NZ761110B2 - Liquid aeration - Google Patents
Liquid aeration Download PDFInfo
- Publication number
- NZ761110B2 NZ761110B2 NZ761063A NZ76106317A NZ761110B2 NZ 761110 B2 NZ761110 B2 NZ 761110B2 NZ 761063 A NZ761063 A NZ 761063A NZ 76106317 A NZ76106317 A NZ 76106317A NZ 761110 B2 NZ761110 B2 NZ 761110B2
- Authority
- NZ
- New Zealand
- Prior art keywords
- ore
- coarse
- flotation
- grade
- stream
- Prior art date
Links
- 238000005273 aeration Methods 0.000 title 1
- 239000007788 liquid Substances 0.000 title 1
- 238000005188 flotation Methods 0.000 claims description 84
- 238000000034 method Methods 0.000 claims description 64
- 239000002699 waste material Substances 0.000 claims description 56
- 238000000227 grinding Methods 0.000 claims description 23
- 239000011435 rock Substances 0.000 claims description 18
- 238000011084 recovery Methods 0.000 claims description 17
- 239000012141 concentrate Substances 0.000 claims description 16
- 239000000463 material Substances 0.000 claims description 13
- UCKMPCXJQFINFW-UHFFFAOYSA-N sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims description 7
- 238000004458 analytical method Methods 0.000 claims description 4
- 230000004913 activation Effects 0.000 claims description 3
- 229910052751 metal Inorganic materials 0.000 claims description 2
- 239000002184 metal Substances 0.000 claims description 2
- 150000002739 metals Chemical class 0.000 claims description 2
- 238000007619 statistical method Methods 0.000 claims description 2
- 238000002386 leaching Methods 0.000 claims 1
- 239000004753 textile Substances 0.000 abstract 8
- 239000004744 fabric Substances 0.000 abstract 2
- 239000000835 fiber Substances 0.000 abstract 2
- 230000035515 penetration Effects 0.000 abstract 2
- 230000003068 static Effects 0.000 abstract 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 34
- 239000004576 sand Substances 0.000 description 13
- 229910052500 inorganic mineral Inorganic materials 0.000 description 11
- 239000011707 mineral Substances 0.000 description 11
- 238000005065 mining Methods 0.000 description 11
- 239000002245 particle Substances 0.000 description 9
- 238000004519 manufacturing process Methods 0.000 description 8
- RYGMFSIKBFXOCR-UHFFFAOYSA-N copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 7
- 229910052802 copper Inorganic materials 0.000 description 7
- 239000010949 copper Substances 0.000 description 7
- 150000002500 ions Chemical class 0.000 description 6
- 238000000926 separation method Methods 0.000 description 6
- 238000000265 homogenisation Methods 0.000 description 5
- 238000011068 load Methods 0.000 description 5
- 210000004027 cells Anatomy 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 238000005422 blasting Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 230000005484 gravity Effects 0.000 description 3
- 230000002209 hydrophobic Effects 0.000 description 3
- 230000001965 increased Effects 0.000 description 3
- 230000000717 retained Effects 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- 241000602850 Cinclidae Species 0.000 description 2
- 229940035295 Ting Drugs 0.000 description 2
- 238000003066 decision tree Methods 0.000 description 2
- 230000001419 dependent Effects 0.000 description 2
- 238000005553 drilling Methods 0.000 description 2
- 238000006062 fragmentation reaction Methods 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 230000003134 recirculating Effects 0.000 description 2
- 230000001603 reducing Effects 0.000 description 2
- 230000002000 scavenging Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 150000004763 sulfides Chemical class 0.000 description 2
- 239000010878 waste rock Substances 0.000 description 2
- PHTXVQQRWJXYPP-UHFFFAOYSA-N Ethyltrifluoromethylaminoindane Chemical compound C1=C(C(F)(F)F)C=C2CC(NCC)CC2=C1 PHTXVQQRWJXYPP-UHFFFAOYSA-N 0.000 description 1
- 241000229754 Iva xanthiifolia Species 0.000 description 1
- 210000004940 Nucleus Anatomy 0.000 description 1
- 102100012174 PIWIL2 Human genes 0.000 description 1
- 101710043199 PIWIL2 Proteins 0.000 description 1
- 210000004761 Scalp Anatomy 0.000 description 1
- 210000000538 Tail Anatomy 0.000 description 1
- 238000007792 addition Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- DVRDHUBQLOKMHZ-UHFFFAOYSA-N chalcopyrite Chemical compound [S-2].[S-2].[Fe+2].[Cu+2] DVRDHUBQLOKMHZ-UHFFFAOYSA-N 0.000 description 1
- 229910052951 chalcopyrite Inorganic materials 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000011362 coarse particle Substances 0.000 description 1
- 230000001447 compensatory Effects 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 230000000875 corresponding Effects 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000002708 enhancing Effects 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 238000005755 formation reaction Methods 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 239000010931 gold Substances 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 239000011133 lead Substances 0.000 description 1
- 238000005007 materials handling Methods 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 238000009376 nuclear reprocessing Methods 0.000 description 1
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical group [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 1
- 238000004094 preconcentration Methods 0.000 description 1
- 230000002250 progressing Effects 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
- 230000002195 synergetic Effects 0.000 description 1
- HCHKCACWOHOZIP-UHFFFAOYSA-N zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
- 239000011701 zinc Substances 0.000 description 1
Abstract
spike resistant package (10) comprising a pouch (100) having an inner surface and an outer surface, and a first grouping (200) of spike resistant textile layer. The grouping has a first side (200a), a second side (200b), and comprises plurality of spike resistant textile layers (210). Each spike resistant textile layer comprises a plurality of interwoven yarns or fibers having a tenacity of about 14 or more grams per denier. The package further comprises a slip layer (300) having a thickness of less than about 0.1 mm, a stiffness of less than about 0.01 N-m, and a static coefficient of friction (COF) between the slip layer and the second side of the first grouping of less than about 0.40. The slip layer is located on the second side of the grouping of spike resistant textile layers. The pouch fully encapsulates the grouping of spike resistant textile layers and the slip layer, and the slip layer and the inner surface of the pouch are in direct and intimate contact. The invention provides a flexible light weight structure that resists penetration by spike-like threats, wherein the slip layer provides improved spike resistance compared with prior art multi layer fabric devices. esistant textile layer comprises a plurality of interwoven yarns or fibers having a tenacity of about 14 or more grams per denier. The package further comprises a slip layer (300) having a thickness of less than about 0.1 mm, a stiffness of less than about 0.01 N-m, and a static coefficient of friction (COF) between the slip layer and the second side of the first grouping of less than about 0.40. The slip layer is located on the second side of the grouping of spike resistant textile layers. The pouch fully encapsulates the grouping of spike resistant textile layers and the slip layer, and the slip layer and the inner surface of the pouch are in direct and intimate contact. The invention provides a flexible light weight structure that resists penetration by spike-like threats, wherein the slip layer provides improved spike resistance compared with prior art multi layer fabric devices.
Description
se the Vaiue of a Sulphide Ore Resource h Sequential
Waste Rejection
OUND TO THE INVENTION
de ores containing metais such as copper, gold, platinum group
metais, nickel, lead and zinc are recovered commerciaiiy by fine grinding
and flotation to concentrate the valuable component and discard the
The conventional process invoives grade control drilling to delineate the
ore, blasting the necessary waste (below economic cutoff-grade (00(3))
and ore, ioading trucks to haui the ore for primary crushing and the waste
to a. disposal area. The crushed ore is conveyed to a miiling process,
typicaliy using semi-autogenous grinding (SAG) or high pressure grinding
rolls (HPGR); foilowed by bali miiiing to fuily te the valuable particles
at a p80 of around 75—200 micron. Then the ore is separated using a
flotation process to produce a saleabie concentrate and taiiings. The
tailings from flotation are pumped to a taiiings storage facility (TSF) and
stored in perpetuity.
As the conventional process chain requires ali of the ore to be ground
finely, it consumes large quantities of energy (typicaliy ZOkwhl’t ore) and
water .0 tonne water per tonne of ore). The majority of this water is
lost in the fine tailings, where it is intimately mixed and retained with the
very fine residue produced from the conventional flotation process.
The shortage of available water in some ons has generated different
approaches to water . Some mines have instailed desalination piants
on the adjacent coast, and pumped the desaiinated water to the processing
faciiity. Others have led large filter presses to squeeze as much water
from taiiings as possible. However these solutions both suffer very high
capitai and operating costs. The high cost of fine grinding and high water
consumption aiso means the recovery efficiency of the in~ground resource
is limited to that which is economic to process.
At any particular time in the mine iife, the (DOS for ore is set to maximise the
feed grade and hence production from the avaiiabie processing capacity.
This CoG may be variously ained by available water, or tailings
capacity, or the ied processing capacity. Whichever constraint s,
economically attractive ore is often being rejected to a waste pile, simply
because higher grade materials are available at the time. Even if a low
grade stockpile is introduced to manage the material which is above
economic processing grade but beiow the 008 of the day, the materials
handling cost of stockpiling and reclaiming this marginally attractive
material iater in the mine life, impiies a fraction of the economic resource
wiil be lost to the waste rock piie.
If the run—ofnmine ore couid be ciated prior to fine ng, to reject
as waste material which is below economic -grade, with a high
recovery of the values and a reasonabiy high upgrade ratio, and in a
relatively low cost operation, the unit costs and consumption of water would
be reduced. The consequential grade of feed to processing wouid be
increased. And the grade of any stockpile required by a constraint to
avaiiable processing capacity would be higher, resuiting in improved
margins when eventuaily recovered.
Recognising the value associated with removing a fraction of the ore that is
below 606, and preferably beiow economic treatment grade, various
beneficiation techniques have been proposed. For sulphides, these are
y based around gravity techniques such as dense media separation,
spirais, etc, and rock sorting methods. But for most suiphide ores, these
ciation techniques iaii either the upgrade ratio/recovery or cost
hurdles for implementation.
if the beneficiation parameters are set to reject sufficient ore (i.e. achieve a
high upgrade ratio) to economically warrant the cost of the beneficiation
process, the loss of values is excessive. This means an increase in mining
cost per tonne of t, and a decrease in the ive utilisation of the
overall resource.
Hence run of mine (ROM) ores are conventionally ground to very fine sizes
to achieve te liberation of the valuabie components then d,
despite the obviously high cost of comminution and water consumption.
Recently, the ability to use a chemically based coarse flotation process for
beneficiating des, using a fit for purpose ion cell has been
ed by Eriez Flotation Division (EFD), a wholly owned subsidiary of
Eriez Manufacturing Co. Using this coarse flotation technology, the ability
to dry stack sand residue was recognised, thus opening up another
potential beneficiation technique to reduce water and energy
(W02016l170437). As a one off process for water recovery, it is very
useful, but due to particle size vs. ry constraints on coarse flotation,
and the size separation precision of hydrocyciones, only 30—50% of the ore
ends up as sand. Hence water consumptions and tailings volumes are
typically only reduced by some 25-40%.
in a second beneficiation technique for sulphidic ores, the differential
fracture along the mineraiised grain boundaries, causing most of the
sulphides to concentrate in'the finer size ranges, has been recognised.
The differential fracture s ing to reject the coarsest rocks,
which usually contain the lowest grade. This technique was first uced
in Bougainville in the late 19808 (Australasian institute of Mining and
Metallurgy, Papua New Guinea Minerai Development Symposium, 27-28
June 1986, Madang, The Application or Preconcentration by Screening at
Bougainville Copper Limited, Bums RS and Grimes AW, the content of
which is incorporated herein by reference). The beneficiation technique is
being actively reexamined by a number of operations under the CRC Ore
trademark of ‘Grade Engineering'. CRC ORE is a not for profit organisation
funded by the Australian Federal ment and the giobal ls
industry httg:!lwww.crcore.orgau/mainlindex. phpleatutions/grade
engineering.
And finally, beneficiating using bulk sorting has aiso been proposed. The
development of sensors that can adequately ine average grades on
a conveyor belt or shovel at a high rate, allows for the stream of broken
rock to be identified and diverted to either ore or waste. Reference: Valery
etai. World Mining Congress 2016; nse
http:/Iwww.minesensesomlgroducts :
The ShovelSenseTM shovel t is a real-time mineral telemetry and
decision support system for surface or underground ations. it is a
retrofit package installed in the dipper of surface shovels or into the scoop
of underground machines such as scooptrams or LHD’s. The
ShovelSense"M rm is used for:
Measurement of ore quality while material is being scooped into the
dipper;
Reporting of ore quality and type to the grade controi/ore routing
system
Realutime, oniine decision support for orelwaste dispatch decisions.
Buik sorting takes advantage of the natural heterogeneity of orebodies, with
the separation of zones of high and low grade material that would
conventionaliy be mixed into homogenised run~ot~mine ore. The weakness
of bulk sorting is it can only reject those zones that are low grade at the
time of sensing, and hence to retain an acceptabie upgrade ratio it must be
installed prior to significant homogenisation of the ore.
Despite these three recent and quite ct beneficiation techniques being
veiy well known, none has yet found widespread use in the mining
industry. This may be at least partialiy attributed to the same upgrade ratio,
recovery, and cost reasons that have hampered the implementation of
traditionai gravity based beneficiation.
in y, the mining industry is very l intensive, a iarge consumer
of water and energy, and oniy partialiy recovers the values contained in the
earth that is mined. Whilst beneficiation techniques are known which can
potentially address these , they have been considered in isolation to
resolve each constraint individually, and mostly found to be uneconomic.
SUMMARY OF THE lNVENTlON
According to the present invention there is provided an integrated process
for recovering vaiue metals from sulphide ore, including the steps of:
a) obtaining a crushed ore;
b) bulk sorting and screening the crushed ore to provide a
sortedlscreened coarse ore stream and a waste ore stream;
c) subjecting the sorted/screened coarse ore stream to ng in
a mill foliowed by classification to provide a coarse fraction
suitabie for coarse flotation and a first tine fraction le for
conventional flotation;
d) subjecting the coarse fraction suitable for coarse flotation to
coarse ion thereby to obtain a gangue and an intermediate
concentrate;
e) ting the intermediate concentrate to grinding to provide a
second fine traction suitable for conventions! flotation; and
f) subjecting the first fine fraction and the second tine fraction to
conventional flotation to provide a concentrate and tailings.
Preferably, blending of the crushed ore is limited, for example to a truck
load or shovel load, in order to limit homogenisation of the ore prior to step
At step a), the ore is preferably crushed to a size suitable for tation
on a or, as a feed to a subsequent grinding stage, and is typically in
the range of 5 to 40 cm.
The bulk sorting in step b) may be on a buik sorter comprising a conveyor
beit with a diverter mechanism controlled by a continuous analysis sensor,
wherein the diverter mechanism diverts low grade zones of rock which do
not meet a selected cut off grade (COG) to the waste stream. The
continuous analysis sensor preferabiy comprises a rapid scanning sensor,
preferably a ic resonance or neutron activation or X-ray sensor.
in step b), the crushed ore may be subjected to buik sorting followed by
screening or screening foliowed by bulk sorting.
Preferably, at step b), the d ore is subjected to bulk sorting to
provide a sorted coarse ore stream which is subjected in to grinding in step
c), and a first waste ore stream.
Advantageousiy. the sorted coarse ore stream is screened to provide a
ed coarse ore stream which is subjected to grinding in step c), and a
second waste ore stream.
Typicaiiy, the size of screen apertures of a screen used to screen the
coarse ore stream are selected to provide a ed coarse ore stream
that is about 80-90% by weight of the coarse ore stream from bulk sorting.
Preferably, at step b), the first waste stream is screened to provide a third
waste ore stream and a higher grade fraction that is sent for ng in the
grinder at step c) together with the sortedlscreened ore stream.
Typically, the size of screen apertures of a screen used to screen the first
waste ore stream are ed to recover from 15—25% by weight of the
stream.
At step c), the ore is ably ground in ciosed loop with a ciassification
circuit, to aliow scatping of material that is already reduced to the
appropriate size ranges for coarse and tional flotation.
2017/053963
At step c), the ore is preferably subjected to fication to e a
coarse fraction suitable for coarse flotation with a size of 100 pm up to 1000
pm, preferably 150 pm up to 800 pm, most preferably from 200 pm up to
600 pm, and a first fine traction suitable for conventional flotation with a
size of less than 100 pm, typicalty less than 150 pm, preferably less than
200 pm.
At step e), the intermediate concentrate is preferabty ground to a size of
less than 150 pm to provide a second tine fraction suitabie for tional
flotation.
Preferably, a natural grade recovery curves is determined for the ore, and
each of the following beneficiation steps:
i) buik sorting;
ii) ing;
iii) coarse flotation;
is arranged and controlled to permanently reject the maximum
quantity of waste at a grade fess than an economic cut-off—grade.
The beneficiation steps:
i) buik sorting;
ii) screening;
iii) coarse flotation;
may be further arranged and controlled to also separate a low grade
ore suitabte for stockpiiing or heap ng, and hence produce a
high grade feed to fitl the availabte comminution and conventional
flotation ty.
For the constraints of a particular mining asset, the design and set points
are further selected for each beneficiation step, to:
. optimise the production of the whoie mining and processing asset
system, within the constraints of water or taiiings storage capacity;
and l or
WO 34855
. optimise the capital costs of productive assets and infrastructure in
a new or expanded mine; and I or
. optimise the recovery of mineral vaiues from an orebody; and I or
. optimise the overall operating costs per tonne of product
by ultimateiy rejecting the maximum waste, at less than the economic cut
off grade (CoG) for retreatment.
Preferabiy, homogenisation is minimised prior to bulk sorting to maximise
the removal of gangue.
Screening may be used specificaily to scavenge the higher grade fines
from the reject stream of bulk g
Screening may aiso be used specificaiiy to scavenge the lower grade
coarse ai from the ore product stream of bulk sorting.
BRiEF DESCRIPTION OF THE DRAWINGS
Figure 1 is a flow diagram of a beneficiation process according to an
embodiment of the invention;
Figure 2 is a graph showing a grade tonnage curve for buik sorting of
a typical copper porphyry ore;
3 is a graph of the ing achievable by screening at
s proportions of a typicai copper porphyry ore
Figure4 is a decision tree for a typical process design for an
embodiment of the invention; and
Figure 5 is a graph iilustrating the ial impact of the process of
the present invention on power consumption, water
consumption, and tailings generation in comparison with a
conventional crushing, grinding and flotation process.
DESCRIPTiON OF PREFERRED EMBODIMENTS
The t invention relates to a process that capitaiises on the natural
heterogeneity of sulphide orebodies, and utilises beneficiation technologies
in a novel muttistage configuration to reject the maximum ty of waste
gangue prior to fine comminution. This rejected gangue is normally below
economic reprocessing grade (ie. waste) but might also be in the form of a
feed to heap leach; or in the form of a low grade stockpile for treatment
later in the mine life (grade profiling).
The exact quantum of benefits will be dependent on the grade recovery
characteristics of a particular orebody. However, using combination of the
techniques, the water and ution energy consumption are typically
reduced by 50-80% at the same mining cut—off—grade (CoG). Alternatively,
the mining cut«off—grade can be reduced. extending the life of mine, and
e only siightly lower reductions in overall water and energy
consumption. The invention also enables unit costs of production, capital
and operating, to be icantly reduced, and where appropriate the profile
of production to be brought forward to enhance the return on invested
A simplified block flowsheet of one embodiment of the invention is shown in
Figure 1. An orebody is mined 12 and fed to a primary crusher 14, from
where it is bulk sorted to to provide a sorted coarse ore stream 18 for
grinding and classifying 20 and a sorted waste stream 22. A screen 24
recovers a high grade finer fraction 26 from the sorted waste stream 22,
and this rejoins the high grade stream for grinding and classifying 20. If the
sorted coarse ore stream 18 from buik sorting 16 is sufficiently low grade, it
can be similarly ed 28 to reject the coarsest material 30 to the waste
or low grade stockpile 32. Classification splits the ore after partial grinding
into a coarse product stream 34 suitable for coarse flotation 36 and a fine
product stream 38 suited to proceed direct to flotation 40. The coarse
WO 34855
fiotation process 36 then rejects further gangue 42 to a sand iie 44,
with an intermediate concentrate 46 being reground 48 to proceed to
conventional ion 40. A concentrate 50 and tailings 52 are obtained
from the conventional flotation 40.
Thus, low grade materiai 32 and 44 is rejected from the sorter/screen
combination 16/24128, and from the coarse flotation 36, thus requiring only
a proportion of the original ore to be finely ground to achieve the full
liberation required to produce a saieable concentrate.
The variable nature of ore mineralogy and/or mine designs, means that
deportment of the values will be different at each mine. For e at
onal mines, it may be le to e the screening and bulk
sorting, whilst stili retaining the naturai ore heterogeneity. In this variant, the
fine al from screening would proceed to grinding, and the coarse
fraction would be bulk sorted to reject waste. The system design would be
such as to minimise homogenisation during sorting.
And for some mines with particularly attractive grade recovery curves for
one or two of the beneficiation techniques, it may be economicaily more
appropriate to utiiise only some of the components of the muiti-stage novel
processing chain that is the subject of this invention.
The grade recovery curve for bulk sorting is weii suited to waste removai,
providing the nature! spatial heterogeneity of the orebody is retained.
Screening is well suited to scavenging vaiues (the tines) from low grade
streams, but only for occasionai orebodies does the selective fracture
enable high recoveries and immediate rejection of waste. Coarse ion
is well suited to rejection of waste with a high recovery, albeit after partial
comminution.
First Comgonent —~ Bulk Sorting
The first component beneficiation step in the most common configuration of
this invention. is bulk sorting. Ore that has been fragmented by ng, is
transported by truck or conveyor to a primary crusher, and by conveyor to
grinding. On the conveyor either before or after the primary crusher, the
grade of the ore (or deieterious contaminants) can be anaiysed, using
techniques such as magnetic resonance, for example an cit—conveyor MR
Analyser for a species other than chaicopyrite being devetoped by CSERO
in collaboration with CRCOre, which will resuit in the veyor MR
technology attaining a TRL 4 for detection of setected non-chalcopyrite
mineral targets
httgzllwww.crcore.org.au/mainlimages/snagshotlgroiects/CRC-ORE~
Sna shot---Research~i.003-«Buik-sensin with-ma netic-resonance. cit-
or neutron activation, for example a cross belt analyser avaiiabie from
SODERN which makes use of a CNA (Controiled n er) using
an ical neutron source with stabilised emission
httg:liwww.sodern.comlsiteslenlret/Cross-belt—Anatyser 7t.htmi, aliowing a
decision to divert the stream of rock to ore or to waste. NA is a nuclear
process used for determining the concentrations of elements in a vast
amount of materials. CNA aliows discrete sampling of elements as it
disregards the chemical form of a sample, and focuses solely on its
nucleus.
By minimising homogenisation wherever possible in the materiais ng,
the high and tow grade zones of ore are retained almost . This point of
analysis for bulk sorting may be before or after the primary crushing
depending on the nature of fragmentation in blasting. But the bulk sorting
must be located prior to a SAG or bait mitt where biending and recirculating
loads ate the heterogeneity. Any ediate stockpiles between the
mine and the bulk sorter shouid aiso be avoided.
These zones of high and low grade rock, when loaded on the conveyor
belt, translate into corresponding iengths. Some sections along the iength
of the loaded conveyor belt are below the economic processing cut-oft:
grade, while others are made up from the high grade zones. Based on the
continuous sensor is, a diverter mechanism is used to divert those
iow grade lengths of rock, which do not meet the desired COG, to a
separate waste stream.
The typical grade tonnage curve for bulk sorting will be very dependent on
the orebody heterogeneity, Through retaining this natural zonai
heterogeneity and using a rapid scanning sensor, the effective sorting lot
size is considerably smalier than the typical 20~25rn grid used for
conventional in—pit grade control. (in conventions? grade l, everything
in this grid being averaged and deciared as either ore or waste). Thus, the
buik sorting process discriminates more accurately between waste and ore
than conventional grade l.
The quantity of rock that is below cut~off~grade, and hence can be d
from conventional ore can be estimated from gee-statistical analysis of drill
core. Assuming the rock is homogenised at the granularity of a 300i truck
delivered to the conveyor, a grade tonnage curve is iilustrated in Figure 2,
for a typical copper orebody in Chile, illustrates that up to 25% of the run-
of—rnine ore can be rejected as waste.
An even more amenable Piatreef pgm ore from South Africa can yield up to
40% waste rejection at below the processing COG. Similarly, a reasonably
homogeneous porphyry copper RoM from Peru, can yield up to 20% waste
at beiow the 0.25% COG.
Optionally, the process can be configured such that one stream from the
first diverter can be further , using a second diverter system. This
technique can be used to create three fractions (high grade stream for
immediate processing: and lower grade stream of ore to be iled, or
heap d: and a waste stream). This grade ing technique is idealiy
suited where mining costs are modest relative to processing, and the
orebody is iarge enough to warrant ting of the lower grade on at
some later date. if water is highiy constrained, this enabies high production
in early years (grade profiling) within an available water constraint.
sing the ievei of ng that occurs prior to this bulk sorting sensor
and diverter is important to maximise the rejection of low grade ore. The
partially blended lot size (eg. a truckload) that can be analysed and
diverted is r than that achievable with the spacing of normal grade
control drilling. Due to natural orebody heterogeneity, a significant
proportion of the conventional RoM feed is below the mine COG, and can
be diverted to waste or assigned to a tow grade stockpile.
This eariy rejection of a waste stream that would otherwise be processed
as ore, has implications for both resource utilisation and costs. The waste is
no longer ground (energy savings) and is stored dry (water savings). The
separation efficiency of bulk g is better than grade controi driiling and
seiective loading, so that this grade control activity can be limited to
delineating the ultimate pit shell, saving r costs and simplifying mining
activities. The removal of waste means that unit costs of processing are
reduced. and hence a lower COG can be used for this ultimate pit shell.
Thus the l utiiisation of the resource ent can be ed.
Second Component - Screening
in the second component of the muitiple beneficiation steps that make up
this invention, one or both of the waste and ore streams from butk sorting
are screened. Sulphide ores selectively re along the mineralised grain
boundaries during biasting and crushing. As such the finest fraction of the
rocks in any ore zone will be of a higher grade.
If an ore exhibits a significant selectivity, the waste stream from the bulk
sorting is screened to further separate the higher grade, finer fraction.
These smaller rocks, are inciuded in the ore stream. An example of this is
shown in Figure 3 for a reasonably selective Chilean copper ore, where the
finest 10—20% of the ore. typically exhibits around twice the grade of the
remaining 8043096 of the ore. Thus a screening process is used to
scavenge those fines, which are higher than the processing cut~off-grade.,
from the reject stream from bulk sorting. As such, the grade of the waste
discard stream is further reduced, thus improving overall resource recovery.
Depending on the particular grade recovery curves for any ore, the set
points for each beneficiation process can be selected to optimise the waste
rejection by the overall butk sorting/screening system.
Depending on the selectivity of fracture of the particutar ore, this ing
will lly require a screen re to recover around 15-25% by weight
of the low grade stream. The coarse fraction proceeds to waste.
The high grade ore stream from primary crushing also contains a mix of
rock sizes. Due to selective fracture that occurs in blasting, and any
crushing undertaken prior to the bulk sorting, the highest grade is
concentrated in the finer fraction of rock. Removal of the lower grade
coarsest rocks by screening can result in further upgrading of the feed to
comminution. Whilst it may be unusual for such coarse material in the reject
stream to be below economic processing grade, this fraction may be well
suited to heap leach or low grade stockpile.
lf screening of the coarsest rocks is applicable, the high grade fines stream
will typically be around 80-90% of the total feed from bulk g. However
for those ores where selective fracture is not nced, this high grade
ing will not produce a sufficient grade differential to warrant the lower
grade coarse al being rejected, and hence the screening of the bulk
sorted ore will simply not be implemented.
The combined system of bulk sorting and screening of the high and low
grade streams will have different optimum set-points for each ore to be
d, and for the economic drivers of each mine. lt is apparent to those
skilled in the art, that the set-points of the system can readily be optimised
to produce the maximum grade for comminution, while rejecting the
maximum rock that is at or below the ic cut-off~grade for
processing.
Third Component — Coarse Flotation
The third stage of the multistage beneficiation is coarse particle flotation.
This process utiiises the heterogeneity at the sand (sub 1mm) size level, for
a chemically assisted gravity separation. The partially ground ore is
classified to produce a sand fraction, which is beneficiated using a fit for
purpose flotation machine such as the Erie}:TM Hydrofioat. The Eriez
Hydrofioatm, s out the concentration process based on a combination
of fluidization and flotation using fiuidization water which has been aerated
with micro—bubbles of air. The flotation is carried out using a suitable
tor and collector concentrations and residence time, for the particuiar
mineral to be floated. At this size, the ore is sufficientiy ground to liberate
most of the gangue and expose but not necessarily fully liberate the
valuable l grains. The coarse ion recoveries of ily exposed
mineralisation is high, and the residual gangue forms a sand which does
not warrant further comminution and conventional flotation. The reject sand
from coarse flotation can be stacked and d to recover water.
The system used to select a suitabiy sized feed for coarse flotation utilises
ciassitication devices such as cyciones or hydraulic classifiers to scalp that
fraction of the stream that is suited to tional flotation. in a typical
configuration for this third beneficiation ent, the material at a size
less than the upper size iirnit for coarse flotation is separated from the bait
miil circulating toad. This stream can then be further fied to separate
the materiai that is y ground to below the lower bound for coarse
flotation, and this finer fraction is sent directly to conventionai flotation. This
creates the feed to coarse flotation at a size in which the residue which is
‘free draining’.
in the normai configuration, the coarse flotation size range wiil be bounded
by the maximum size where the vaiuabie minerals are sufficiently exposed
to be floated, with ient recoveries such as to produce a sand residue
suitable to discard. The minimum size is set by the particle size at which
the coarse fiotation machine can operate efficiently to e a free
draining sand for disposal. Depending on the mineralogy, the fracture
characteristics of the ore, and the design of the classification circuit; this
lower size range is typically around 0 microns, and the upper size is
typically between 350 and 600 micron. ing on the size range for
coarse flotation, and the classification efficiency. this scalping captures for
coarse flotation between 40—60% of the total feed to comminuticn, with the
remainder reporting to conventional flotation.
in a conventional froth fiotation process, particle sizes are typicaily fess
than 0.1 mm (100 pm). The ore les is mixed with water to form
a slurry and the d mineral is rendered hydrophobic by the addition of
a surfactant or coilector chemicai. The particular chemical depends on the
nature of the mineral to be recovered. This slurry of hydrophobic particles
and hydrophilic particles is then introduced to tanks known as flotation
cells that are aerated to produce bubbles. The hydrophobic particles attach
to the air bubbles, which rise to the e, forming a froth. The froth is
removed from the calf, producing a concentrate of the target mineral.
Frothing agents, known as frothers, may be uced to the slurry to
promote the formation of a stable froth on top of the flotation cell. The
minerals that do not float into the froth are ed to as the flotation
tailings orflotation tails. These tailings may also be subjected to further
stages of flotation to recover the le particles that did not float the first
time. This is known as scavenging.
The undersize from the classification is ideally sized for conventional
flotation, as it does not suffer significantly from the poor recoveries that
most conventional flotation exhibits with particles above around 200 micron.
The oversize from the initiai classification of the bail mill recirculating load
(above the upper bound ed for coarse flotation) is recycled for further
comminution. Due to the extended size range that is scalped, the
comminution energy is significantly reduced.
The sand residue from coarse flotation has a tow exposed sulphide content.
it represents 7043096 of the scalped coarse flotation feed. It has a
sufficiently high lic conductivity and can be hydrautically stacked and
drained to recover the water.
The intermediate concentrate produced by coarse flotation is the remaining
-30% of the coarse flotation feed. This requires regrinding to fully te
the minerals, prior to conventional flotation in either the rougher n of
conventional flotation along with the fines fraction from the ball mill
classification, or direct to the conventional cteaner cells.
in a variant to coarse flotation, the size fraction of the feed to coarse
flotation can be widened at the upper end to say 0.84.5mm. This variant of
the invention is typically utilised when the throughput of the overall mine is
constrained by the fine grinding, conventional flotation, or taiiings storage
process, including total ble water to the mine. in this t, a greater
proportion of the ball mili ulating load is scalped and ciated,
aibeit that the coarse fraction of the coarse flotation residue will not be of a
grade that can be discarded directly. Some but not most of the coarsest
feed material has d sulphide surfaces that will float. Thus the coarse
fraction is liy denuded of its values, albeit not sufficiently to justify
immediate assignment as waste." 80 the overall residue from coarse
flotation, is further classified to separate the partiatly denuded coarse sand
that is above the normally selected upper bound for optimum recovery in
coarse flotation. This partially denuded coarse material can then be dry
stacked for processing tater in the mine life. In this t the throughput
capacity of the ball mills is further increased, and the consequential grade
profiling enables higher production from conventional flotation early in the
mine tife.
Integration of the Beneticiation System
WO 34855
By configuring bulk sorting and screening and coarse flotation, the benefits
of zones of high and low grade ores, and the differential deportment of
mineral values during fragmentation, and the selective liberation and
separation of gangue, are synergistic. Bulk sorting utilises the naturai
heterogeneity at the ore zone level. Screening captures the natural
heterogeneity at the individual rock level. And coarse fiotation captures the
heterogeneity at the sand level. The sequential steps are also
compensatory, in that there can be a second, modest cost, backstop to
avoid ent al of values that may have found their way into the
wrong stream in a prior beneficiation step, and reject gangue which has
been misplaced into the values .
Whilst the stage beneficiation process may be configured in s
ways, the most economic decision for a long life mine is usually to
maximise production from existing assets. The decision tree illustrated for
this case in Figure 4, is an example of the design ples that can be
applied, and the associated rational for selection of set-points.
In Figure 4, the reference numerals indicate: 80 mine, 82 is the Ore above
Processing 008?, 64 No, 66 Yes, 68 Waste, i’O Bulk Sort to reject waste,
72 Screen to scavenge vaiues, 74 Set points are seiected (bulk sensor
setting and screen size) to maximize the waste rejection at a grade below
ic 008, 78 is the available tonnage > processing capacity?, 78
Yes, 80 No, 82 Second stage bulk sort r screen), 84 Classification
and CPF, 86 Conventionai flotation, 88 Low grade stockpiie, 90 is
throughput further constrained eg. water/tailing?, 92 Yes, 94 No, 98
Classification to recover oversize, 98 Set points are selected for
classification sizes to maximise grade and tonnage to conventional flotation
whilst maintaining high i processing recovery.
The exact distribution of beneficiation steps and their set~points for every
orebody and every optimised business case will be different. As an
example, Figure 5 iliustrates the potential impact on power consumption,
water consumption, and tailings generation in an atternative configuration of
the invention which is directed to increasing mine life, whiist continuing to
save water and energy and increase production. Through the ion, a
proportion of what would be ently discarded in—pit and expanded pit
mineraiised waste in a conventionai mine, is now converted to ore (i_e.
above the economic CoG). The expanded source of ore is sorted and
screened to reject a substantive fraction of the ore as a waste (‘in pit waste
rock' which is below the economic processing CoG). CPF rejects further
waste as dry stacked sand, thus the quantity of ore progressing to fine
comminution for conventional flotation is considerably d. Since most
of the energy and water consumption is attributable to the requisite amount
of fine grinding required for conventionai flotation (illustrated by the height
of the tailings bar), the water and energy consumption per unit of product is
more than halved, and the tits of the resource is extended.
in summary, by combining the three ciation processes, each of which
relies on a different form of ore geneity; the invention achieves a
greater recovery of the vaiues in an orebody through reducing the
processing cut-off-grade, and enables more of the gangue to be discarded
in dry form, and the potentiai for a low grade ore to be stockpiied prior to
fine grinding later in the mine life. This in turn reduces the water
consumption and comminution energy, and reduces the amount of taiiings
generation to a modest proportion of the originai ore. The resultant
operating costs are reduced, and capital productivity of the processing
facilities is much enhanced.
ages of the process of the present ion are:
. Requirements for grade control activities in pit are minimised,
enabling simpier .
- The grade of ore to grinding may be sed by more than 10%,
and more preferably by 20% and most preferably by more than
%.
. The te economic cutoff-grade for mining of an orebody may
be reduced by more than 10% and preferably by more than 20%,
and more preferably by more than 30%.
. The total amount of fine tailings ed from the conventionai
run-of—mine ore may be reduced to tess than 50% of those resutting
from conventionat processing technology, and preferably less than
40%, and even more preferably iess than 30%.
. The totat amount of energy used in ution may be reduced to
less than 50% of that resulting from conventional processing, and
preferably less than 40%, and even more preferably less than 30%.
. The total amount of water consumed in taitings may be reduced to
less than 50% of those resulting from conventional processing, and
preferably less than 40%, and even more preferably less than 30%.
Claims (22)
1. An integrated process for recovering value metals from sulphide ore, including the steps of: a) obtaining a crushed ore; b) bulk sorting and screening the d ore to provide a /screened coarse ore stream and a waste ore stream; c) subjecting the sorted/screened coarse ore stream to ng in a mill followed by classification to provide a coarse fraction suitable for coarse flotation and a first fine fraction suitable for conventional flotation; d) subjecting the coarse fraction suitable for coarse flotation to coarse flotation thereby to obtain a gangue and an intermediate concentrate; e) subjecting the intermediate concentrate to grinding to provide a second fine fraction suitable for flotation; and f) subjecting the first fine fraction and the second fine fraction to conventional flotation to provide a concentrate and tailings.
2. The process claimed in claim 1, wherein, at step a), the ore is crushed to a size suitable for presentation on a conveyor, as a feed to grinding stage at step c).
3. The process claimed in claim 2, wherein, at step a), the ore is crushed to a size in the range of 5 to 40 cm.
4. The process claimed in any one of claims 1 to 3, wherein bulk g in step b) is on a bulk sorter comprising a conveyor belt with a diverter mechanism controlled by a continuous is , wherein the diverter mechanism diverts low grade zones of rock which do not meet a selected cut off grade (CoG) to the waste stream.
5. The process claimed in claim 4, wherein the continuous analysis sensor comprises a rapid scanning sensor.
6. The process claimed in claim 5, n the sensor is a magnetic resonance or neutron activation or an X-ray sensor.
7. The process claimed in any one of claims 4 to 6, wherein the cut off grade (CoG) is determined from geo-statistical analysis of drill core from the source of the ore.
8. The process claimed in any one of claims 1 to 7, wherein, at step b), the crushed ore is ted to bulk g followed by screening or screening followed by bulk sorting.
9. The process claimed in any one of claims 1 to 8, wherein, at step b), the crushed ore is subjected to bulk sorting to provide a sorted coarse ore stream, which is subjected in to grinding in step c), and a first waste ore stream.
10. The process d in claim 9, wherein the sorted coarse ore stream is screened to e a screened coarse ore stream, which is subjected to grinding in step c), and a second waste ore .
11. The process claimed in claim 10, wherein the size of screen apertures of a screen used to screen the coarse ore stream are selected to provide a screened coarse ore stream that is about 80- 90% by weight of the coarse ore stream from bulk sorting.
12. The process claimed in claim 10 or 11, wherein, at step b), the first waste stream is screened to provide a third waste ore stream and a higher grade fraction that is sent for grinding in the grinder at step c) er with the sorted/screened ore stream.
13. The process claimed in claim 12, wherein the size of screen apertures of a screen used to screen the first waste ore stream are selected to r from 15-25% by weight of the stream.
14. The process d in any one of claims 1 to 13, wherein, at step c), the ore is ground and classified to separate a size of less than 1000 micron.
15. The process claimed in any one of claims 1 to 14, wherein, at step c), the ore is ground in closed loop with a classification t such that material that is already reduced to the appropriate size ranges for coarse and conventional flotation can be scalped.
16. The process claimed in claim 15, wherein, at step c), the ore is subjected to fication to provide a coarse fraction suitable for coarse flotation with a size range of 100 µm up to 1000 µm, and a first fine fraction suitable for conventional flotation with a size of less than 100 µm.
17. The process claimed in claim 16, wherein, at step c), the ore is subjected to classification to provide a coarse fraction suitable for coarse flotation with a size range of 150 µm up to 1000 µm, and a first fine fraction suitable for conventional flotation with a size of less than 150 µm.
18. The process claimed in claim 17, wherein, at step c), the ore is subjected to classification to provide a coarse on le for coarse flotation with a size range of 200 µm up to 1000 µm, and a first fine fraction suitable for conventional flotation with a size of less than 200 µm.
19. The process claimed in any one of claims 1 to 18, wherein, at step e), the intermediate concentrate is ground a size of less than 150 µm to provide a second fine fraction suitable for conventional flotation.
20. The process claimed in any one of claims 1 to 19, in which natural grade recovery curves are ined for the ore, and each of the following ciation steps: iv) bulk sorting; v) screening; vi) coarse flotation; is arranged and controlled to permanently reject the maximum quantity of waste at a grade less than an economic f-grade.
21. The process claimed in claim 20, in which the beneficiation steps iv) bulk sorting; v) screening; vi) coarse flotation; are further arranged and controlled to also te a low grade ore suitable for stockpiling or heap leaching, and hence produce a high grade feed to fill the available comminution and conventional flotation capacity.
22. The process as claimed in claim 1, substantially as herein described with reference to any one of the
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PCT/US2017/039398 WO2019005004A1 (en) | 2017-06-27 | 2017-06-27 | Liquid aeration |
Publications (2)
Publication Number | Publication Date |
---|---|
NZ761063A NZ761063A (en) | 2021-10-29 |
NZ761110B2 true NZ761110B2 (en) | 2022-02-01 |
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