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WO1995025585A1 - Procede de production d'agglomerats - Google Patents

Procede de production d'agglomerats Download PDF

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Publication number
WO1995025585A1
WO1995025585A1 PCT/AU1995/000156 AU9500156W WO9525585A1 WO 1995025585 A1 WO1995025585 A1 WO 1995025585A1 AU 9500156 W AU9500156 W AU 9500156W WO 9525585 A1 WO9525585 A1 WO 9525585A1
Authority
WO
WIPO (PCT)
Prior art keywords
agglomerates
process defined
mineral
fluidised bed
particle size
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.)
Ceased
Application number
PCT/AU1995/000156
Other languages
English (en)
Inventor
David John Mccarthy
John Takos
Terence Box
Peter John 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.)
Pasminco Australia Ltd
Technological Resources Pty Ltd
Pasminco Ltd
Original Assignee
Pasminco Australia Ltd
Technological Resources Pty Ltd
Pasminco Ltd
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 Pasminco Australia Ltd, Technological Resources Pty Ltd, Pasminco Ltd filed Critical Pasminco Australia Ltd
Priority to AU20621/95A priority Critical patent/AU704350B2/en
Priority to EP95912963A priority patent/EP0751821A4/fr
Priority to JP7524253A priority patent/JPH10500353A/ja
Priority to FI963770A priority patent/FI963770L/fi
Publication of WO1995025585A1 publication Critical patent/WO1995025585A1/fr
Priority to MXPA/A/1996/004214A priority patent/MXPA96004214A/xx
Anticipated expiration legal-status Critical
Priority to NO964000A priority patent/NO964000L/no
Ceased legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2/00—Processes or devices for granulating materials, e.g. fertilisers in general; Rendering particulate materials free flowing in general, e.g. making them hydrophobic
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/02—Roasting processes
    • C22B1/10—Roasting processes in fluidised form
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/14—Agglomerating; Briquetting; Binding; Granulating
    • C22B1/16—Sintering; Agglomerating

Definitions

  • the present invention relates to a process for producing agglomerates of a feed material for a fluidised bed roaster or a fluidised bed combustion furnace.
  • particles of the mineral concentrate feed that are above an upper limit of the preferred particle size distribution tend to remain in the bed and may lead to defluidisation of the bed.
  • the preferred particle size distribution for fluidised bed roasters varies with the type of fluidised bed roaster.
  • 0.1 to 2mm is the preferred particle size distribution for a known type of Lurgi fluidised bed roaster which operates with superficial gas velocities in the bed of approximately 0.67 m/sec at a temperature of 975°C and approximately 0.4 m/sec in the freeboards.
  • the preparation of a mineral concentrate feed for fluid bed roasting is normally done by a process of grinding and froth flotation of an ore containing the mineral.
  • froth flotation invariably results in the mineral concentrate being produced as a slurry and, in this form, the mineral concentrate cannot be transported by shipping or handled or stored using conventional solid handling systems, and the mineral concentrate is not a suitable feed for a Lurgi-type fluidised bed roaster.
  • dewatering and agglomeration of a mineral concentrate are necessary to produce a mineral concentrate in a form that can be readily handled, transported, and stored, and subsequently calcined under optimum operating conditions for a fluidised bed roaster.
  • An object of the present invention is to provide an improved process for producing agglomerates of a mineral concentrate, particularly a finely-ground mineral concentrate.
  • the agglomerates be suitable for use as a feed material for a fluidised bed roaster or a fluidised bed combustion furnace.
  • the process may include the addition of water to the agglomerates.
  • the compaction step (b) forms agglomerates that are relatively dense with a sufficient "green” strength to enable handling, transportation, and storage without significant breakdown of the agglomerates.
  • relatively dense is understood herein to mean that the agglomerates be sufficiently compact to withstand handling without degradation to an unsatisfactory size range.
  • the compaction step (b) forms relatively dense agglomerates and/or that the moisture content of the agglomerates be selected so that, when the agglomerates are fed into a fluidised bed roaster or a fluidised bed combustion furnace and are subjected to elevated temperatures, the agglomerates break down into smaller-sized agglomerates that can be processed more efficiently in the fluidised bed roaster or the fluidised combustion furnace.
  • the present invention is based on the realisation that:
  • step (i) by appropriate selection of the particle size of the input feed and the compaction of the input feed in step (b) , it is possible to form agglomerates having a preferred pore size;
  • the agglomerates when the agglomerates are fed into a fluidised bed roaster or a fluidised bed combustion furnace and are subjected to elevated temperatures, the agglomerates break down into smaller-sized agglomerates that can be processed more efficiently in the fluidised bed roaster or the fluidised combustion furnace.
  • the feed material may be any material.
  • the feed material may be an organic material, such as coal washery slimes.
  • the feed material may also be an inorganic material, such as a mineral or a mineral concentrate.
  • the feed material be a zinc sulphide concentrate for calcining in a fluidised bed roaster.
  • the input feed for step (a) comprises an ore containing the mineral.
  • the process further comprises an additional step of treating the ground mineral-containing ore to separate the mineral from other components of the ore and to form a slurry of the mineral.
  • the particle size distribution of the ground mineral-containing ore produced in step (a) be 100% less than 100 micron.
  • the particle size of the ground mineral-containing ore produced in step (a) be less than 40 micron.
  • the particle size of the ground mineral-containing ore produced in step (a) comprises at least 50% of the particles being less than 10 micron.
  • the particle size of the ground mineral-containing ore produced in step (a) comprises at least 10% of the particles being less than 2 micron.
  • the size of the agglomerates produced in step (b) be 1 to 25mm.
  • size of the agglomerates produced in step (b) be 4.5 to 15 mm.
  • the moisture content of the agglomerates produced in step (b) be less than 15% at the time the agglomerates are fed to a fluidised bed roaster or a fluidised bed combustion furnace.
  • the moisture content of the agglomerates produced in step (b) be less than 13% at the time the agglomerates are fed to a fluidised bed roaster or a fluidised bed combustion furnace.
  • the moisture content of the agglomerates produced in step (b) be greater than 1% at the time the agglomerates are fed to a fluidised bed roaster or a fluidised bed combustion furnace.
  • the moisture content of the agglomerates produced in step (b) be greater than 5% at the time the agglomerates are fed to a fluidised bed roaster or a fluidised bed combustion furnace.
  • the compaction step (b) be carried out in a high pressure filtration apparatus.
  • a process for calcining a mineral concentrate comprising, feeding agglomerates of the mineral concentrate formed by the process described in the preceding paragraphs into a fluidised bed roaster or a fluidised bed combustion furnace, and calcining the agglomerates therein.
  • the figure is a graph which illustrates the particle size distribution of calcine produced from zinc sulphide concentrate in fluidised bed reactors from agglomerates formed by a range of different compaction processes, as summarised below.
  • Denver tube press to form ' agglomerates having a moisture content of 12% and a particle size distribution of 9.5 to 10 16mm;
  • the grain size distribution of the unagglomerated concentrate used to produce the samples was as follows:
  • the samples were calcined in either a 300mm diameter pilot plant fluidised bed roaster or a 70mm diameter bench scale fluidised bed roaster.
  • the fluidised bed roasters were found by the applicants to have similar fluidising conditions to the commercial Lurgi-type fluidised bed roasters discussed above and thus the results of the experimental work are indicative of the results that would be achieved in those Lurgi-type fluidised bed roasters.
  • the particle size distribution for samples b, c, and d and, to a lesser extent, sample e are within the preferred particle size distribution of 0.1 to 2mm for optimum operation of a Lurgi-type fluidised bed roaster.
  • sample b is particularly significant, and unexpected, because the particle size distribution of the input feed of agglomerates was in the range of 9.5 to 16mm, which is considerably larger than the upper limit of the preferred prior art particle size distribution for Lurgi-type fluidised bed roasters, and it was expected that, under normal circumstances, such large- sized agglomerates would not be fluidised and hence render the roasters inoperable.
  • sample e was prepared in view of concern that agglomerates of zinc sulphide concentrate may break-down into fines during transportation from an ore resource to a commercial fluidised bed roaster.
  • the result for sample e shows that re-agglomeration of shredded agglomerates produced agglomerates that had a satisfactory particle size distribution when calcined in a fluidised bed roaster.
  • sample b ii also illustrates the effect of moisture content on the agglomerates. Specifically, as is noted above, sample b ii was formed by re-wetting the dried agglomerate which had been used to produce sample a and thereafter re-forming this agglomerate to a moisture content of 12%. The results for sample b ii were the same as for sample b i and indicate that agglomerates can be re-wetted without loss of performance should the agglomerates be over-dried.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Environmental & Geological Engineering (AREA)
  • Materials Engineering (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Geology (AREA)
  • Metallurgy (AREA)
  • Manufacturing & Machinery (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Mechanical Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Processing Of Solid Wastes (AREA)
  • Glanulating (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)

Abstract

L'invention se rapporte à un procédé de production d'agglomérats d'un matériau d'apport destiné à un four de grillage à lit fluidisé ou un four de combustion à lit fluidisé. Le procédé consiste à broyer une charge de remplissage renfermant le matériau d'apport en une répartition granulométrique comprenant au moins une partie importante de fines, puis à compacter la charge de remplissage broyée afin de former des agglomérats.
PCT/AU1995/000156 1994-03-21 1995-03-21 Procede de production d'agglomerats Ceased WO1995025585A1 (fr)

Priority Applications (6)

Application Number Priority Date Filing Date Title
AU20621/95A AU704350B2 (en) 1994-03-21 1995-03-21 A process for producing agglomerates
EP95912963A EP0751821A4 (fr) 1994-03-21 1995-03-21 Procede de production d'agglomerats
JP7524253A JPH10500353A (ja) 1994-03-21 1995-03-21 凝集体の製造方法
FI963770A FI963770L (fi) 1994-03-21 1995-03-21 Prosessi agglomeraattien tuottamiseksi
MXPA/A/1996/004214A MXPA96004214A (en) 1994-03-21 1996-09-20 Process for the production of aglomera
NO964000A NO964000L (no) 1994-03-21 1996-09-23 En fremgangsmåte for å fremstille agglomerater

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AUPM4609 1994-03-21
AUPM4609A AUPM460994A0 (en) 1994-03-21 1994-03-21 A process for producing agglomerates

Publications (1)

Publication Number Publication Date
WO1995025585A1 true WO1995025585A1 (fr) 1995-09-28

Family

ID=3779224

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/AU1995/000156 Ceased WO1995025585A1 (fr) 1994-03-21 1995-03-21 Procede de production d'agglomerats

Country Status (9)

Country Link
EP (1) EP0751821A4 (fr)
JP (1) JPH10500353A (fr)
AU (1) AUPM460994A0 (fr)
CA (1) CA2186132A1 (fr)
FI (1) FI963770L (fr)
NO (1) NO964000L (fr)
TW (1) TW350791B (fr)
WO (1) WO1995025585A1 (fr)
ZA (1) ZA952315B (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1997041268A1 (fr) * 1996-04-29 1997-11-06 Cominco Ltd. Procede de grillage sur lit fluidise

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1514963A1 (de) * 1961-06-12 1969-09-04 Atomic Energy Authority Uk Verfahren zur Herstellung von Sphaeroiden aus einem Pulver,insbesondere aus Kernbrennstoff
DE2044707A1 (de) * 1969-09-11 1971-03-18 Veremgde Kunstmestfabneken Mekog Albatros N V , Utrecht (Niederlande) Verfahren zum Granulieren von pulver formigen Stoffen
US3738785A (en) * 1968-11-08 1973-06-12 Degussa Apparatus for processing of finely divided particulate materials
JPS5323797B1 (fr) * 1971-06-30 1978-07-17
DE2730941A1 (de) * 1977-07-08 1979-01-25 Loedige Maschbau Gmbh Geb Verfahren und vorrichtung zum granulieren von pulverfoermigem, faserigem, pastoesem oder breiigem gut
EP0100168A2 (fr) * 1982-07-06 1984-02-08 Alan George Rogerson Procédés de préparation de tablettes pour une technique modifiée de granulation humide
DE3734760A1 (de) * 1987-10-14 1989-05-03 Kloeckner Humboldt Deutz Ag Verfahren und anlage zur kompaktierung feinkoernigen gutes mit pelletierung

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1514963A1 (de) * 1961-06-12 1969-09-04 Atomic Energy Authority Uk Verfahren zur Herstellung von Sphaeroiden aus einem Pulver,insbesondere aus Kernbrennstoff
US3738785A (en) * 1968-11-08 1973-06-12 Degussa Apparatus for processing of finely divided particulate materials
DE2044707A1 (de) * 1969-09-11 1971-03-18 Veremgde Kunstmestfabneken Mekog Albatros N V , Utrecht (Niederlande) Verfahren zum Granulieren von pulver formigen Stoffen
JPS5323797B1 (fr) * 1971-06-30 1978-07-17
DE2730941A1 (de) * 1977-07-08 1979-01-25 Loedige Maschbau Gmbh Geb Verfahren und vorrichtung zum granulieren von pulverfoermigem, faserigem, pastoesem oder breiigem gut
EP0100168A2 (fr) * 1982-07-06 1984-02-08 Alan George Rogerson Procédés de préparation de tablettes pour une technique modifiée de granulation humide
DE3734760A1 (de) * 1987-10-14 1989-05-03 Kloeckner Humboldt Deutz Ag Verfahren und anlage zur kompaktierung feinkoernigen gutes mit pelletierung

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
DATABASE WPI Derwent World Patents Index; AN 1978-58067A *
See also references of EP0751821A4 *

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1997041268A1 (fr) * 1996-04-29 1997-11-06 Cominco Ltd. Procede de grillage sur lit fluidise

Also Published As

Publication number Publication date
MX9604214A (es) 1998-05-31
AUPM460994A0 (en) 1994-04-14
FI963770A0 (fi) 1996-09-23
NO964000D0 (no) 1996-09-23
NO964000L (no) 1996-11-20
JPH10500353A (ja) 1998-01-13
EP0751821A4 (fr) 1998-01-28
TW350791B (en) 1999-01-21
FI963770A7 (fi) 1996-11-21
ZA952315B (en) 1995-12-14
EP0751821A1 (fr) 1997-01-08
CA2186132A1 (fr) 1995-03-21
FI963770L (fi) 1996-11-21

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