rates have been suggested for commercially available screens using a downward velocity of 0.1 of the terminal velocity for galena and a downward velocity of 0.2 of the terminal velocity for gold, using a 19mm internal diameter plastic tube. The maximum separation rates are for the separation of galena from barite and free gold from pyrite.

Screen Size (microns) Galena (Q/hour) Gold (Q/hour) 45 0.4 45 53 0.5 7 53 61 0.8 11.5 S61 76 1.3 17.5 76 100 2.4 33.5 0 100 130 5.6 76 So 130 142 12.3 167 o a The above calculated separation rates assume that the °1 0 desired mineral is fed to the top of the separator tube at a rate equal to the rate at which the separated material is extracted from the lower end of the separator. Turbulence in the feed cone will always return some of the desired mineral oO, back up into the cone. If feed to the top cone is stopped, 0000 o then the separation rate will tail off exponentially. If the feed of the desired minerals to the top of the separator tube is greater than the best separation rate possible, then turbulence occurs in the central portion of the separation tube as too much mineral tries to descend at once and the 0 particle separation is not adequate. Such turbulence carries down with it some of the less dense mineral and destroys separation accuracy. For example, if a 100 to 150 micron head 130 sample contains 20% galena, and the separation rate for a test L 01sample of galena is 5.6g/hour in a 19mm tube, then the material should be fed at 28g/hour.

As shown in Figure 4, separator tube 1 has a central portion 4 with an inner wall 11. A boundary layer 53 is formed adjacent the inner wall 11 and particles descending the central portion 4 will tend to do so in this boundary layer 53. The central rod 9 is axially located within the central portion 4 and a second boundary layer 54 is also formed around 39 the central rod 9. Maximum flow velocity for the liquid in KA -11the tube will be approximately midway between the boundary layers.

Optionally there may be a slight spiralling motion of liquid flowing up the central portion 4 of the tube 1 so that a centrifugal force will tend to urge the heavier particles towards the wall 11 of the tube 1 and into the boundary layer 53 so that gravitational force can carry those heavy particles to the lowermost end of the tube and into the container 12.

The inner wall 11 of the central portion 4 may have a helically shaped groove indicated by dotted line 55 in Figure 2 which will tend to in.part the spiralling motion to the oO liquid flowing up the tube. Optionally, the baffles 22 may be aligned at an angle to the vertical axis of the tube so as to o 00 0 induce this spiralling motion of the liquid flowing up the S tube.

0 o 0The separator need not be used on its own and it is 0 70 envisaged that separators may be connected together in a unit 0004 comprising a series of two or more separators, the liquid outlet 7 from one separator being connected into the slurry inlet 8 of the second or subsequent separator prior to being 0o°° discharged to waste. Figure 5 depicts such an arrangement.

In this manner lighter particles must pass through at least 0 0 two separators prior to discharge. The flowrates through the two separators will preferably differ, that is to say, the 0 4o liquid being introduced into one separator need not be at the same rate as the liquid being introduced into the second or subsequent separator. In addition, the actual configuration of the separators in series may differ so that the diameter of the central portions 4 of the different separators in the unit need not be the same.

i Generally the material to be separated is first treated either by crushing or otherwise broken down into separate particles. Thereafter the material is sized in order that particles of substantially the same order of magnitude are separated together. It has been found in practice that a factor of two relationship between sizes is satisfactory.

For separating material having a normal distribution range of particle sizes it may prove advantageous to mount a 39 number of separator units in parallel relationship to each 12 other, each separator unit being arranged to separate a different size range of material. The separator units in parallel may then be mounted in a bank which will be used to treat all material to be separated. Figure 6 depicts such an arrangement. The separator units in the bank of separators will each separate out a different range of particle sizes.

Thus, as shown in Figure 6, each separator unit 60 which comprises two separator tubes 61 will be mounted in parallel such that the entire bank of separators will separate out a normal distribution range of particle sizes. Each separator unit will receive material from its specific sizing screen and So the bank of separators will thus serve to separate the entire o range of particle sizes produced by the crushing plant.

Clearly, when separators are mounted in series to form a 0 2 unit it will be possible to use that unit in different ways by o o adjusting the flowrats through the unit. One way in which the unit can be used is as described above in which the first 00 separator in the unit separates out almost pure concentrate, and the second separator in the unit separates out a less pure fraction of concentrate.

A second way of using the unit will be to separate o different minerals having differing specific gravities in the So two separators. Also, where separator units are mounted in a o bank of units that bank may be used for separating out either o 00 different sizes of concentrate, or different minerals from the same slurry, as may be required.

It is to be understood that various alterations, modifications, and/or additions may be introduced into the constructions and arrangements of parts previously described without departing from the spirit or ambit of the invention.

39 KA 13-

Claims (9)

1. A mineral separator comprising an elongate separator tube arranged to be mounted with its axis substantially vertical, said separator tube including a relatively narrow central portion having a generally cylindrical inner wall, a relatively broad upper chamber and a relatively broad lower chamber, an inlet for operating I fluid in said lower chamber and an outlet for operating 1 0 fluid in said upper chamber, a slurry inlet in said upper chamber, and a transition section between said lower chamber and said central portion, said transition section having a relatively small angle of conicity for providing a gradual transition between said lower chamber and said inner wall, said separator being operable by passing S.operating fluid between said fluid inlet and said fluid outlet at a rate such that relatively heavier particles in ta slurry introduced into said slurry inlet will pass down a 8 said separator tube in a boundary layer adjacent said inner wall and counter current to said operating fluid, and relatively lighter particles in said slurry will pass out of said separator tube through said fluid outlet.

2. A mineral separator according to claim 1 wherein said upper chamber is of circular cross-section. V 25 3. A mineral separator according to claim 1 or 2 0 wherein said lower chamber is of circular cross-section. o, 4. A mineral separator according to claim i, 2 or 3 ttt Swherein said tapered transition section has a half-cone angle substantially between 0.50 and

5. A mineral separator according to any one of the preceding claims wherein a further transition section is located between said upper chamber and said central portion, said further transition section being of truncated cone shape with said cone diverging in an upward direction and having a half-cone angle substantially between 10 and

6. A mineral separator according to any one of the preceding claims wherein an upwardly converging axially 39 aligned truncated cone shaped guide plate is mounted above F- K 15 said central portion, said guide plate having a base adjacent the upper end of said central portion, said base f including openings for passage of particles from said upper chamber to said central portion.

7. A mineral separator according to claim 6 wherein said guide plate includes a further opening at its upper end, said further opening having a diameter which is less I than the diameter of the central portion.

8. A mineral separator according to any one of the i 10 preceding claims wherein an elongate rod is suspended in H l said central portion and extends at least a significant H portion of the length of said central portion. i 9. A mineral separator according to claim 8 wherein K said rod is arranged to be electrically or magnetically j 15 charged and is adapted to impart a charge to particles to i be separated by said separator in use. i1 0. A mineral separator according to claim 8 or 9 Swherein said rnd is suspended at at least one end thereof g by guide vanes which induce laminar flow in said central portion in use.

11. In combination, a plurality of mineral separators each according to any one of the preceding claims connected together in series such that the fluid outlet j from a first mineral separator will pass into a slurry 25 inlet in a second mineral separator, said separators being operable together.

12. A method of obtaining separation of a relatively j high density mineral from a mineral ore containing said high density mineral including, crushing and grinding said ore to form a particularized material mix, screening said particularized material mix to obtain a material of substantially uniform particle size, introducing said uniform size material into the slurry inlet of a separator according to any one of claims 1 to passing an operating fluid between said fluid 39 inlet and said fluid outlet of said separator, S Nh '1,

16- said fluid being passed through at a rate such that said heavier density mineral will fall S the action of gravity, whilst other minerals in the mix" will pass out of said fluid outlet as tailings, and removing separated high density mineral from a collector at the operatively lower end of said separator. 13. A method according to claim 12 including the step of testing said mineral ore to determine the percentage of high density mineral in said ore and introducing said particularized material mix into said separator at a rate commensurate with the rate at which said high density mineral can be efficiently separated by said separator. 14. A mineral separator substantially as herein described with reference to the accompanying drawings. o. 20 15. A method of obtaining separation of a relatively high density material from a mineral ore containing said o ohigh density material substantially as herein described with reference to the accompanying drawings. So n DATED: 13 October 1992 I a° PHILLIPS ORMONDE FITZPATRICK Attorneys for: TGE PTY. LTD., ENGINEERING GEOLOGY SPECIALISTS PTY. LTD. and NEIL ROBERT ALLEN 3720u 39 JT