Note: Descriptions are shown in the official language in which they were submitted.
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APPARATUS AND METHOD FOR
SEPARATING/MIXING PARTICLES/FLUIDS
This application claims priority on
Canadian Patent Applications No. 2,421,246, filed
on February 12, 2003, No. 2,419,451, filed on
February 21, 2003, and No. 2,435,086, filed on
July 18, 2003.
BACKGROUND OF THE INVENTION
1. Field of the Invention
The present invention generally relates to
the separation and mixing of particles and, more
specifically, to a dry particle stream
separator/mixer and methods for separating particle
streams into particle groups and for mixing/treating
particle groups.
2. Background Art
Previously known techniques and methods are
currently used for the separation of aggregates into
particle groups. For instance, gravity classifiers,
inertial Classifiers, centrifugal classifiers, and
cyclone separators are well known and used
technologies. Amongst other patents, Canadian Patent
No. 2,257,674, issued on January 7, 2003 to
Cordonnier et al., discloses an air classifier with
centrifugal action. Canadian Patent Applications
No. 2,068,935 (by Tyler et al.) and 2,294,829 (by
Gruenwald) respectively describe an air separator and
an air classification of water-bearing fruit and
vegetable ingredients for peel and seed removal and
3o size discrimination.
Another known separation method is gravity
separation by elutriation. In this process, a
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predetermined particle group is lifted by an airflow
against the force of gravity. A finer particle group
is collected by an upwardly positioned collector,
whereas coarser particles overcome the airflow to~be
collected at a downwardly positioned collector. The
velocity of air has a direct effect on the particle
group that is collected by the upwardly positioned
collector.
This previously described method is a dry
l0 process, in that the fluid used for the separation is
not in a liquid phase. Such systems are advantageous
in that no liquid is polluted in the separation
process. The cleaning of liquids after particle
separation is a costly process, and this results in a
clear cost-efficiency advantage for dry processes.
SUMMARY OF INVENTION
It is therefore an aim of the present
invention to provide a novel apparatus for separating
a particle stream into particle groups.
It is a further aim of the present
invention to cause a dilution of a particle stream to
enhance the separation of the particle stream into
particle groups.
It is a further aim of the present
invention to provide a novel apparatus for mixing
particle groups into a particle stream.
It is a further aim of the present
invention that the apparatuses for separating a
particle stream into particle groups, and for mixing
particle groups into a particle stream use minimum
space and air volume so as to be cost and space
efficient.
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It is a further aim of the present
invention to provide a novel method for separating
particle streams into particle groups.
It is a further aim of the present
invention to provide a novel method for mixing
particle groups.
It is a further aim of the present
invention to reduce a need for conventional dust
collection systems.
A few factors are considered in creating
separation equipment. For instance, it is desired
that the amount of fluid used in the process be kept
low. The fluid that is used for the separation will
lose the particles it carries in suspension by
settling.
Also, the.separation is a. sub-process of
larger processes, and is often performed in limited
space areas with the larger process. It is therefore
desired to keep the dry-separation equipment as space
efficient as possible.
Therefore, in accordance with the present
invention, there is provided an apparatus for
separating a particle stream into particle groups,
comprising a dilution treatment chamber defining an
upstanding channel having a particle inlet at a top
end, and a first-particle group outlet at a bottom
end, the channel being adapted to receive a particle
stream at the particle inlet such that the particle
stream falls toward the first-particle-group outlet;
a , transfer casing adj acent to the dilution treatment
chamber and defining a transfer chamber adapted to
receive a second particle group; at least one second-
particle-group outlet laterally positioned with
respect to the channel of the dilution treatment
chamber and allowing fluid communication between the
transfer chamber and the channel; a distributor in
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the channel between the particle inlet and the at
least one second-particle-group outlet, for breaking
down the particle stream and distributing the
particle stream over a surface area of the channel;
and at least one fluid flow aperture in the dilution
treatment chamber and below the distributor, adapted
to create a fluid flow between the transfer chamber
and the channel so as to entrain a second particle
group from the channel through the second=particle-
l0 group outlet to the transfer chamber with a first
particle group remaining in the channel for exiting
through the first-particle-group outlet, the
apparatus being adapted to be connected to a positive
pressure source to create the fluid flow.
Further in accordance with the present
invention, there is provided a method for separating
a particle stream into particle groups, comprising
the steps of:, i) breaking down the particle stream
by subjecting the particle stream to lateral forces;
ii) vertically diluting the particle stream by
directing the particle stream to a falling condition;
iii) entraining a particle group away from a
remainder of the particle stream by creating a fluid
flow of predetermined magnitude across the particle
stream in said falling condition; and iv) collecting
the particle group and the remainder of the particle
stream at separate locations.
Still further in accordance with the
present invention, there is provided an apparatus for
at least one of mixing and treating particle and/or
fluid streams, comprising a dilution treatment
chamber defining an upstanding channel having an
inlet at a top end, and an outlet at a bottom end,
the channel being adapted to receive said particle
and/or fluid streams at the inlet such that said
particle and/or fluid streams fall toward the outlet;
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at least one fluid flow aperture in the dilution
treatment chamber, adapted to create a generally
lateral flow of at least one of a fluid and particle
jet within the channel to create a turbulence in the
channel for at least one of mixing said particle
and/or fluid streams and treating said particle
and/or fluid streams , whereby a mixture and/or
treated matter will exit the channel at the outlet;
and a positive pressure source connected to the fluid
l0 flow aperture to create the lateral flow of the at
least one of the fluid and the particle jet.
Still further in accordance with the
present invention, there is provided a method for at
least one of treating and mixing particle and/or
fluid streams, comprising the steps of:
i) vertically diluting particle and/or fluid streams
by directing particle and/or fluid streams to a
falling condition; ii) creating a lateral flow of
fluid and/or a particle jet across the particle
and/or fluid streams in said falling condition for at
least one of mixing the particle and/or fluid streams
by a turbulence resulting from the lateral flow of
fluid and/or particle jet, and treating said particle
and/or fluid streams; and iii) collecting the mixture
and/or treated matter below the lateral flow.
BRIEF DESCRIPTION OF THE DRAWINGS
Having thus generally described the nature
of the invention, reference will now be made to the
accompanying drawings, showing by way of illustration
a preferred embodiment thereof and in which:
Fig. 1 is a schematic view of an apparatus
,for separating a particle stream in accordance with a
preferred embodiment of the present invention, and of
a method for separating the particle stream;
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Fig. 2 is a perspective view of the
apparatus in accordance with a preferred embodiment
of the present invention;
Fig. 3 is a further perspective view of the
apparatus of Fig. 1;
Fig. 4 is a perspective view of a nozzle to
be used with the apparatus of the first embodiment;
Fig. 5 is a perspective view of the
apparatus in accordance with a second embodiment of
the present invention;
Fig. 6 is a perspective view of a lateral
particle separator to be used with the apparatus of
the second embodiment;
Fig. 7 is a perspective view of a
recuperator tray of the apparatus;
Fig. 8 is a schematic view of an impeller
used to create horizontal dilution and separation of
a particle stream in accordance with an alternative
embodiment of the present invention;
Fig. 9 is a schematic view of a laterally
reciprocating strainer in accordance with a further
alternative embodiment of the present invention; and
Fig. 10 is a schematic view of an apparatus
for separating a particle stream in accordance with a
still further alternative embodiment of the present
invention.
DESCRIPTION OF THE PREFERRED EMBODIMENTS
It is pointed out that the present
invention is associated with the separating and
mixing of particles. The term particle stream is
broadly used herein to designate a mass of particles,
granules, pellets, and other elements of different
mass and volume gathered together. Various uses of
the present invention are, defined hereinafter, far
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which the mass that is separatedjmixed is referred to
as particle stream, unless stated otherwise.
Referring to the drawings, and more
particularly to Fig. 1, an apparatus for separating a
particle stream into particle groups is generally
shown at 10. The apparatus 10 has a dilution
treatment chamber 12, a transfer casing 13 adjacent
to the dilution treatment chamber 12, nozzles 14
serially mounted on the dilution treatment chamber
12, and a pretreatment module 15. It is pointed out
that the nozzles 14 are affixed with letters in
various figures, whereby reference to the nozzles 14
will relate to all nozzles (e.g., nozzles 14A, 14B
and 14C), while reference to a specific one of the
nozzles will include an affixed letter.
The dilution treatment chamber 12 performs
a dilution of a particle, stream by gravity, and hosts
a step of separation of the particle stream into
particle groups.
The transfer casing 13 is in fluid
communication with the dilution treatment chamber 12
and receives a 'particle group separated from the
remainder of the particle stream in the dilution
treatment chamber 12.
The nozzles 14 are used to inject fluid (to
be discussed hereinafter) which breaks down the mass
of particle stream andjor enhance the dilution of the
particle stream in the dilution treatment chamber 12.
Moreover, the nozzles 14 are used to inject fluid
which separates the particle stream into the particle
groups.
The pretreatment module 15 is used to guide
and accelerate the particle stream toward the
dilution treatment chamber 12, such that the particle
stream will have some velocity. The velocity will
cause a horizontal dilution of the particle stream.
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DILUTION TREATMENT CHAMBER 12
Referring concurrently to Figs. 1, 2 and 3,
the dilution treatment chamber 12 is shown having an
upstanding elongated shape, and defines a vertical
channel 20 of rectangular cross-section. Although a
rectangular cross-section is described, any other
suitable cross-section shapes are contemplated. The
channel 20 has an inlet 21 at a top end thereof and
an outlet 22 at a bottom end thereof. The dilution
treatment chamber 12 shares a wall 23 with the
transfer casing 13. Lateral outlets 2~ are provided
in the wall 23, such that the dilution treatment
chamber 12 and the transfer casing 13 are in fluid
communication. Moreover, the dilution treatment
chamber 12 may vary in cross-sectional dimensions.
For instance, appropriate translating mechanisms may
be provided so as to increase/decrease a length or
width of the cross-section parameters of the dilution
treatment chamber 12.
The dilution treatment chamber 12 also has
pressure-differential apertures 25' (herein' three
apertures, i.e., fluid flow apertures), two of which
are horizontally opposite the lateral outlets 24 in
the wall 23.
TRANSFER CASING 13
Referring concurrently to Figs. l, 2 and 3,
the transfer casing 13 defines an .inner transfer
chamber 30. The inner transfer chamber 30 has a
funnel-shaped outlet 31 at a bottom end thereof, so
as to collect a particle group in suspension in the
transfer chamber 30.
Referring to Fig. 5, a lateral particle
separator 60, in accordance with another embodiment
of the present invention, is received in the transfer
chamber 30 of the transfer casing 13. The lateral
particle separator 60 will be described in further
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detail hereinafter, and is used to cause a further
particle group separation.
NOZZLES 14
Referring concurrently to Figs l, 2 and 3,
the nozzles 14B and 14C are positioned opposite the
lateral outlets 24 of the dilution treatment chamber
12. The nozzles 14, in a preferred configuration,
are connected to a pressure source so as to inj ect a
gaseous fluid (e. g:, air or any other suitable gas,
whereby reference will. be made non-restrictively
hereinafter to air or gaseous fluid) into the channel
of the dilution treatment chamber 12.
Referring to Fig. 4, one of the nozzles 14
is illustrated in greater detail. The nozzle 14 has
15' an inlet 40, by which it is connected to a pressure
source, and an outlet 41 of elongated rectangular
shape. The nozzle 14 has a diffusing body 42 between
the inlet 40 and the outlet 41.
In a preferred embodiment of the present
20 invention, the diffusing body 42 has an accumulator
portion 43 connected to the inlet 40, arid tapered
diffusing sectors 44 between the accumulator portion
43 and the outlet 41. The diffusing sectors 44 are
used in order to create a substantially uniform
diffusion of air~out of each of the nozzles 14.
A gate 45 is displaceable vertically for
the adjustment of the height of the outlet 41. A
connection flange 46 is used to secure the nozzle 14
to the dilution treatment chamber 12 opposite the
pressure-differential apertures 25. It is also seen
in Figs. 2 and 3 that the gate 45 can be accessed
from an exterior of the apparatus 10, thereby
enabling the rapid adjustment of the outlet size of
the nozzles 14 from an exterior of the apparatus 10.
The above-described configuration of the
nozzle 14 enables a high-pressure, low-volume output
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of gaseous fluid into the dilution treatment chamber
12 to produce a high impact on the particle stream.
Accordingly, the output of gaseous fluid will
decelerate at a high rate, so as to entrain in some
instances described hereinafter a given particle
group out of the dilution treatment chamber 12, and
to avoid enhancing turbulence in the transfer chamber
30. Such turbulence would slow down the settling
process in the transfer chamber 30, for instance, if
the apparatus 10 were used for classifying particle
groups.
PRETREATMENT MODULE 15
Referring concurrently to Figs. l, 2 and.3,
the pretreatment module 15 is positioned at the inlet
21 of the dilution treatment chamber 12. The
pretreatment module 15 conveys the particle stream
from a particle stream source, such as conveyor C, to
the inlet 21 of the dilution treatment chamber 12.
More specifically, the pretreatment module 15 will be
used to produce specific inlet conditions for the
particle stream.
In a preferred embodiment of the present
invention, the pretreatment module 15 has a slide 50,
sloping downwardly towards the inlet 21 of the
dilution treatment chamber 12. A deflector 51 is
positioned between the slide 50 and the inlet 21 of
the channel 20. The deflector 51 has a generally
horizontal launch surface, but may also be oriented
otherwise. As seen in Figs. 2 and 3, the slide 50
tapers towards the inlet 21 of the dilution treatment
chamber 12, so as to have an outlet width generally
equal to the inlet width of the channel 20 of the
dilution treatment chamber 12. The slide 50 is
preferably provided with guiding rails 52 (Figs. 2
and 3). The particle stream reaching the slide 50 is
preferably uniformly distributed toward the inlet 21
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of the dilution treatment chamber 12, and the guiding
rails 52 are provided to this effect.
A further slide 53 is .optionally provided
above the slide 50 so as to dampen the fall of the
particle stream from the conveyor C. The slide 53
will absorb a portion of the downward force, and will
absorb the lateral velocity transmitted from the
conveyor C to the particle stream, such that the
particle stream reaches the dilution treatment
chamber 12 at predetermined velocity parameters.
It is contemplated to provide various
geometries to the pretreatment module 15. For
instance, the sl~.de 50 is herein illustrated as being
generally a flat, inclined surface. However, it is
contemplated to provide the slide 50 with a
downwardly-tapered frusto conical shape, whose
smallest cross-section would meet the inlet 21 of the
dilution treatment chamber 12~. Moreover, for Such an
embodiment, the slide 53 preferably has an upright
conical shape.
THE OPERATION OF THE APPARATUS IN SEPARATTON
Now that the various components of the
apparatus 10 have been described, a separation
operation of the apparatus 10 is set forth.
Referring concurrently to Figs. 1, 2 and 3,
a particle stream is fed by the conveyor C to the
apparatus 10. The particle stream has a lateral
velocity and will accelerate downwardly when leaving
the conveyor C due to gravitational forces.
The slide 53 will absorb a portion of the
downward force of the particle stream, and stop the
lateral velocity of the particle stream that had been'
transferred to the particle stream by the action of
the conveyor C. The mass of particle stream is
directed by the slide 53 toward the Tide 50 of the
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pretreatment module 15, at generally predetermined
velocity conditions.
Upon reaching the slide 50, the particle
stream will be guided by the guiding rails 52 so as
to be conveyed uniformly towards the dilution
treatment chamber 12 as a result of the downward
slope of the slide 50. The downward slope of the
slide 50 will cause the particle stream to
accelerate.
The deflector 51, having a launch surface,
will deflect the particle stream so as to initiate a
break-up of the mass of particle stream. A lateral
dilution will be the result of the deflection of the
particle stream by the deflector 51. Accordingly,
the particle stream will reach the dilution treatment
chamber 12 , having been subj acted to a mass break-up
and to a horizontal dilution.
The particle stream then falls in the
channel 20 of the dilution treatment chamber 12. The
gravity will cause a vertical dilution of the
particle stream.
A first one of the nozzles, namely nozzle
14A, will inject air within 'the channel 20 of the
dilution treatment chamber 12 so as to cause a
break-up of the mass of particle stream into particle
groups (i.e., breaking down the mass of particle
stream) and spread out, dilute and/or create space
between particle groups. This nozzle 14A is also
referred to as a distributor, as it will be
distributing the particle stream over a surface area
of the channel 20. As alternative distributors, the
apparatus 10 may be provided with vibrating
strainers, impellers or the like, as will be
illustrated hereinafter.
The particle stream, having been subjected
to a horizontal and a vertical dilution (i.e.,
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break-up or distribution), will be crossing a
horizontal flow of air as injected by the second
nozzle 14B, and the optional third nozzle 14C. .The
nozzles 14B and 14C inject air at a predetermined
pressure through the apertures 25, which are opposite
the lateral outlets 24, such that the air will carry
the finer-particle group out of the channel 20,
through the lateral outlets 24, and into the inner
transfer chamber of the transfer casing 13, in a high
particle to air concentration. The air injected by
the nozzles 14 is at the predetermined pressure, such
that the coarse particle group will not be entrained
out of the channel 20 by the air flow. The dilution
that has taken place previously is an important
factor in the separation of the fine particles from
the coarse particles. The magnitude of the pressure
of air injection will have a direct effect on the
particles being withdrawn from the particle stream in
the channel 20. It is pointed out that the vertical
distance from the inlet 21 to the nozzle 14B is an
essential factor in diluting the particle stream to
facilitate the subsequent separation of the particle
groups so as to increase fluid/particle contact.
Although three nozzles (namely 14A, 14B anal
14C) are described, the number of nozzles 14 is
variable according to the present invention. The
apparatus 10 is operative with a single nozzle 14
opposite an aperture 25, but a plurality of nozzles
14 may be serially added on the dilution treatment
chamber 12 to increase the efficiency of the
operation taking place within the dilution treatment
chamber 12.
Thereafter, the fine, particle group exits
through the outlet 31 at the bottom of the inner
transfer chamber 30 of the transfer casing 13 after
settling, whereas the coarse particle group continues
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its drop into the dilution treatment chamber 12
toward the outlet 22.
THE OPERATION OF THE APPARATUS IN MIXING/TREATING
As mentioned previously, the apparatus 10
of the present invention can also be used for mixing
and/or treating particle and/or fluid streams.
Therefore, a mixing/treating operation of the
apparatus 10 is set forth.
Referring to Fig. 1, particle and/or fluid
streams to mix/treat are fed by the conveyor C, and
possibly other conveyors or particle and/or fluid
sources (not shown) to the apparatus 10. The
particle and/or fluid streams have a lateral velocity
and will accelerate downwardly when leaving their
source due to gravitational forces.
The slide 53,wi11 absorb a portion of the
downward force of the particle and/or fluid streams,
and stop the lateral velocity of the particle and/or
fluid streams that had been transferred thereto by
the action of the conveyor C or other possible
source. The particle and/or fluid streams are
directed by the slide 53 toward the slide 50 of the
pretreatment module 15, at generally predetermined
velocity conditions. _
Upon reaching the slide 50, the particle
and/or fluid streams will be guided by the optional
guiding rails 52 (Fig. 2) so as to be' conveyed
uniformly towards the dilution treatment chamber 12
as a result of the downward slope of the slide 50.
The downward slope of the slide 50 will cause the
particle and/or fluid streams to accelerate.
The deflector 51, having a launch, surface,
will deflect the particle and/or fluid streams
horizontally. A lateral dilution will be the result
of the deflection of the particle and/or fluid
streams by the deflector 51. Accordingly, the
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particle and/or fluid streams will reach the dilution
treatment chamber 12, having been subjected to a
horizontal dilution.
The particle and/or fluid streams then
falls in the channel 20 of the dilution treatment
chamber 12. The gravity will cause a vertical
dilution of the particle and/or fluid streams.
A first one of the nozzles, namely nozzle
14A, will laterally inject fluid, or any other
suitable fluid or particle jet, within the channel 20
of the dilution treatment chamber 12 so as to cause a
turbulence, a mix, or a treatment of the particle
and/or fluid streams. The fluid/particle injected by
the nozzle 14A is of predetermined pressure so as to
have a variable effect relative to the size, mass and
other characteristics of the particles and/or fluid
streams. The nozzle 14A injects ai'r, or any other
suitable fluid, at high pressure and low volume.
The lateral outlets 24 are not used in the
mixing process of the apparatus 10. The nozzles 14B
and 14C are optionally used with the lateral outlets
24 being blocked, so as to create further turbulence,
as it is contemplated to provide a plurality of the
nozzles 14 to enhance the mixing of particle and/or
fluid streams in the channel 20, or for treating the
particle and/or fluid streams. Additional nozzles
may also be added to the apparatus 10.
Thereafter, the mix or treated matter,
resulting from the mix/treatment of the particle
3o and/or fluid streams, continues its drop into, the
dilution treatment chamber 12 toward the outlet 22.
ADDITIONAL COMPONENTS OF THE APPARATUS 10
It is contemplated to provide additional
components to the apparatus 10 in order to optimize
the separation of the particle stream into .particle
groups.
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Referring to Figs. 5 and 6, a lateral
distributor is generally shown at 60. The lateral
distributor 60 is positioned in the , transfer chamber
30 of the transfer casing 13. Referring more
specifically to Fig. 6 in which all reference
numerals are shown to simplify Fig. 5, the lateral
distributor 60 is shown defining three upstanding
sectors 61, each converging to a segmented outlet
portion 62. Each of the sector 61 has a respective
collecting surface 63 upon which particles coming
from the dilution treatment chamber 12 will be
collected. An air flow outlet 64 is provided
downstream of the upstanding sectors 61 to allow an
appropriate flow of air, that will not impede on the
lateral flow of air (or gaseous fluid) out of the
lateral outlets 24 of the dilution treatment
chamber 12.
More specifically, the lateral distributor
60 operates with the principle that the distance
traveled by the particles carried in the flow of air
from the dilution treatment chamber 12 is a function
of the particle size parameters (e. g., surface area',
mass). Accordingly, coarser particles will travel a
shorter distance than finer ones, whereby the coarser
particles will be collected by the upstream sector
61. Therefore, a further particle group separation
takes place with the lateral distributor 60. The
hence separated particle groups are collected
separately at the segmented outlet portion 62.
Referring to Figs. 3 and 7, recuperation
trays 70 are provided below each of the lateral
outlets 24 of the dilution treatment chamber 12.
More specifically, it is possible that particles that
should selectively remain with the dilution treatment
chamber 12 are deflected out of the lateral outlets
24. It is anticipated that these coarser particles
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will not travel a long distance out of the lateral
outlets 24 due to their size parameters,
Accordingly, the recuperation trays '70 are provided
to collect these particles, as they are positioned
directly below the apertures 24. These particles are
returned to the dilution treatment chamber 12 by the
sloping shape of the recuperation trays.
Moreover, the recuperation tray 70
illustrated in Fig. 7 also effects a particle
to separation. More specifically, the recuperation tray
70 as a first sector 71 and a second sector 72. The
first sector 71 collects the particles that should
not have left the dilution treatment chamber 12,
whereas the second sector 72 collects rapidly falling
particles, of a grade just below that of the particle
group remaining within the dilution treatment chamber
12. It is pointed out that the second sector 72 is
connected to its own outlet.
Also, the recuperation tray 70 may be
pivotally connected at a bottom edge thereof to the
wall of the dilution. treatment Chamber 12. This
would enable adjustment of an angle of the
recuperation tray 70 with regard to the vertical, as
a function of the particle stream/particle group
being separated.
Figs. 12 and 13 illustrate alternatives to
the nozzle 14A for use in the dilution process. In
Fig. 8, an impeller is shown at 80. In Fig. 9, a
laterally reciprocating strainer is generally shown
at 90. Both these alternatives will cause a
horizontal dilution of the particle stream. Qther
alternatives include fans, electrostatic or magnetic
emitters (e.g., in, accordance with the type of
particle stream being treated), as well as any
mechanical or ultrasound system.
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It is also contemplated to inject additives
to the particle stream being diluted in the dilution
treatment chamber 12. For instance, an aperture such
as one of the pressure-differential apertures 25 can
be used with a suitable injection system (e. g.,
blower and conduit combination) to inject color
(e. g., in the form of a powder) to the particle
stream being diluted in the dilution treatment
chamber 12, or to particle groups being mixed
therein.
It is also contemplated to provide a
plurality of the apparatus 10 in series, with a
conveying system transporting/conveying the output of
an upstream one of the apparatus 10 to a downstream
one. Alternatively, a pair (or more) of the
apparatus 10 may be positioned in parallel and share
a common transfer chamber 30, to collect a specific
particle group. In such a case, the transfer chamber
30 could be used to mix a particle group from a first
dilution treatment chamber 12 with a particle group
of a second dilution treatment chamber 12.
For instance, referring to Fig. 10, an
apparatus ~in accordance with an alternative
embodiment of the present invention is generally
shown at 10'. The apparatus 10' is similar to the
apparatus 10 of Fig. 1 in that the apparatus 10' has
a dilution treatment chamber 12, nozzles 14 (herein
four nozzles for the dilution treatment chamber 12)
and an pretreatment module 15'. The pretreatment
module 15' shows a different shape (e.g., with a
conical slide 53'), but operates in a fashion similar
to that of the pretreatment module 15. The apparatus
10' has a transfer casing 13' in which a secondary
separation is performed.
More specifically, the transfer casing 13'
has a transfer plate 100, a dilution treatment
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chamber 102, nozzles 104 and a subcasing 106. The
particle group reaching the transfer casing 13' from
the dilution treatment chamber 12 will drop into the
inlet of the dilution treatment chamber 102, or will
settle onto the transfer plate 100, to then reach the
inlet of the dilution treatment chamber 102.
Optionally, the transfer plate 100 is
provided with a vibrator 108 so as to avoid having
particles collect thereon. The transfer plate 100
could also be provided with a low adherence coating,
such as PTFE.
The dilution treatment chamber 102 is
illustrated having the nozzles 104A, 104B and 104C.
The nozzle 104A serves the same function as the
nozzle 14A of Fig. 1, namely to break down the
particle group that has reached the dilution
treatment chamber 102. The nozzle 104A can be
replaced with other devices, such as those
illustrated in Figs. 12 and 13.
The nozzles 104B and 104C serve the same
function as the nozzles 14B and 14C of Fig. 1, and
are thus positioned opposite lateral outlets 110,
through which a particle group will be forced, to
reach the subcasing 106 and settle therein. The
removed particle group will exit through outlet 112,
whereas the particle group remaining in the dilution
treatment chamber 102 will exit through outlet 114.
Recuperation trays 116 are adjustable similarly to
the recuperation trays 70 of the preferred
embodiment.
Accordingly, the output of the apparatus
10' is three particle groups, with the particle group
exiting from the subcasing 106 being the finest. It
is pointed out that the gaseous fluid output of the
nozzles 14 and 104 is adjusted in view of the desired
size of the particle groups. The transfer casing 13'
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can be used for mixing, as described previously for
the apparatus 10.
TTQ'G'C
Amongst the various process that can take
place with the apparatus 10 of the present invention,
it is contemplated to separate, treat, classify (with
an initial step of separation), mix, add, vaporize,
clean, calibrate, or eliminate fines from particle
streams. Other treatments, such as painting,
coating, .sandblasting or cleaning, can be effected
with the apparatus 10 of the present invention.
Existing batch processes, such as the injection of
gas or chemicals into soft drinks, can be converted
to continuous processes using the present invention.
The. differential pressure in the dilution
treatment chamber 12 can be controlled electronically
and the apparatus 10 may be combined to magnetic,
electrical, ultrasound, electronic and
electromagnetic systems.
The apparatus 10 can be used with mineral,
vegetable, biological, organic aggregates, as well as
with fertilizers, treatment or transformation
residues, waste, food products, drugs and other
pharmaceutical products, powders, agriculture related
products, chemical or metallurgical products,
compost, plastics and composites, paper, soil and
bio-soil, ashes, crushed stone, ceramics, coal.
The apparatus 10 of the present invention
is relatively small. Accordingly, it is possible to
place the apparatus 10 at various parts of a ~ process
due to these advantageous features. The apparatus 10
enables large quantities of particles/fluid streams
to be treated in a relatively limited amount of
space, with little wear of material, low energy
consumption anal, in some embodiments, no moving parts
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(i.e., depending on the choice of the type of
dilution) .
The apparatus 10 can be used as part of a
multi-step or multi-pass process. Moreover, although
the preferred embodiment includes only a settling
cavity for the collection of particles, an outflow of
air for the partic=les remaining in suspension can be
added as an option. The apparatus 10 is made of
rigid materials, such as metals, polymers, etc... It
is pointed out that aside~from the slide 53, the
apparatus 10 goes through limited wear.
It is within the ambit of the present
invention to cover any obvious modifications of the
embodiments described herein, provided such
modifications fall within the scope of the appended
claims.
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