EP0298777B1 - Method of producing fine particles - Google Patents

Method of producing fine particles Download PDF

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Publication number
EP0298777B1
EP0298777B1 EP88306282A EP88306282A EP0298777B1 EP 0298777 B1 EP0298777 B1 EP 0298777B1 EP 88306282 A EP88306282 A EP 88306282A EP 88306282 A EP88306282 A EP 88306282A EP 0298777 B1 EP0298777 B1 EP 0298777B1
Authority
EP
European Patent Office
Prior art keywords
classification device
mill
particle size
receptacle
particles
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.)
Expired - Lifetime
Application number
EP88306282A
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German (de)
English (en)
French (fr)
Other versions
EP0298777A3 (en
EP0298777A2 (en
Inventor
Herbert Frank Askew
Stephen Clifford Brown
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.)
Rio Tinto Alcan International Ltd
Original Assignee
Alcan International Ltd Canada
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Alcan International Ltd Canada filed Critical Alcan International Ltd Canada
Priority to AT88306282T priority Critical patent/ATE77974T1/de
Publication of EP0298777A2 publication Critical patent/EP0298777A2/en
Publication of EP0298777A3 publication Critical patent/EP0298777A3/en
Application granted granted Critical
Publication of EP0298777B1 publication Critical patent/EP0298777B1/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B02—CRUSHING, PULVERISING, OR DISINTEGRATING; PREPARATORY TREATMENT OF GRAIN FOR MILLING
    • B02C—CRUSHING, PULVERISING, OR DISINTEGRATING IN GENERAL; MILLING GRAIN
    • B02C23/00—Auxiliary methods or auxiliary devices or accessories specially adapted for crushing or disintegrating not provided for in preceding groups or not specially adapted to apparatus covered by a single preceding group
    • B02C23/18—Adding fluid, other than for crushing or disintegrating by fluid energy
    • B02C23/36—Adding fluid, other than for crushing or disintegrating by fluid energy the crushing or disintegrating zone being submerged in liquid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B02—CRUSHING, PULVERISING, OR DISINTEGRATING; PREPARATORY TREATMENT OF GRAIN FOR MILLING
    • B02C—CRUSHING, PULVERISING, OR DISINTEGRATING IN GENERAL; MILLING GRAIN
    • B02C21/00—Disintegrating plant with or without drying of the material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B02—CRUSHING, PULVERISING, OR DISINTEGRATING; PREPARATORY TREATMENT OF GRAIN FOR MILLING
    • B02C—CRUSHING, PULVERISING, OR DISINTEGRATING IN GENERAL; MILLING GRAIN
    • B02C23/00—Auxiliary methods or auxiliary devices or accessories specially adapted for crushing or disintegrating not provided for in preceding groups or not specially adapted to apparatus covered by a single preceding group
    • B02C23/08—Separating or sorting of material, associated with crushing or disintegrating
    • B02C23/10—Separating or sorting of material, associated with crushing or disintegrating with separator arranged in discharge path of crushing or disintegrating zone
    • B02C23/12—Separating or sorting of material, associated with crushing or disintegrating with separator arranged in discharge path of crushing or disintegrating zone with return of oversize material to crushing or disintegrating zone

Definitions

  • This invention relates to a method of reducing the particle size of solid particles and is applicable to the production of very fine particles of a wide variety of solids, including relatively hard solids.
  • Very fine inorganic particles are used for various purposes.
  • One application of such particles is as a filler material for plastics compositions, for example in filled cable sheathing compounds.
  • Use of fine powders can also accelerate reaction rates in chemical reactions involving a solid reagent and accelerate dissolution of the solid, metallic or ceramic powders of small particle size are used for processing into components, and some solid catalysts are more effective when of small particle size.
  • a superior solid product, or superior process using the products may be obtained.
  • Reduction of solid particles, especially of hard materials, to micron and sub-micron size is generally achieved by means of an attrition mill, such as a bead mill, fed with a dispersion of the coarse particles in a liquid (usually water).
  • the milled particles obtained usually have a wide particle size distribution and to obtain a reasonably uniform small particle size the particles obtained have to be classified.
  • the Applicants' EP-A-0253635 describes and claims alumina hydrate particles having a high surface area and a narrow particle size distribution, optionally with a low soluble soda content.
  • Such finely divided particles are useful as fillers in paper, rubber and plastics compositions where, not only can they improve the mechanical and electrical properties of such compositions, but also can act both as a fire/flame retardant and as a smoke supressant. Too wide a particle size distribution can have deleterious effects on filled polymer mechanical properties and residual soda can adversely affect the alumina hydrate's performance in many applications, particularly because of water pick-up.
  • the preferred method of producing alumina hydrate particles comprises milling a liquid suspension of larger alumina hydrate particles in a stirred media mill, subjecting the milled suspension to continuous classification to separate the suspension into a coarse fraction of greater particle size and a fine fraction of smaller particle size, recycling the coarse fraction to the mill input and recycling the fine fraction to the continuous classification step, if required subjecting the milled suspension to ion exchange to reduce the content of the soluble soda in the particles, and subsequently drying the suspension.
  • this particular preparative method does yield particles with a desirably narrow particle size distribution with a wide range of differing materials.
  • EP-A-0253635 no particular classification system or device is described. It has now been realised that the preparative method of EP-A-0253635 is particularly suited to classification devices which have a low separation efficiency, particularly hydrocyclones.
  • Hydrocyclones are known for dividing a suspension of milled particles into a coarse fraction and a fine fraction, but it has not so far been possible to obtain satisfactory particle size separation for particles smaller than 2 or 3 microns in a single pass through the classifying device. It has been necessary to pass the suspension through a series of classifying devices, which results in an inefficient process having a very poor yield. Furthermore, conventional theory holds that hydrocyclones have little useful separating capacity for particles below about 4 microns, particularly using relatively high slurry loadings.
  • a method of producing solid particles of reduced median particle size, other than alumina hydrate which comprises milling a liquid suspension of solid particles in an agitated media mill, pumping the milled suspension through a particle size classification device to separate the slurry into a coarse fraction and a fine fraction, the particles of the coarse fraction having a greater median particle size than the particles of the fine fraction, recycling the coarse fraction from the particle size classification device to the input of the mill, and recycling the fine fraction by pumping it to the classification device wherein recycling of both coarse and fine fractions are continued until solid particles of the desired reduced particle size are produced.
  • the agitated media mill may be of known type and may be a stirred media mill in which milling media, such as ceramic balls or rods typically of size 0.5 to 3.0 mm are agitated by means of a rotating shaft.
  • the shaft may be provided with agitating discs.
  • the mill may be a vibro energy mill in which the milling medium is agitated by vigorous movement of the milling chamber. In all cases the milling medium reduces the average particle size of the solid by attrition.
  • the mill is preferably of a type allowing continuous operation, in which the slurry can be continuously fed into the mill, generally pumped into the mill under pressure, and continuously removed at one or more points.
  • the classification device used may be a continuous centrifugal device or a hydrocyclone which allow particle size classification of the solid suspended in the slurry.
  • a suitable hydrocyclone typically has a maximum internal diameter up to 10 cm.
  • the concentration of solid in the slurry may vary widely and would normally be within the range of 5% to 65%, preferably 35% to 50% by weight.
  • the preferred concentration generally depends on the use to which the milled slurry is to be put.
  • a high concentration is normally favourable when the slurry is to be dried to produce a dry solid.
  • a viscosity modifier can be added if desired.
  • the milled suspension discharged from the mill and the fine fraction discharged from the classification device are both conducted to a receptacle for receiving the desired milled product and the contents of the receptacle are recycled to the input of the classification device by a pump intermediate the receptacle and the classification device.
  • the suspension may be pumped from a container for the initial unmilled suspension, passed into the mill at a typical pressure of up to 20 psi, and discharged to the receptacle where it is not under pressure.
  • the pump intermediate the receptacle and hydrocyclone may feed the contents of the receptacle to the hydrocyclone at a typical pressure of 50 psi.
  • the coarse fraction is discharged to the container for starting material, and the fine fraction discharged to the receptacle, at substantially zero gauge pressure.
  • the median average size of the particles obtained in the receptacle is reduced, and the larger particles eliminated by attrition, so that after a certain time the suspension may have a substantially uniform particle size which is very small.
  • the suspension discharged from the mill is conducted, not to the final receptacle for the product, but to an intermediate reservoir, and the contents of the reservoir are pumped to the classification device, from which the coarse fraction is recycled to be passed again through the mill and the fine fraction is delivered to the receptacle.
  • the fine fraction from the receptacle is brought, for example by pumping, to the reservoir so that the fine fraction is recycled through the classification device together with the suspension discharged by the mill.
  • Control of the process of this embodiment is more complex than for the embodiment described above, but the efficiency of the process is greater as only the fine fraction from the classification device is discharged to the receptacle in which the desired suspension of finely divided product eventually accumulates.
  • the suspension is aspirated through the mill by a pump arranged between the mill and the classification device, the pump feeding the milled suspension from the mill to the classification device under positive pressure.
  • the pump can feed the milled suspension to a hydrocyclone at the desired relatively high pressure, typically about 50 psi, and the pressure difference across the mill may approach atmospheric pressure (about 15 psi) which may be sufficient to allow efficient operation of the mill.
  • the coarse fraction from the classification device is again recycled to pass through the mill and the fine fraction, discharged to the receptacle, may be returned to the feed line for the classification device at a point between the mill and the pump, so that the pump aspirates the suspension from the receptacle also.
  • a further pump is provided to pump the fine fraction from the receptacle to the line feeding the classification device, the fine fraction from the receptacle being delivered to the classification device feed line at a point between the classification device and the pump feeding suspension from the mill to the device.
  • the efficiency of the mill may be increased as the pump aspirating suspension through it does not have the additional function of aspirating the fine fraction from the receptacle.
  • the mill used in the method of the invention may be a bead mill of the known "Eiger” type, loaded with zirconia beads of diameter about 0.8 mm.
  • the classification device may be a hydrocyclone of a known type, such as the "Mozley" hydrocyclone.
  • a liquid slurry of particles to be treated is fed from a container 1 to a bead mill 3 which grinds the slurry and discharges the ground slurry to hydrocyclone 4 which separates it into a coarse and a fine fraction.
  • the coarse fraction is returned through line 5 to container 1 for recycling through the mill and hydrocyclone and the fine fraction is delivered through line 6 to receptacle 7.
  • the slurry containing the solid particles is fed from container 11 to pump 12 which delivers the slurry at a pressure of up to 20 psi to the input of bead mill 13, which is of the type described below with reference to Figure 6.
  • the slurry is ground in the mill and discharged to receptacle 14.
  • the slurry in receptacle 14 is then fed to pump 15 which feeds it at a pressure of about 50 psi to hydrocyclone 16, which separates the slurry into a coarse fraction which is returned by line 17 to container 11, and a fine fraction which is sent by line 18 to the receptacle 14.
  • the method described with reference to Figure 2 allows the mill to be operated under favourable grinding conditions, that is with a slurry having a relatively high solids content (up to 65% by weight) and a high flow rate.
  • the slurry is fed to the mill under positive pressure.
  • the rate of flow is easily adjusted by adjusting the rate of operation of pump 12 so that the rate of flow of the slurry through the mill is matched to the requirements of the hydrocyclone.
  • Pump 15 may be used simply to maintain the feed pressure for hydrocyclone 15; thus the method is simply controlled by adjusting pump 12 according to the respective levels of the slurry in container 11 and in receptacle 14.
  • the method When operated with an aqueous slurry of a solid particles the method is capable of yielding particles of a median particle size of 0.3 microns or less, using only one mill and only one hydrocyclone.
  • FIG. 3 The method illustrated by Figure 3 is similar to that of Figure 2 and common components are shown by the same reference numerals.
  • Pump 12, mill 13, pump 15, and hydrocyclone 16 operate in the same way as in Figure 2 and the coarse fraction from the hydrocyclone is again recycled to container 11 through line 17, the fine fraction being delivered to receptacle 14 through line 18.
  • the output of slurry from the mill 13 is fed not to receptacle 14, but to a reservoir 20 from which it is fed by pump 15 to the hydrocyclone 16, and a further pump 21 returns the fine fraction from receptacle 14 to reservoir 20.
  • Figure 4 shows an arrangement in which only one pump is required.
  • the slurry from container 11 is again fed to bead mill 13 and passes from the mill 13 to hydrocyclone 16 which divides it into a coarse fraction which is returned to container 11 through line 17 and a fine fraction which is sent through line 18 to receptacle 14.
  • a single pump 20 both delivers the slurry to the hydrocyclone 16 at a pressure of about 50 psi and draws the slurry through mill 13 by suction.
  • the pressure difference urging the slurry through mill 13 is thus generated by aspiration by pump 20 and it may correspond substantially to atmospheric pressure, that is about 15 psi.
  • container 11 may be a closed tank and the tank may be pressurised.
  • the slurry discharged to receptacle 14 is recycled through line 21 to a point between mill 13 and pump 20, and the slurry is drawn through line 21 by the aspiration of the pump 20.
  • a valve 22 is inserted in line 21 to control the rate of recycling of the slurry from receptacle 14 and the process is controlled by adjustment of pump 20 and valve 22 as required.
  • Figure 5 shows a variant of the process of Figure 4.
  • the slurry is again aspirated through mill 13 and fed to hydrocyclone 16 by pump 20, the coarse fraction is again recycled through line 17 and the fine fraction of the slurry is recycled from receptacle 14 to the hydrocyclone 16.
  • line 21 returns the fine fraction to a point between the pump 20 and the hydrocyclone 16 and is impelled by a further pump 23 provided in line 21.
  • Pump 23 delivers the recycled fine fraction to the hydrocyclone 16 at a pressure of about 50 psi and the process is controlled by adjusting both pumps 20 and 23.
  • This variant allows pump 20 to aspirate slurry from container 11 through mill 13 more efficiently.
  • the mill comprises a tubular vessel 31 containing an agitator 32 comprising paddles extending radially from a shaft which is driven in rotation by motor 33.
  • the vessel contains a screen 34 to prevent discharge of gross oversize particles from the mill and the vessel contains, around agitator 32, beads of hard material which grind the liquid suspension.
  • the suspension is fed into the mill at inlet 35, the suspension passes through the mill and is discharged at 36 after passing through the screen 34.
  • the classification device can yield a fine fraction of narrow particle size distribution down to a very small average particle size, down to 0.4 microns or even lower.
  • a hydrocyclone classifying device does not produce any useful separation of particle size fractions at particle sizes as small as this.
  • the invention may be applied to a very wide variety of solids which may be slurried with a wide range of liquids.
  • Solids which may be milled include iron oxide, talc, silica and other minerals like chalk, zinc oxide, boric oxide, borax, zinc borate, pigments, carbon black, various metals, solid organic compounds, e.g. terephthalic acid, and mixtures thereof.
  • the liquid may be chosen from water, volatile non-aqueous liquids such as hydrocarbons, tetrahydrofuran, dioxan, alcohols and esters, and non-volatile solvents such as phthalates, polyvinylchloride plastisols and waxes.
  • Non-volatile liquids may be used when the slurry is to be used subsequently in liquid form, without drying, for example as plastisols or in certain pharmaceutical preparations.
  • the slurry may include one or more additives to aid milling, such as a dispersant, or to assist later processing, for example a stearate which forms a coating on the particles.
  • milled solid Possible applications for the milled solid include ceramics, catalysts, plastics fillers, fire/flame retardants, smoke supressants and powder metallurgy.
  • the classification device may be operated continuously or it may be operated intermittently to give quasi-continuous operation, so as to balance the flow of coarse fraction from the classification device with the mill input.
  • the overall process is generally operated as a batch process, i.e. with 100% recycle of both coarse and fine particle fractions since generally the efficiency of the separation device is too low for continuous operation to yield particles of the desired average particle size and breadth of particle size distribution.
  • the method of the invention may be operated at a range of temperatures according to the nature of the solid and/or liquid being processed. An operating temperature down to -20°C is generally feasible.
  • the product taken from receptacle 14 was then analysed using the "Malvern" laser photon correlating spectrometer and was found to have a median particle size of 0.28 microns and a polydispersity of 0.23.
  • Polydispersity can be measured in a number of different ways, but for the purposes of the present invention it is based on a light scattering analysis technique utilising photon correlation spectroscopes manufactured by Malvern Instruments Limited of Malvern, England.
  • terephthalic acid available from ICI 50 kg were dispersed into 100 litres of water and milled as Example 1 above for a total of 15 hours.
  • a further 400 litres of water were added at intervals during the 15 hours together with 2 litres of "Teepol" surfactant available from Shell.
  • the feed material prior to grinding had a specific surface area of 0.18 m2/g as determined by the standard Strohlein method as described in "Particle Size Measurement", p. 390, Terence Allen, Chapman and Hall Ltd. 1975, a median particle size of 83 microns as determined by Coulter counter, and a particle size mode of 90 microns as determined by Coulter counter.
  • the product taken from receptacle 14 had a surface area of 3.9 m2/g, a median particle size of less than 1.2 microns, and particle size mode of 1.1 microns as evaluated by the same methods.

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  • Engineering & Computer Science (AREA)
  • Food Science & Technology (AREA)
  • Crushing And Grinding (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Manufacturing Of Micro-Capsules (AREA)
  • Separation Of Solids By Using Liquids Or Pneumatic Power (AREA)
  • Glanulating (AREA)
  • Cyclones (AREA)
  • Disintegrating Or Milling (AREA)
EP88306282A 1987-07-09 1988-07-08 Method of producing fine particles Expired - Lifetime EP0298777B1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT88306282T ATE77974T1 (de) 1987-07-09 1988-07-08 Verfahren zur herstellung von feinkoernigen partikeln.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB8716213 1987-07-09
GB878716213A GB8716213D0 (en) 1987-07-09 1987-07-09 Producing fine particles

Publications (3)

Publication Number Publication Date
EP0298777A2 EP0298777A2 (en) 1989-01-11
EP0298777A3 EP0298777A3 (en) 1990-02-07
EP0298777B1 true EP0298777B1 (en) 1992-07-08

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Family Applications (1)

Application Number Title Priority Date Filing Date
EP88306282A Expired - Lifetime EP0298777B1 (en) 1987-07-09 1988-07-08 Method of producing fine particles

Country Status (12)

Country Link
EP (1) EP0298777B1 (zh)
JP (1) JPH01104354A (zh)
AT (1) ATE77974T1 (zh)
AU (1) AU605886B2 (zh)
BR (1) BR8803484A (zh)
CA (1) CA1323015C (zh)
DE (1) DE3872610T2 (zh)
GB (1) GB8716213D0 (zh)
IE (1) IE61937B1 (zh)
IN (1) IN171515B (zh)
NO (1) NO174282C (zh)
ZA (1) ZA884970B (zh)

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2579984B2 (ja) * 1988-01-28 1997-02-12 株式会社クボタ 粒状体の製造方法及びその製造装置
US5171631A (en) * 1990-07-19 1992-12-15 Aluminum Company Of America Spacer/extender for titanium dioxide in pigment systems for coatings
KR100754454B1 (ko) * 2003-06-17 2007-09-03 수닝 왕 분쇄-연마 장치 및 그것을 포함하는 두유 제조기 및제조방법
JP4703126B2 (ja) * 2004-03-29 2011-06-15 太平洋セメント株式会社 水素貯蔵材料の製造装置および水素貯蔵材料の製造方法
JP5058037B2 (ja) * 2008-03-17 2012-10-24 Ｊｆｅスチール株式会社 一酸化炭素吸着剤の製造方法
SG170634A1 (en) * 2009-10-20 2011-05-30 Musse Singapore Pte Ltd An apparatus and method for size reduction
TR201904225A2 (tr) 2019-03-21 2019-07-22 Kaleseramik Canakkale Kalebodur Seramik Sanayi Anonim Sirketi Bi̇r öğütme si̇stem ve yöntemi̇ ve bunlarla i̇lgi̇li̇ bi̇r serami̇k üreti̇m yöntemi̇

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL103261C (zh) * 1954-12-17
CH505651A (de) * 1968-03-21 1971-04-15 Escher Wyss Ag Vorrichtung zum Mahlen und Sichten eines körnigen Gutes, insbesondere von Zement
US3887142A (en) * 1973-06-21 1975-06-03 Richard E Mcelvain Ore grinding circuit
DE3334235A1 (de) * 1982-11-04 1984-05-10 Heinz 4630 Bochum Jäger Verfahren und vorrichtung zur energiesparenden herstellung eines feingutes, insbesondere zement
GB8617387D0 (en) * 1986-07-16 1986-08-20 Alcan Int Ltd Alumina hydrates

Also Published As

Publication number Publication date
NO174282C (no) 1994-04-13
EP0298777A3 (en) 1990-02-07
NO174282B (no) 1994-01-03
JPH01104354A (ja) 1989-04-21
ATE77974T1 (de) 1992-07-15
IE61937B1 (en) 1994-11-30
BR8803484A (pt) 1989-01-31
NO883051L (no) 1989-01-10
AU605886B2 (en) 1991-01-24
NO883051D0 (no) 1988-07-08
DE3872610D1 (de) 1992-08-13
ZA884970B (en) 1989-03-29
DE3872610T2 (de) 1993-02-18
IE882089L (en) 1989-01-09
IN171515B (zh) 1992-10-31
AU1891088A (en) 1989-01-12
CA1323015C (en) 1993-10-12
EP0298777A2 (en) 1989-01-11
GB8716213D0 (en) 1987-08-12

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