U.S. patent number 3,559,895 [Application Number 04/706,880] was granted by the patent office on 1971-02-02 for apparatus for and method of comminuting solid materials.
Invention is credited to Edwin F. Fay.
United States Patent |
3,559,895 |
Fay |
February 2, 1971 |
APPARATUS FOR AND METHOD OF COMMINUTING SOLID MATERIALS
Abstract
A fluid energy mill for pulverizing to finely comminuted state
dry solid material the particles of which are injected into a
grinding chamber for entrainment in a high velocity vortex of a
gaseous grinding fluid established in said chamber. The particles
to be pulverized and the primary grinding fluid are conjointly
introduced into the grinding chamber in the form of feed jets of
the material and grinding jets of the fluid relatively so arranged
as to locate each feed jet in such close downstream proximity and
so oriented with respect to an associated grinding stream that each
pair of the associated jets serves as an individual grinding unit
to insure the desired reduction in size of the particles serviced
by said unit before they are permitted to be discharged from the
mill. The discharge outlet of the mill, which may be provided with
one or more of the above-mentioned grinding units or of any
conventional form, is internally fitted with a spider having
exposed directional vanes for minimizing pressure drop at the
intake end of the outlet and correspondingly increasing the
vortical velocity of and the available energy in the gaseous energy
fluid stream present in the grinding chamber of the mill.
Inventors: |
Fay; Edwin F. (Marlton,
NJ) |
Family
ID: |
24839453 |
Appl.
No.: |
04/706,880 |
Filed: |
February 20, 1968 |
Current U.S.
Class: |
241/5 |
Current CPC
Class: |
B02C
19/061 (20130101) |
Current International
Class: |
B02C
19/06 (20060101); B02c 019/06 () |
Field of
Search: |
;241/5,39 |
References Cited
[Referenced By]
U.S. Patent Documents
Primary Examiner: Kelly; Donald G.
Claims
I claim:
1. Apparatus for the pulverization of material into finely divided
form comprising a generally circular grinding chamber for the
particles of material to be pulverized, means for injecting a
pressurized gaseous grinding fluid into said chamber through
plurality of circumferentially spaced jet orifices in communication
between a source of supply of said pressurized fluid and the
interior of said chamber to establish therein a high velocity
inwardly spiralling vortex of the gaseous fluid, and means for
injecting the material to be pulverized into said grinding chamber
through a plurality of circumferentially spaced jet orifices in
communication between a source of supply of said material and the
interior of said chamber for entrainment of said particles of
material in said vortex and movement therewith at a vortical speed
of travel which is high as compared with the speed of movement of
said particles radially inward toward a discharge outlet at the
center of said vortex, said fluid jet orifices being equal in
number to that of said material jet orifices with each said
material jet orifice located downstream of a single one of said
fluid jet orifices in such close proximity thereto and with its
axis so oriented relatively to that of its proximate fluid jet
orifice that the axis of each jet of the material at its point of
entry into the grinding chamber extends in nonintersecting relation
to the axis of its proximate gaseous fluid jet at the point of
entry of the latter into the grinding chamber.
2. In the apparatus as defined in claim 1 wherein each jet of the
gaseous fluid entering the grinding chamber is disposed inwardly of
and extends at an acute angle to its closely related jet of
material entering the grinding chamber whereby to initially confine
said material jet between said gaseous fluid jet and the
surrounding wall of the grinding chamber.
3. In the apparatus as defined in claim 1 wherein each jet orifice
for entry of the material into the grinding chamber is disposed
immediately adjacent the confining sidewall of the grinding chamber
with its axis so oriented with respect to the axis of its proximate
fluid jet as to direct the feed jet of said material tangentially
with respect to a circle in closely spaced concentric relation to
said sidewall of the grinding chamber and outside of a circle
substantially tangent to the axes of said fluid jets whereby to
introduce said material into the outermost circular region of the
vortex.
4. In the apparatus as defined in claim 1 which includes a pair of
opposed plate members and an annular member secured in intervening
position between the peripheral portions of said plate members to
form said grinding chamber, at least one of said plate members
being provided with a replaceable liner having an annular recess
extending about its circumferential margin spaced inwardly of said
annular member, the open end of said annular recess being sealed
off by its associated plate member to provide an annular manifold
into which the material to be pulverized is injected, the wall of
said manifold opposite its said associated plate member being
provided with said plurality of jet orifices through which said
material issues in jet form for entrainment in the vortex of the
gaseous energy fluid operating within said grinding chamber.
5. In apparatus as defined in claim 4 wherein each of said material
injecting orifices in the aforesaid wall of said manifold is
similarly oriented with its axis extending at an angle to the plane
of wall and along a line coincident with a circle closely adjacent
and concentric with respect to the outer circumferential wall of
said manifold whereby said material is injected into the grinding
chamber in a direction corresponding to the direction of rotation
of the vortex in said chamber and within an area external of a
circle tangent to the axes of said jets of the grinding fluid.
6. Apparatus for finely comminuting solid material in pulverulent
state comprising in combination a circular chamber in closed
communication with a source of pressurized gaseous fluid through a
jet forming nozzle for establishing in said chamber an inwardly
spiralling vortex of said fluid of high vortical velocity adapted
to discharge from said chamber through a discharge outlet extending
outwardly from the center region of the vortex, means for injecting
the pulverulent material into the outer marginal portion of the
vortex for movement inwardly thereof to and through said discharge
outlet, and means in said outlet for reducing turbulence of the
gaseous fluid and attendant pressure drop thereof in the region of
its entry into said outlet to thereby maintain a high rotational
speed of travel of the gaseous vortex in said chamber and
utilization of the maximum amount of grinding energy available as
the difference between the energy of the fluid supplied to the
grinding chamber and that of the fluid contained within the chamber
itself, said last-mentioned means comprising a spiderlike member
fitted in said discharge outlet and having a plurality of angularly
related vanes which provide a plurality of circumferentially spaced
separated passages extending rectilinearly through said outlet in
parallel relation to its central axis, said vanes extending freely
beyond the intake end of said discharge outlet in intercepting
relation to the gaseous fluid discharging from the center of the
stream and moving radially inward across the peripheral edge of the
intake end of said discharge outlet.
7. Apparatus according to claim 6 wherein the freely projecting
ends of said vanes extend beyond the intake end of said discharge
outlet a distance equal to from one-half to the full diametrical
dimension of the outlet.
8. Apparatus according to claim 6 wherein the freely projecting
ends of said vanes are respectively longitudinally and laterally
curved to provide the same with corresponding concave surfaces for
intercepting the gaseous fluid exiting from the central region of
the vortex and effecting streamlined flow thereof into the
discharge outlet.
9. The method of pulverizing solid pulverulent material into finely
divided form which consists in injecting the material to be
pulverized in the form of a feed jet into the outer region of an
inwardly spiralling vortex of a gaseous energy fluid having a
rotational speed substantially higher than that at which the fluid
moves inwardly toward the center of the vortex the said vortex of
the fluid being established and maintained at said high rotational
speed within an enclosed grinding chamber into which the energy
fluid is injected in the form of a grinding jet for effecting high
velocity vortical flow of the fluid toward a discharge outlet at
the center of the vortex, said feed jet of the material to be
pulverized being introduced into the vortex at a selected number of
circumferentially uniformly spaced points each in close proximity
to and downstream of the point of entry of one of an equal number
of similarly spaced grinding jets into the grinding chamber, the
axes of each grinding jet and its associated proximately located
feed jet being relatively so oriented that said feed jets are each
embraced on one side thereof by said grinding jet and on its
opposite side by the encircling wall of the grinding chamber.
10. Apparatus for the pulverization of material into finely divided
form comprising a generally circular grinding chamber for the
particles of material to be pulverized, means for injecting a
pressurized gaseous grinding fluid into said chamber through a jet
orifice in communication between a source of supply of said
pressurized fluid and the interior of said chamber to establish
therein a high velocity inwardly spiralling vortex of the gaseous
fluid, means for injecting the material to be pulverized into said
grinding chamber through a jet orifice in communication between a
source of supply of said material and the interior of said chamber
for entrainment of said particles of material in said vortex and
movement therewith at a vortical speed of travel which is high as
compared with the speed of movement of said particles radially
inward toward a discharge outlet at the center of said vortex, said
material jet orifice being located downstream of the fluid jet
orifice in close proximity thereto and with its axis so oriented
relatively to that of the fluid jet orifice that the axis of the
jet of the material at its point of entry into the grinding chamber
extends in nonintersecting relation to the axis of the gaseous
fluid jet at the point of entry of the latter into the grinding
chamber, and means in said discharge outlet for reducing the
pressure of the gaseous energy fluid in the grinding chamber to
thereby achieve a substantial increase in the vortical velocity and
the grinding energy of said fluid, said pressure reducing means
comprising a spiderlike member having a plurality of angularly
related vanes to form a plurality of circumferentially spaced
passages extending rectilinearly through said outlet parallel to
its central axis, said vanes having end portions extending freely
beyond the intake end of the discharge outlet to intercept and
effect streamlined entry into the discharge outlet of the spent
gaseous fluid exiting from the center of the vortex.
Description
This invention relates generally to fluid energy mills for the
pulverization of dry solid material wherein the particles of said
material are reduced to a predeterminedly desired finely comminuted
size through attrition caused by bombardment of the particles
against one another and against the wall of a grinding chamber in
which is established a high velocity vortex of a primary gaseous
fluid in which the particles to be pulverized are entrained, the
rotational speed of the vortex being high as compared with its
component of inward movement toward a discharge outlet located in
the central region of the vortex.
Among the principal objects of the present invention is to provide
improvements in the apparatus for and method of utilizing to best
advantage and with the highest possible efficiency the maximum
amount of grinding energy which is available in the fluid
introduced into the grinding chamber.
More specifically it is an object of the present invention to so
introduce the material to be pulverized into the high velocity
vortical stream of the prime gaseous energy fluid so as to prevent
premature dispersion of the material particles in said stream such
as would result in the discharge of particles from the grinding
chamber by the radially inward component of movement of the fluid
before they had been reduced to the desired comminuted size.
A further object is to provide an apparatus for and method of
entering the material to be pulverized conjointly with the primary
gaseous energy fluid for effecting the reduction to desired size of
the particles so as to confine and maintain the heavier and coarser
particles of the material to a path of travel in the outer region
of the gaseous vortex until such time that they are sufficiently
reduced in size as to be free to move radially inwardly of the
vortex against the restraining influence of centrifugal action of
the vortex for eventual discharge from the mill.
Still another object of the invention is to provide a means for and
method of decreasing the pressure drop of the energy fluid at the
point of its entry into the discharge outlet of the mill and
thereby increase the vortical velocity of the fluid with
corresponding increase of the fluid energy available for most
efficient grinding of the material to its predeterminedly reduced
size.
Other objects and advantages of the invention will be apparent from
the detailed specification which follows, it being understood that
the invention consists in the combination, construction, location
and relative arrangement of parts, as well as in the improved
method for effecting pulverization of the material, all as
described more fully hereinafter, as shown in the accompanying
drawings, and as finally pointed out in the appended claims.
In the accompanying drawings:
FIG. 1 is a side elevational view, partly in vertical section, of
one form of the pulverizer apparatus constructed in accordance with
and embodying the principles of the present invention;
FIG. 2 is a vertical sectional view of the apparatus as taken along
the line 2-2 of FIG. 1;
FIG. 3 is a horizontal sectional view as taken along the line 3-3
of FIG. 2;
FIG. 4 is a transverse sectional view as taken along the line 4-4
of FIG. 2;
FIG. 5 is a fragmentary view in vertical section of a portion of
the apparatus as viewed along the lines 5-5 of FIGS. 2 and 3;
FIG. 6 is a view of a modified form of the spider element which is
fitted in the discharge outlet of the pulverizer;
FIG. 7 is a transverse sectional view of this modified form of
spider element as taken along the line 7-7 of FIG. 6;
FIG. 8 is a vertical sectional view of a modified form of the
pulverizer apparatus for discharge of both the pulverized material
and spent air through a common discharge outlet in the top of the
apparatus;
FIG. 9 is a vertical sectional view of a pulverizer apparatus
generally similar to that of the modified form shown in FIG. 8 but
including provision for independent discharge of the pulverized
material and of the spent air respectively through top and bottom
discharge outlets provided in the apparatus;
FIG. 10 is a vertical sectional view of another form of pulverizer
having a common topmost discharge outlet for the pulverized
material and spent air;
FIG. 11 is a vertical sectional view of still another type of
pulverizer apparatus in which is incorporated the discharge outlet
spider element of the present invention;
FIG. 12 is a sectional view of the pulverizer as taken along the
line 12-12 of FIG. 11;
FIG. 13 is a top plan view partly in section, of a still different
type of pulverizer apparatus having incorporated therein the
discharge outlet spider of the present invention; and
FIG. 14 is a horizontal sectional view as taken along the line
14-14 of FIG. 13.
Pulverizers of the general type to which the present invention
relates are conventionally known as fluid energy mills and are
ordinarily classified as being either of the horizontal type or of
the vertical type. In either case the fluid energy mill essentially
includes a chamber wherein the substrate particles of the raw
material to be ground to size are whirled at high velocity through
a spiralling vortex path terminating in a discharge outlet in the
center region of the vortex. In order to effectuate and maintain
the high-speed vortical flow of the particles in the vortex chamber
a gaseous fluid is introduced into the outer portion of the
spiralling vortex at one or more points spaced about its outer
circumference under such nozzle pressure to provide the introduced
fluid with a high velocity sufficient as to impart a high speed of
vortical travel to the particles which, when injected into the
vortex chamber, are subjected to the influence of the energizing
fluid.
The particles of the material to be pulverized to a predeterminedly
desired particle size or classification, when whirled about the
spiralling vortex path at high speed, are reduced or ground to the
desired smaller particle size through attrition caused by the
colliding and rubbing together of the substrate particles and by
their abrading contact with the internal wall surfaces of the
vortex chamber. Despite the fact that the vortical or rotational
speed of travel of the particles is very high as compared with the
speed of movement of the particles inwardly of the vortex toward
the discharge outlet located proximate the center of the vortex so
that the heavier and coarser particles tend to travel about the
outer portion of the vortex due to the centrifugal force acting
thereon, it has been found that a substantial proportion of these
coarser substrate particles are carried to the discharge outlet of
the vortex for discharge therefrom together with the more finely
reduced particles. Generally, this undesired result occurs in all
those fluid energy mills wherein the entire mass of raw material to
be treated is injected at one point, thereby causing considerable
reduction in velocity of the fluid energy stream at the point of
injection thereinto of the material, or where the injection is made
in such manner as to allow the escape of unground material before
it becomes a part of the mass moving vortically in the vortex
chamber.
While this reduction in velocity of the vortex stream due to
injection into that stream of the entire mass of raw material at a
single point is not of critical importance in vertical mills where
classification occurs by the ability of the high velocity airstream
to entrain and lift the particles of finely reduced size out of the
vortex stream, leaving the coarser particles to be separated out by
gravity or centrifugal force operating in the classifying zone, it
is of great importance that there be no such reduction in velocity
at the point of entry of the raw material into the fluid energy
stream in horizontal mills wherein classification is accomplished
solely by velocity of the gaseous stream in which the particles are
entrained and the centrifugal force exerted by the stream upon the
particles as they move toward the discharge outlet of the vortex.
In these horizontal-type fluid energy mills, while the more finely
sized particles are discharged from the grinding chamber together
with the spent airstream in which they have been entrained, some of
the coarser particles eventually also find their way out of the
grinding chamber with the spent airstream, thereby degrading the
quality of the classification desired for the finer particles.
Obviously, when the velocity of the stream is reduced at the point
of injection of the raw material, the fluid energy stream acting in
the presence of a reduced centrifugal force is still sufficiently
strong to penetrate and disperse the stream of the injected raw
material with the result that a substantial increment of the
heavier and coarser particles are drawn to and through the
discharge outlet before they have had an opportunity of being
effectively reduced in size through collision and rubbing contact
with other particles of the injected mass of material.
In accordance with the principles of the present invention very
considerably improved classification is achieved by providing a
construction of fluid energy mill wherein the material to be finely
pulverized is injected into the grinding chamber of the mill at a
point so related and in a direction so oriented with respect to the
high velocity stream of gaseous fluid which forms the inwardly
spiralling vortex as to impart a high rotational or vortical speed
of travel to the material undergoing pulverization without at the
same time creating any tendency for the fluid stream to cut through
and so disperse or otherwise change the integrity of the jet or
jets of raw material directed into the grinding chamber for
entrainment in the high velocity vortical stream of the energy
fluid.
The principle of the present invention is applicable to mills
provided with any number of uniformly spaced nozzles for
introduction of the raw material into the grinding chamber so long
as each such nozzle has associated therewith its own individual
grinding stream of the gaseous fluid. This gaseous fluid may be
air, steam or other suitable gas which is introduced into the
grinding chamber at any desired temperature and pressure, usually
from 100 to 150 p.s.i. The gaseous fluid is introduced into the
grinding chamber through the aforesaid nozzles or jet orifices to
provide "grinding jets" as distinguished from the "feed jets" of
the material introduced into the grinding chamber for pulverization
of the particles to a predetermined classified size. As will appear
more fully hereinafter, these feed jets of the particles to be
pulverized are supplied with the raw (unpulverized) material from a
feeding head or manifold into which the material is fed under
relatively slight pressure (usually from 5 to 8 p.s.i.) by an
injector-type feeder mechanism which includes a venturi-fitted
conduit through which a pressurized gaseous fluid flows as the
vehicle for injecting the material to be pulverized into the
grinding chamber.
Preferably, a plurality of the feed jet orifices are provided in
uniformly spaced relation about the circumference of the grinding
chamber, all of which are commonly fed with raw material by a
single injector-type feeder mechanism by way of a manifold which
embraces the grinding chamber and is in communication therewith
through the aforesaid plurality of circumferentially spaced feed
jet orifices. Each such feed jet is so oriented in relation to the
grinding chamber as to project the raw material feed jets along a
circular path which closely adjoins and is concentric with respect
to the circular outer wall of the grinding chamber, in consequence
of which the feed jets of the raw material particles are each
projected more or less tangentially with respect to a circle
described within the outer region of the gaseous fluid vortex. In
accordance with the principles of the present invention, the
gaseous fluid which forms the grinding jets is introduced into the
grinding chamber through uniformly spaced orifices equal in number
to that of the feed jets and in such positional relationship to the
feed jets as to provide each feed jet upstream thereof with its own
grinding jet. Further, the grinding jets are each so oriented with
respect to the direction of discharge of the feed jets respectively
associated therewith as to substantially reduce any tendency of the
grinding jets to effect premature dispersion of the feed jets, the
relative arrangement of the paired feed and grinding jets being
such that each of the feed jets is located downstream from and thus
so leads its associated grinding jet as not to be impinged and
thereby prematurely disrupted by the grinding jet.
This relative arrangement of the feed and grinding jets not only
maintains a high velocity vortical travel of the raw material in
the grinding chamber, but even more importantly maintain the
heavier and coarser particles in the outer regions of the vortex
until such time as they are sufficiently reduced in size to be
carried out through the vortex discharge outlet with the spent
gaseous energy fluid. Thus, a classification is accomplished solely
by the velocity of the energy fluid (grinding jets) and the
centrifugal force which maintains the coarser particles in the
outer region of the vortex until they have been so reduced in size
by attrition as to enable them to be carried out by the flow of the
gaseous fluid inwardly of the vortex and out of the discharge
outlet with the spent gas.
It will be seen from the foregoing that in accordance with the
present invention the raw material to be ground is introduced or
injected into the grinding chamber at regions in each of which is
also included a coacting grinding jet. Since each feed jet is
directed substantially tangential to a circle just within and
concentric to the outer wall of the grinding chamber, that is
tangential to a circle within the outer region of the vortical path
of travel of the particles in the grinding chamber, each jet is in
effect embraced at one side thereof by the circular wall of the
chamber and at its opposite side by the grinding jet individual to
and coacting with the feed jet. Thus, each pair of related feed and
grinding jets constitutes in effect an individual grinding unit and
when the grinding chamber is provided with a plurality of such
units in uniform circumferentially spaced relation, they all
operate in unison to form a symmetrical vortex in the grinding
chamber, resulting in uniform distribution of the material to be
ground within the grinding chamber and greatly increased efficiency
in operation of the mill due to the fact that the full work load of
mill is equally distributed between the several grinding units.
Another important aspect of the present invention is in the
provision of means in the discharge outlet of the mill for reducing
the pressure of the gaseous fluid in the grinding chamber to
thereby achieve a substantial increase in the vortical velocity of
the fluid which forms the grinding jets. The available grinding
energy is the difference between that of the pressurized fluid
supplied to the grinding chamber and that of the fluid within the
grinding chamber which latter fluid energy is determined by the
pressure and temperature conditions prevailing in the chamber. It
has been found that for each reduction of 1 pound per square inch
of pressure within the grinding chamber, an increase of from 21/2to
5 percent in velocity can be realized.
Since the vortical velocity in an important factor for efficient
grinding in fluid energy mills, the means of the present invention
for reducing the internal pressure of the gaseous fluid in the
grinding chamber with consequent increase in its vortical velocity
is of great value not only in horizontal mills but also in vertical
mills and in fact in any type of fluid energy mill for the
pulverization of dry particulate material to a predetermined
uniformly fine particle size.
To this end the present invention contemplates, in addition to the
provision of the individualized grinding units above described, the
provision in the discharge outlet of the fluid energy mills of a
set of stream straightening vanes which are so arranged and
disposed in the discharge outlet tube as to effect a substantially
rectilinear passage of the spent gas through the discharge
outlet.
The tendency of the gas discharged from the center of vortex in the
grinding chamber is to continue to spiral as it moves outwardly
through the discharge outlet, in addition to which it is also
subject to turbulence tending to restrict its rapid discharge
through said outlet. This turbulence is due primarily to portions
of the gaseous energy stream impinging against one another as they
pass from the grinding chamber radially inward across the outer
circle of the intake end of the discharge outlet toward the center
thereof. It has been determined that due to the spiralling action
alone of the gas passing through the discharge outlet, the distance
of travel of the spiralling stream of gas through the discharge
outlet is more than six times that of the gas exiting in the form
of a straight line stream. As will be more particularly pointed out
in the detailed description which follows, the stream straightening
vanes of the present invention not only serve to decrease the
distance of travel of the spent gas through the vortex discharge
tube and thus reduce the frictional resistance to passage of the
gas outwardly of said tube with resulting increase in the vortical
velocity of the gaseous fluid in the grinding chamber, but also by
virtue of their disposition in the discharge tube, they
substantially reduce the turbulence which is normally induced by
the abrupt 90.degree. change in direction of the gaseous fluid
stream as it leaves the center of the vortex in the grinding
chamber and enters the discharge line.
It is known, for example, that the pressure drop of a fluid passing
through a 90.degree. elbow in a fluid pressure pipe line is
approximately equivalent to that of 5 to 6 feet of straight pipe in
the line and under certain circumstances may be as much as 5 to 10
times this approximate equivalent. By providing the outlet tube of
the grinding chamber with a set of directional vanes having exposed
end portions which freely project beyond the inlet end of the
discharge tube a distance equal to from one-half to the full
diameter of the outlet tube, the gaseous fluid exiting from the
grinding chamber is streamlined as it encounters the exposed
directional vanes and thus enters the discharge line with a minimal
pressure drop between the gaseous fluid pressure in the grinding
chamber and that at the point of its entry into the discharge tube,
thereby insuring utilization of the maximum amount of energy for
grinding which is available as the difference between the energy of
the fluid supplied to the grinding chamber and that of the fluid
contained inside the grinding chamber itself.
Referring now to the drawings and more particularly to FIGS. 1 to 5
thereof, which show one form of a horizontal-type fluid energy mill
constructed in accordance with and embodying the hereinbefore
described principles of the present invention, it will be observed
that the mill designated generally by the numeral 10 includes a
recessed circular top plate 11 and a recessed circular bottom plate
12 which are respectively provided with oppositely presenting
annular flanges 13 and 14 which circumferentially embrace and
marginally define the opposed recesses of the plates 11 and 12.
Respectively fitted in the recesses of these plates 11 and 12 are
preformed, replaceable liners 15 and 16 formed of any suitable
abrasion-resistant material, which may be any plastic material such
as Teflon, nylon, polyurethane and the like or a suitable rubber,
metal or ceramic material. The exposed faces of these liners 15 and
16 are respectively dished, as at 17 and 18, to provide
therebetween a cavity 19 which increases in vertical depth inwardly
from its outer peripheral margin. This cavity 19 is marginally
enclosed by an annular member 20 of general T-shape in transverse
section to provide it with an annular radially extending inner
portion 21 and an annular hollow outer portion 21a. The internal
radially extending portion 21 of the member 20 is snugly fitted
between the oppositely presenting outermost portions of the
liner-fitted plate members 11 and 12, while the annular outer
hollow portion 21a is disposed in closely embracing relation about
the annular flanges 13 and 14 of these plate members.
While the liner-fitted plates 11 and 12 and the intermediate
annular member 20 may be secured together in their assembled
relation as best shown in FIG. 1 by any suitable means, these parts
are preferably held assembled by a plurality of quick-detachable
C-type clamps 22, of which only one is shown in FIGS. 2 and 3, to
facilitate quick and easy disassembly of the mill for cleaning and
otherwise servicing the same as may be required. The cavity 19 thus
formed by the top and bottom plate members 11 and 12 in assembly
with the intermediate annular member 20 constitutes the grinding
chamber of the mill.
The top plate 11 is provided with a suitably shouldered central
aperture 23 in axial registry with a central aperture 24 formed in
the liner 15. Similarly, the bottom plate 12 is provided with a
shouldered central aperture 25 in axial registry with a central
aperture 26 formed in its liner 16. A discharge tube 27 projects
axially inwardly through the top plate assembly of the mill to a
point just beyond the bottom central opening of the mill cavity 19,
while extending axially downward of the cavity 19 in axial
alignment with the discharge tube 27 is a collector member 28. It
will be noted that the internal diameter of the collector in the
region thereof which embraces the lower end of the discharge tube
27 is of greater diameter than the external diameter of the
terminal portion of said tube to thereby provide an annular space
or orifice 29 through which the particles of the material ground to
size in the grinding chamber of the mill may pass by gravity flow
into the collector 28 and the spent gas from the grinding chamber
may pass for discharge through the discharge tube 27.
The discharge tube 27 is preferably secured to the top plate and
liner assembly as a fixed part thereof by providing it with an
enlarged head 30 having a flange adapted to be seated in the
shouldered aperture 23 of the top plate 11 and held therein by an
anchoring ring or nut 31 threaded onto the head 30 for clamping
engagement against the bottom of the liner 15. An air exhaust
conduit 32 is suitably bolted or otherwise secured to the outer end
of the discharge tube as an extension thereof.
The collector 28 is bolted or otherwise suitably secured to the
bottom plate and liner assembly.
The liner 15 for the top plate member is provided with an upwardly
presenting annular channel or recess 33 which extends
circumferentially about the full circle of the liner closely
adjacent the peripheral edge thereof. With the liner 15 secured in
position within the recessed top plate 11, the latter serves as a
closure for the open top side of the channel 33 in the liner and so
provides in the top plate and liner assembly an annular plenum or
manifold 34 into which may be introduced the raw material to be
pulverized in the mill. As is best shown in FIGS. 1 and 2, the top
plate 11 is provided with a feeding head, designated generally as
35, which includes a conduit 36 having a venturi passageway 37 in
communication with the interior of the manifold 34. Connected to
the venturi conduit 36 is a pressurized gaseous fluid supply
conduit 38 having a nozzle 39 in spaced coaxial relation to the
venturi passage 37.
Operatively associated with the venturi conduit 36 is a material
supply hopper 40 having a discharge throat in communication with
the inlet to the venturi passage 37 whereby upon the flow of the
pressurized fluid through the nozzle 39 and into the venturi
passage the raw material from the hopper 40 is drawn into the fluid
stream for injection thereby into the manifold 34 of the mill. The
material feeder mechanism 35 is so oriented relatively to the
annular manifold 34 as to inject the coarse material to be
pulverized into said manifold in a direction which causes the
material to flow clockwise about the manifold when viewed in plan
as shown in FIG. 3 and thus be spread uniformly throughout said
manifold. The amount and pressure of the fluid flowing through the
venturi passage is desirably restricted to that necessary to carry
the material delivered from the hopper 40 into the manifold 34 and
thence into the grinding chamber 19 of the mill without any undue
pressure drop between the annular manifold 34 and the grinding
chamber.
The coarse material thus introduced into the manifold 34 is
discharged therefrom into the grinding chamber 19 by way of a
plurality of uniformly spaced openings 41 formed in the bottom wall
42 of the manifold. While in the construction shown in FIGS. 1 to
3, eight such openings are provided, it will be understood that any
desired number of such circumferentially equally spaced openings
may be provided in the bottom wall of the manifold in order to
insure uniform distribution of the coarse material about the
circumferential margin of the grinding chamber.
It is of importance to note that the openings 42 are all similarly
oriented with their bores each extending at the same angle to the
vertical and pointing in the same general direction (clockwise) as
does the injection nozzle of the raw material feeding head, as best
shown in FIG. 1. Also it will be noted that the openings 42 are
disposed with their axes intersecting at uniformly spaced points
the line of a circle which is concentric with respect to and in
such closely spaced relation to the outer sidewall 43 of the
manifold as to locate the discharge ends of said openings 42 in
very close proximity to the interior surface of the annular
sidewall of the grinding chamber, as is best shown in FIG. 2. These
openings 42 serve as passages from the material feed distributing
manifold 34 to the grinding chamber 19 through which the coarse
material to be pulverized is injected into the grinding chamber in
the form of spaced jets under uniform pressure, velocity and volume
dependent upon the pressure of the injecting fluid passing through
the injector-type feeder mechanism 35. The material thus injected
into the grinding chamber is initially constrained to flow
circumferentially about the outer region of the gaseous vortex
generated in the grinding chamber.
This inwardly spiralling vortex is set up and maintained at high
velocity by the gaseous energy fluid which is introduced under a
relatively high pressure (100 to 150 p.s.i.) to the interior of the
hollow outer ring portion 21a of the member 20 forming the circular
side enclosing wall of the grinding chamber. This high-pressure
fluid is applied to this hollow outer portion of the annular member
30 by a conduit 44 connected to a suitable supply of the
pressurized fluid and is injected into the interior of the grinding
chamber in the form of a plurality of high velocity jets by way of
uniformly spaced openings 45 extending through the radially
projecting inner portion 21 of the member 20. These jet openings
45, which produce the high velocity fluid grinding jets
hereinbefore mentioned, are equal in number to the number of the
material feed jets which discharge into the grinding chamber by way
of the openings 41 provided in the bottom of the material feeding
manifold or plenum 34. The several grinding jets each enter the
grinding chamber in such intersecting angular relation to the outer
boundary of the grinding chamber as to set up in the latter a high
velocity inwardly spiralling vortical flow of the pressurized fluid
coursing in the same general direction as do the material feed
jets, namely, in a clockwise direction when the mill is viewed as
in FIG. 3.
It will be noted, however, that each of the grinding jet openings
45 is located upstream of and in close proximity to a feed jet
opening 41 and that the angle of injection of each grinding jet
into the grinding chamber is such that its bore extends at an acute
angle to the direction of initial discharge of the material to be
pulverized from its closely related feed jet opening 41, this angle
being that designated a in FIG. 3. Since the feed jets are each
located downstream with respect to its associated grinding jet,
there is no impingement of these paired jets one against the other
in the immediate region of their entry into the grinding chamber
and thus the integrity of the feed jets is not prematurely
destroyed as would occur through immediate impinging engagement of
the grinding jets with the feed jets. Instead, the feed jets
containing the coarse material to be pulverized are directed along
paths substantially tangential to a circle closely adjacent the
circumferential outer wall of the grinding chamber and thus are
each embraced on its outer side by said wall and on its inner side
by a coacting grinding jet, in consequence of which each feed jet
at its point of injection into the grinding chamber is constrained
to move in a circle immediately adjoining the grinding chamber
wall. This effectively reduces to a minimum any tendency for the
heavier and coarser particles of the material to be pulverized from
being prematurely carried by the inwardly directed force component
of the vortex toward the discharge outlet of the mill and thus
these heavier and coarser particles of the material continue to be
reduced in size by collision against one another and against the
wall of the grinding chamber until they have been sufficiently
reduced in size to relieve them from the influence of centrifugal
force and permit their movement inwardly toward the center of the
vortex across the divergent end regions of the grinding jets.
As is most clearly shown in FIGS. 2 and 3, the discharge tube 27 is
interiorly fitted with a spider member 46 having a plurality of
angularly related vanes 47 extending lengthwise of the tube to
provide therein a plurality of circumferentially spaced channels or
passages 48 (see FIG. 3) through which the gaseous energy fluid may
pass for discharge from the grinding chamber. The vanes 47 of the
spider member 46 project freely beyond the inlet end of the
discharge tube a distance equal to from one-half to the full
diameter of the discharge tube and in the form of mill shown in
FIGS. 1 to 5, these freely extending exposed end portions of the
spider project downwardly into the inner, i.e., top, end of the
collector 28 with the longitudinally extending outer edges of the
spider vanes 47 spaced inwardly of the cylindrical wall of the
collector.
These exposed end portions of the spider vanes 47 are thus disposed
in the path of travel of the gas discharging from the grinding
chamber and entering the inlet end of the discharge tube and
effectively operate to prevent disrupting impingement between
circumferentially spaced segments of the gas stream which seek to
enter the discharge tube by travel radially across the circular end
of the discharge tube toward and thence upwardly through the center
of the tube. The exposed ends of the vanes 47 serve to divide and
separate the gaseous stream as it leaves the vortex into spaced
segments which are then smoothly deflected by the vanes to move
upwardly about the inlet end of the discharge tube with minimal
turbulence at the center of said inlet. Upon such streamlined entry
of the spent gas into the discharge tube, the upper sections of the
vanes enclosed within the tube insure continued streamlined flow of
the gas upwardly and out through the discharge end of the tube. As
has been pointed out hereinbefore, by so reducing turbulence of the
exhausting gas stream at the point of its entry into the discharge
outlet to thereby preclude excessive or undue pressure drop at this
point, the grinding energy of the pressure fluid within the
grinding chamber is rendered available to the maximum degree
possible.
The spider 46 may if desired be provided with vanes 47a which have
their exposed extremities 47b each similarly curved, as shown in
FIGS. 6 and 7, to provide concave surfaces to smoothly deflect and
direct the above described segmental portions of the gaseous stream
exiting from the vortex in the grinding chamber about the solid
center of the exposed portion of the spider and thence upwardly
through the passages 48 formed by the spider vanes in the discharge
tube 27 for straight line flow therethrough toward and through the
terminal outlet for the spent gas.
In operation of the mill as described and shown in FIGS. 1 to 7,
the high-pressure gaseous fluid introduced into the hollow annulus
21a is injected into the grinding chamber by way of its orifices 45
in the form of a plurality of high velocity jets or streams each in
the direction as indicated by the arrows in FIG. 3. As shown the
direction of discharge of these grinding jets is chordally across
the interior of the grinding chamber at an acute angle with respect
to the peripheral wall of the chamber. These grinding jets set up
and maintain in the grinding chamber an inwardly spiralling vortex
into the outer circular region of which is introduced the raw
material to be pulverized by way of the orifices 41 of the material
distributing manifold 34.
As the particles of the material are ground to size by attrition
thereof in the grinding chamber, those of finely reduced size are
carried by the inwardly directed force moment of the vortical
stream to the center thereof for discharge thereof by gravity into
the collector 28 by way of the annular discharge orifice 29 formed
between the concentric wall portions of the discharge tube 27 and
the collector 28. The heavier and coarser particles of the material
are restrained from undesired premature movement across the
vortical path of the energy fluid by the confining action of the
grinding jets each acting in conjunction with an associated feed
jet as above described and so are held bound in the vortex against
discharge therefrom until they have been so sufficiently reduced in
size that they may move inwardly to the discharging center of the
vortex against the restraining centrifugal action thereof.
As the gas-entrained particles of the desired reduced size enter
the zone of the material discharge orifice 29, the comminuted
particles separate out from the gas stream and flow by gravity into
the collector 28 at the same time that the spent gas escapes by way
of the discharge tube 27. Classification of the material is
achieved in the inner or central zone of the vortex, since only the
particles which have been reduced to the desired size are carried
out of the vortex for discharge into the collector, while the
particles of greater size remain bound in the vortex until they too
are reduced to the desired size. Since the spent gas is discharged
to atmosphere with minimal pressure drop at the point of its entry
into the discharge tube, the vortical velocity of the fluid energy
stream in the grinding chamber is maintained at a high level for
most efficient pulverization of the material injected into the
mill.
FIGS. 8, 9 and 10 show modified forms of fluid energy mills
embodying one or more of the features of the present invention. The
fluid energy mill of FIG. 8 is similar in all material respects to
that of FIGS. 1 to 5 except that the discharge tube 50 thereof with
its streamlining spider 51 is entirely disposed within the grinding
chamber 52 of the mill. As in the previously described mill shown
in FIGS. 1 to 5, the mill of FIG. 8 is provided with a material
distributing manifold 53 having circumferentially spaced orifices
54 through which the material to be pulverized is injected into the
grinding chamber in the form of spaced feed jets. The gaseous
energy fluid is introduced into the grinding chamber in the form of
high velocity grinding jets through the jet orifices 55
communicating with the hollow fluid distributing ring 56, each feed
jet having associated with it one of the grinding jets to provide a
series of spaced grinding units operating as hereinbefore
described. However, in the mill of FIG. 8, the pulverized material
together with the spent gas exhausting from the grinding vortex is
discharged upwardly through the discharge tube to a suitable
collector (not shown) connected in line with the discharge outlet.
Classification is achieved as in the previously described form of
mill in the vortex discharge zone immediately surrounding the
exposed streamlining portions of the spider 51.
FIG. 9 shows another form of horizontal mill wherein the vortex in
the grinding chamber 56 is established by pressurized gaseous fluid
injected thereinto through a plurality of jet orifices 58 uniformly
spaced about the periphery of the mill, these orifices being all in
communication with a common hollow annulus 59 to which the gas is
supplied under suitable pressure. The material to be pulverized is
introduced into the grinding chamber at only a single point by way
of an injector-type feeder mechanism 60 in accordance with
conventional mills. However, this mill is also provided in its
discharge tube 61 with a streamlining spider 62 having its end
exposed beyond the corresponding end of the discharge tube to
provide for maximum high velocity flow of the vortex stream of gas
in the grinding chamber to thereby render available maximum energy
for efficient grinding of the material in the grinding chamber. As
in the first described form of the mill, in the mill of FIG. 9 the
pulverized particles pass by gravity into a collector 63, while the
spent gas exhausting from the vortex escapes by way of the
discharge tube 59 which is fitted with a streamlining spider 60
constructed and operating in accordance with the principles of the
present invention.
FIG. 10 shows the application of the streamlining spider 64 of the
present invention to another more or less conventional design of
horizontal mill wherein the particles of material reduced to their
desired minute size is carried out of the mill together with the
spent gas exhausting from the vortex in the grinding chamber by way
of the discharge tube 65.
FIGS. 11 and 12 illustrate a vertical type of fluid energy mill in
the discharge outlet of which is incorporated the spider feature of
the present invention for streamlining the flow of the spent gas
out of the grinding chamber and thereby maintain in said chamber
the highest possible vortical velocity of the energy fluid supplied
thereto. In this vertical type of fluid energy mill the pulverized
material is introduced into a classifying chamber 70 in which the
gaseous fluid stream whirls at high velocity about a horizontally
extending central axis for discharge of the finely sized particles
through a discharge outlet disposed with its axis coincident with
that of the rotational axis of the vortex. The gaseous fluid energy
stream which serves as the primary grinding fluid is injected from
a suitable pressurized supply thereof into the vortex chamber 70
through a nozzle 71 in axially spaced registry with a passage 72
extending through a venturi tube 73, while the material to be
pulverized is injected into said chamber by a material conveying
stream of gas which issues through a nozzle 74 and passes through
the bore 75 of an axially spaced venturi tube 76 to pick up and
convey the feed material from a supply hopper 77 into the grinding
chamber. It will be noted that the material injecting jet and the
primary fluid injecting jet are directed toward one another from
opposite ends of a bottom chamber 78 which communicates with the
vortex chamber 70 by the communicating passages 79 and 80.
The material to be pulverized is initially shattered in the chamber
78 by impact of the primary grinding fluid with the entering stream
of the feed material, following which the grinding fluid and its
entrained material then passes upwardly through the passage 79 for
vortical travel at high velocity within the vortex chamber 70 and
subsequent discharge through the outlet tube 81 leading to a
collector not shown of any conventional construction. Because of
the centrifugal force acting on the particles within the vortex
chamber, the more heavy and coarser particles migrate to the outer
periphery of said chamber and are carried by the fluid energy
stream tangentially thereof through the passage 80 back into the
primary impact zone 78 for further reduction of these larger
particles of the material to the desired smaller size.
The particles of material which are reduced by attrition and impact
to the smaller size desired are carried by the spent gas leaving
the center of the vortex through the discharge outlet 81, which
latter is provided with a streamlining spider 82 having the
circumferentially spaced directional vanes 83 as incorporated in
the previously described fluid energy mills. Thus, in the
last-described vertical type of mill, as in the previously
described horizontal mills, the vanes 83 have their inner portions
extending freely beyond the corresponding inner end of the outlet
tube 81 to smoothly direct the discharging stream of the primary
grinding fluid into and through the discharge outlet with minimum
turbulence in the immediate region of its entry into the discharge
outlet, thereby minimizing the pressure drop in this region with
consequent decrease of pressure and corresponding increase in
vortical velocity and energy of the primary fluid energy stream
circling through the mill.
FIGS. 13 and 14 illustrate still another construction of the
horizontal-type fluid energy mill in which the spider feature of
the present invention may be employed with great advantage to
increase the quantity of energy which is available from the primary
grinding fluid introduced into the mill at a given pressure and so
provide for increased efficiency toward producing a more uniform
and finer grinding of the material being pulverized. In this
construction of mill, a multistage action is obtained by means of
an outer toroidal chamber 85 having a feed material injection inlet
86 through which the material to be pulverized, supplied from a
hopper 87, is entrained in a gaseous stream under suitable
pressure, and injected into the chamber 85 for distribution
circumferentially therewithin.
This outer chamber 85 is also provided with a plurality of
circumferentially spaced nozzles 88 through which the primary
grinding fluid from a suitable source under requisite pressure is
also injected into the chamber 85, which primary grinding fluid
acts to circulate the feed material about the interior of said
toroidal chamber to effect a first-stage reduction in size of the
material particles. This latter chamber is in communication with a
central chamber 89 through a plurality of nozzles 90 uniformly
spaced about the circumference of the central chamber and arranged
with their axes similarly oriented to create a high velocity vortex
of the primary fluid in said central chamber having in its central
region a discharge outlet 91. Further reduction in particle size of
the material being pulverized is effected in this central vortex
chamber 89 and upon reduction to desired size of the particles they
move radially inward of the vortex for eventual discharge through
the outlet 91 with the spent gas in which said finely comminuted
particles are entrained.
As in all of the previously described forms of energy mill, the
outlet 91 is fitted with the spider 92 of the present invention
having its angularly related directional vanes 93 with their end
portions projecting freely beyond the corresponding intake end of
the outlet to achieve the objectives of the present invention as
hereinabove described.
While the spider vanes have been described as having their end
portions exposed preferably a distance equal to from one-half to
the full diameter of the discharge tube in which the spider is
fitted, it is to be understood that while this length of the
exposed portions of the vanes is preferred, the length thereof is
not necessarily limited to the range specified but may be greater
than the diameter of the discharge or less than one-half its
diameter depending upon other design factors of the mill so long as
the exposed portions of the spider vanes are of a length sufficient
to effect smooth, streamlined entry of the spent grinding fluid
into the intake end of the discharge outlet. Also, it will be
understood that while the spider feature of the present invention
may be employed to good advantage in all of the mills hereinbefore
described, the construction of mill as shown in FIGS. 1 to 8
inclusive, insofar as concerns the described relationship of the
feed and grinding jets for conjoint action of each paired set
thereof, provides increased efficiency in operation of the mill
even in the absence of the spider feature for the reasons
hereinbefore set forth. Further, various changes and modifications
may be made from time to time without departing from the general
principles or real spirit of the several different aspects of the
present invention and it is accordingly intended to claim the same
broadly, as well as specifically, as indicated by the appended
claims.
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