U.S. patent number 3,645,813 [Application Number 04/851,764] was granted by the patent office on 1972-02-29 for method of conglomerating fibers.
This patent grant is currently assigned to Feldmuhle Aktiengesellschaft. Invention is credited to Hans Joachim Funke, Hans Dieter Pelikan.
United States Patent |
3,645,813 |
Pelikan , et al. |
February 29, 1972 |
METHOD OF CONGLOMERATING FIBERS
Abstract
Lignocellulose fibers obtained from wood in a defibrator form
conglomerates when held in a state of high turbulence while
suspended in air. Globular conglomerates having diameters of 2 to
30 mm., relatively dense outer shells and loose cores are produced
continuously in a turbulence zone in dwell times of a few
minutes.
Inventors: |
Pelikan; Hans Dieter
(Duesseldorf-Nord, DT), Funke; Hans Joachim
(Duesseldorf-Oberkassel, DT) |
Assignee: |
Feldmuhle Aktiengesellschaft
(Duesseldorf, DT)
|
Family
ID: |
5690287 |
Appl.
No.: |
04/851,764 |
Filed: |
August 20, 1969 |
Foreign Application Priority Data
|
|
|
|
|
Aug 24, 1968 [DT] |
|
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P 17 28 102.6 |
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Current U.S.
Class: |
156/62.4;
366/301; 427/212; 427/427.6; 366/300; 425/80.1; 366/325.1 |
Current CPC
Class: |
D04H
1/425 (20130101); D04H 1/64 (20130101); B01F
7/042 (20130101); D04H 1/732 (20130101); B01J
2/16 (20130101); D04H 1/736 (20130101) |
Current International
Class: |
B01J
2/16 (20060101); D04H 1/70 (20060101); B01F
7/02 (20060101); B01F 7/04 (20060101); B29j
005/00 () |
Field of
Search: |
;156/62.2,62.4,285,377
;259/147,151 ;233/647 |
References Cited
[Referenced By]
U.S. Patent Documents
Primary Examiner: Borchelt; Benjamin A.
Assistant Examiner: Tudor; H. J.
Claims
What is claimed is:
1. A method of combining individual fibers in conglomerates which
comprises:
a. suspending said fibers in a gaseous fluid;
b. confining the suspension so formed in a space between upright
walls;
c. propelling the fibers in a portion of said suspension through
the remainder of said suspension in an upwardly extending path
spaced from said walls until turbulence is produced in said
suspension; and
d. maintaining said propelling and said turbulence until said
conglomerates are formed.
2. A method as set forth in claim 1, the fibers in said portion of
said suspension being propelled in said path at a velocity
sufficient to cause the formation of a turbulent horizontal layer
containing said fibers at a density higher than the density of said
fibers in all portions of said suspension located below said
layer.
3. A method as set forth in claim 1, said fibers essentially
consisting of cellulose or lignocellulose.
4. A method as set forth in claim 3, the fibers in said portion of
said suspension being propelled in said path at a velocity of 2 to
5 meters per second.
5. A method as set forth in claim 4, said velocity being
approximately 3 meters per second.
6. A method as set forth in claim 3, spraying water into said space
in an amount sufficient to increase the moisture content of said
fibers in said space.
7. A method as set forth in claim 1, the fibers in said portion of
said suspension being propelled by agitator blades moving in said
path.
8. A method as set forth in claim 1, the fibers in said portion of
said suspension being propelled in said path by kinetic energy
transmitted thereto by gas injected into said space.
9. A method as set forth in claim 1, spraying a normally solid
material into said space in liquid form for deposition on said
fibers, removing the fibers carrying the deposited material from
said space, and solidifying said material.
Description
This invention relates to a method of combining fibers in
conglomerates. More specifically, the invention is concerned with
the conglomeration of fibers suspended in a fluid by agitating the
suspension so as to produce turbulence in the same.
While it is usually desired to prevent fibers from conglomerating
while they are being processed and purified, fiber conglomerates
are known to have properties desirable in many applications. The
conglomerates are generally of low-bulk density, soft, and
yieldably resilient, and may be combined with binders or with other
materials to form load-bearing or other construction elements not
readily produced from loose fibers with equally desirable
results.
It is known to make soft webs, feltlike materials, hard plates and
boards, and other shaped bodies from such fiber conglomerates, and
to use the conglomerates without or with minor amounts of binders
in bulk as insulating materials. Plates having excellent acoustical
and thermal insulating properties have been prepared from such
fiber conglomerates and plasticized polyvinyl chloride, and other
applications have been proposed heretofore.
It is known to combine individual fibers in conglomerates by
dispersing or suspending the fibers in a liquid aqueous fluid at
very low concentration, and to agitate the suspension to produce
mild turbulence, until the desired, generally globular
conglomerates are formed. The process is very slow, and it is
necessary to agitate the suspension for several hours before
conglomerates of useful size are formed.
The suspension must then be filtered to separate the conglomerates
from most of the liquid phase, and the fibrous material must be
dried to remove the remainder of the water before further
processing or storage is possible. The method requires much
equipment if a reasonable output rate is to be maintained.
The object of this invention is the provision of a method which
permits fibers to be combined in conglomerates at a much faster
rate than is possible by the aforedescribed known method,
preferably in continuous operation.
Surprisingly, it has been found that many of the shortcomings of
the known method can be overcome by replacing the aqueous carrier
by a gaseous fluid in which the fibers are suspended, and which is
kept in turbulent motion. Rapid conglomeration is achieved when the
suspension is confined in a space between upright walls, and
turbulence is produced therein by propelling the fibers in a
portion of the suspension through the remainder of the suspension
in an upwardly extending path spaced from the confining walls.
The velocity at which the fibers are propelled in the
aforementioned path should be such as to cause the formation of a
turbulent horizontal layer which contains fibers at a density
higher than the density of the fibers in all portions of the
suspension located below the layer.
When the fibers essentially consist of cellulose or lignocellulose,
the preferred fiber material, the upward velocity should be between
2 and 5 meters per second, and best approximately 3 meters per
second. The formation of conglomerates is further accelerated if
water is sprayed into the space in an amount sufficient to increase
the moisture content of the fibers.
The fibers may be propelled upwardly in the aforementioned path by
agitator blades which move in the path, or they may be propelled by
kinetic energy transmitted thereto by gas injected into the
space.
The conglomerates may be given a wide variety of desirable
properties by spraying normally solid materials into the processing
space in liquid form for deposition on the fibers, removing the
fibers from the space, and solidifying the deposited material.
When mechanical agitation is preferred, suitable equipment may
include a container and two shafts whose axes extend in a common
horizontal direction, and which are spaced from each other in a
horizontal direction. Blades project radially from each shaft in
the container, at least one blade projecting from each shaft being
interposed between the two shafts. The shafts are driven
simultaneously in respective directions to cause the interposed
blades to move in an upward direction. Fibers are fed to the
container adjacent an axially terminal portion of one of the
shafts, and conglomerated fibers are discharged from the container
adjacent the other axially terminal portion of the shaft.
Other features, additional objects, and many of the attendant
advantages of this invention will readily be appreciated as the
same becomes better understood by reference to the following
detailed description of preferred embodiments when considered in
connection with the appended drawing in which:
FIG. 1 illustrates a device for producing fiber conglomerates of
the invention in continuous operation, the view being in front
elevational section;
FIG. 2 shows the device of FIG. 1 in side elevational section on
the line II--II; and
FIG. 3 illustrates a modified device of the invention in a view
corresponding to that of FIG. 2.
Referring initially to FIGS. 1 and 2, there is seen an elongated
trough 1 whose bottom wall has two cylindrically arcuate sections
meeting in a ridge along the longitudinal centerline of the trough.
A tall cover 2 is flanged to the horizontal top rim of the trough
to enclose a chamber with the same. Openings 3 are provided in the
top portion of the cover 2 and normally hold nozzles, omitted from
the drawing for the sake of clarity, which permit a liquid to be
sprayed into the chamber in a downward direction, as indicated by
arrows. A chute 4 is provided at one longitudinal end of the cover
2 for feeding fiber material to the chamber from above. A discharge
chute 5 is provided on the transverse end wall of the chamber
remote from the feeding chute 4 and closely below the topmost
portion of the cover 2.
Agitating equipment installed in the chamber includes two shafts 6
journaled in bearings 11 outside the chamber, passing freely
through the end walls of the chamber, and approximately coaxial
with the two cylindrical bottom sections respectively. Two groups
of diametrical arms project from each shaft and are offset
90.degree. from each other. The arms are distributed on the
associated shaft 6 over the entire chamber length in axially spaced
relationship, arms of one group alternating with arms of the other
group. The free ends of each arm carry blades 7 inclined about
45.degree. to the radial plane in which the arm rotates.
A V-belt pulley 8 on the free end of one of the shafts 6 outside
the chamber enclosed by the trough 1 and the cover 2 is connected
by a drivebelt to an electric motor 9. Meshing spur gears 10 on the
two shafts cause the blades 7 associated with the two shafts to
revolve in opposite directions about the axes of the associated
shafts, the arrangement being such, as best seen in FIG. 2, that
the blades 7 between the shafts 6 move upwardly in a path above the
ridge in the bottom wall of the trough 1 in interdigitating
relationship, the arms on the two shafts being out of phase by
45.degree..
An opening in the bottom wall of the trough 1 below the discharge
chute 5 is covered with a coarse screen 12, and a nonillustrated
conveyor leads from the area below the screen 12 to the
nonillustrated storage bin from which the feed chute 1 feeds fibers
into the chamber.
In the modified device shown in FIG. 3, the mechanical agitation
equipment is replaced by pneumatic devices. A trough 1 and cover 2
identical with the corresponding elements described above with
reference to FIGS. 1 and 2 constitute the walls of a chamber into
which material may be sprayed from above through nonillustrated
nozzles set into openings 3 of the cover 2. Partitions arranged
along both upright, longitudinal chamber walls enclose a manifold
inlet duct 13 which extends over the entire length of the chamber
and communicates with the same through closely spaced nozzles 14
distributed over the length of each manifold duct contiguously
adjacent the cylindrical bottom wall section or through a
corresponding slot. The nozzles 14 direct substantially tangential
jets of gas against the associated wall section in a direction
toward the central ridge of the bottom wall at which the two
streams converge.
An outlet duct is arranged above each manifold duct 13 and is
longitudinally coextensive with the same. It is separated from the
central main portion of the chamber by a screen 16. Pumps 17
arranged next to the upright longitudinal chamber walls draw air
from the chamber through the screens 16 and conduits 15, and return
the air under pressure to the manifold ducts 13.
The flow pattern observed in the chamber when the pumps 17 are
operated is indicated by arrows in FIG. 3. The two airstreams
meeting at the ridge in the chamber bottom mingle and mainly flow
upward toward the cover 2 in a straight path until the combined
stream is again split and deflected in two opposite lateral
directions by the suction in the conduits 15. An area of turbulence
thus extends on either side of the vertically rising central
stream.
In actual embodiments of the illustrated devices, the chambers
bounded by the troughs 1 and covers 2 had each a length of 2
meters, a height of 1 meter and a width of 1.2 meters. Other
dimensions are evident from the drawing. They were employed for
making globular conglomerates of lignocellulose fibers produced
from pine wood on a conventional defibrator. The fibers ranged in
length from 1.8 to 4.5 mm., averaging 3.1 mm., and in diameter from
0.014 to 0.046 mm., averaging 0.035 mm. The bulk weight of the
fibers was 50 kg./m.sup.3.
The following Examples 1 to 3 illustrate the operation of the
apparatus of FIGS. 1 and 2.
EXAMPLE 1
The shafts 6 were rotated at 91 r.p.m. The fibers which contained 8
percent moisture were fed continuously to the chamber at a rate of
10 kg./min. The dwell time in the chamber was 3 minutes, and the 30
kg. of fibers present in the chamber filled the same to
approximately one third, the remainder of the chamber being
occupied by air.
The blades 7 imparted sufficient upward motion to the fibers to
produce a relatively dense layer of fibers in the chamber near the
top of the cover 2 which looked somewhat like the surface of a
gently boiling, somewhat viscous liquid, such as bubbling pea soup.
Turbulence in the top layer of the fiber suspension was intense,
and a multiplicity of localized eddies was clearly discernable
through an inspection window in the cover 2, not shown in the
drawing. The fiber density in the turbulent top layer was much
higher than in the lower portion of the chamber.
The turbulent suspension was sprayed through the openings 3 with an
aqueous solution of a catalyzed urea formaldehyde precondensate
containing 50 percent resin-forming material at a rate of 2 kg. of
solution per 10 kg. lignocellulose fibers. Globular fiber
conglomerates bonded by partly set urea formaldehyde resin were
continuously discharged from the chute 5. They lost their excess
moisture quickly while the resin fully set, and thereafter had
relatively high crushing strength.
The dried and fully cured conglomerates were employed in bulk for
filling cavities in building walls to improve acoustical and
thermal insulating properties of the walls. They also could be fed
directly from the cute 5 to a press in which they were converted to
insulating boards under heat and pressure.
EXAMPLE 2
Electric heaters were attached to the outer walls of the apparatus
shown in FIGS. 1 and 2 and supplied with current of a strength
sufficient to maintain a temperature of 120.degree. to 130.degree.
C. in the chamber. The fibers were preheated to the same
temperature before being fed to the chamber through the chute 4,
and lost some of their initial moisture content of 8 percent during
heating. The blades 7 revolving at 91 r.p.m. caused the
conglomeration of a major portion of the individual fibers when
they had traveled over about one-half of the axial length of the
chamber.
They were sprayed in the longitudinal half of the chamber near the
discharge chute 5 with high-vacuum asphalt having a drip point of
85.degree.-95.degree. C. which was sprayed into the chamber at a
rate of 9 kg. per 10 kg. of fiber at a temperature of 230.degree.
C. and at 15 atmospheres gage pressure.
The globular fiber conglomerates impregnated with the bituminous
material which were discharged from the chute 5 were readily
converted under moderate pressure to insulating plates of excellent
thermal and acoustical properties and impervious to moisture.
EXAMPLE 3
Fibers fed to the chute 4 as described in Example 1 were sprayed
through the openings 3 with a latex of styrene butadiene copolymer
containing 45 percent solids. The latex was applied at a rate of
2.5 kg. per 10 kg. of lignocellulose fibers.
The fiber conglomerates charged with latex which were obtained in
this manner were resilient and could be further processed for form
continuous webs or plates similar in their properties to commercial
floor covering material prepared from fiber felt and polyvinyl
chloride.
The operation of the pneumatic apparatus shown in FIG. 3 is
illustrated by Examples 4 to 7.
EXAMPLE 4
Defibrator stock of the type described above and still containing
40 percent moisture was fed to the chamber at a rate of 10 kg./min.
while air was injected from the nozzles 14 at a velocity of 50
m./sec. and at a rate of 20 m..sup.3 /sec. A turbulent, relatively
dense fiber layer formed in the upper portion of the chamber, and
most fibers were converted, mainly in the dense layer, to globular
conglomerates of relatively low mechanical strength. Those fibers
which traveled through the chamber without forming conglomerates
ultimately dropped through the screen 12 and were returned to the
chute 4.
After drying, they were sufficiently coherent for use as bulk
insulating material that could be poured into cavities in guiding
walls and the like.
EXAMPLE 5
The fibrous material received from the defibrator with a moisture
content of 40 percent was predried to 8 percent moisture, and was
thereafter subjected to intensive turbulence in the apparatus of
FIG. 3 by means of air injected in the manner described in Example
4.
The globular fiber conglomerates discharged from the chute 5 were
even looser than those obtained in Example 4. They were ready for
use as a bulk insulating material having thermal and acoustical
properties far superior to those of the starting material.
EXAMPLE 6
The procedure of Example 5 was modified by spraying water droplets
fine enough to form a fog on the turbulent fiber material in the
chamber through the openings 3 at a rate of 3 kg. water per 10 kg.
fibers. The mechanical strength of the conglomerates so obtained
was superior to that of the material produced in the method of
Examples 4 and 5.
EXAMPLE 7
The method of Example 6 was further modified by replacing the water
sprayed through the openings 3 by an equal weight of an aqueous
solution containing 70 g. sodium pentachlorophenate per kilogram
water. The sodium pentachlorophenate not only provided protection
against insects and fungi, but the globular fiber conglomerates so
produced were stronger than those obtained from the procedures of
Examples 4 to 6, though not as strong as the conglomerates bonded
with synthetic resin (Example 1).
Defibrator stock obtained from soft wood without the use of
chemicals is the cheapest fibrous material available to us at this
time. It is preferred for this reason and has been described with
reference to all Examples. However, pure cellulose fibers, fibers
of animal origin, synthetic fibers, and fiber mixtures have been
converted to globular conglomerates within a few minutes as
described above.
It is believed that the fibers are partly interlocked in lumps as
they move at different speeds, and partly in opposite directions in
the generally rising stream above the rib in the trough bottom, and
that the loosely cohering groups of fibers so produced assume the
globular shape in the intensely turbulent zones. Lignocellulose
fibers, such as those produced from wood on a defibrator, have been
found to be superior to most other fibers in their ability of
aggregating or interlocking with each other. Their resiliency is
high, and the conglomerates formed have thus desirable properties
for use as principal ingredients or fillers in compositions for use
in construction work.
Moisture present in the conglomeration zone has been found to
hasten the formation of the globular bodies from cellulose,
lignocellulose, and chemically related fibers. The water need not
necessarily be present in the liquid form, and steam has been used
successfully. The water is believed to be effective by its surface
tension and by the bonding effect of its hydroxyl groups. The small
amount of water which is preferably employed is readily removed
during a short air-drying period or by hot pressing of the
conglomerates.
The normally solid bonding and impregnating agents described in
Examples 1, 2, 3, and 7 are merely illustrative of the materials
which may be employed for modifying the mechanical and other
properties of the fiber balls, and other materials will readily
come to mind which are suitable for application while in a liquid
state, in the form of their melts or solutions, and which can
thereafter be made to solidify by lowering their temperature or by
evaporating a solvent. Water-repellent, flame-retarding, and
pest-control agents have been applied in the manner obvious from
Example 7.
Bonding agents based on polymers other than ureaformaldehyde resin
or styrene-butadiene copolymer have been used to produce basically
fibrous balls whose properties could readily be predicted from the
nature of the synthetic material. Plasticized polyvinyl chloride
has been employed in preparing globular conglomerates of the
invention which were thereafter converted to floor covering sheets
by hot pressing. The ratio of fibers to resin and the pressure
employed during pressing may be varied to adapt the ultimate
product to the intended use. Phenolic resins have been sprayed on
lignocellulose fibers in a procedure similar to that of Example 1,
and the resin was fully cured on the globular bodies discharged
from the chute 5 while the material was converted to storing plates
under high pressure. Such plates have been found to resist
weathering well and to be suitable for wall shingles and the like.
The fiber conglomerations of the invention have also been mixed
with plaster and with cement as fillers in the production of
prefabricated boards and plates capable of carrying loads in
building constructions.
The fiber conglomerates when produced without additives other than
water or other volatile liquids have a globular shell whose fiber
density is higher than that of the interior or core. When
impregnating agents are applied to the fibrous material at a stage
in which the shell has been formed, relatively little of the
impregnating material reaches the core. The procedure described in
Example 2 is therefore preferred when the fiber balls are intended
to be bonded to each other by means of thermoplastic material in a
subsequent hot pressing operation. The penetration of the
conglomerates by the bituminous material sprayed into the chamber
can be controlled precisely by selecting the temperature prevailing
in the chamber and the temperature of the sprayed material.
While not specifically illustrated, it will be understood that
bonding of lignocellulose fiber conglomerates in a hot-pressing
operation can be accomplished by admixing minor amounts of
thermoplastic synthetic fibers to the defibrator stock either prior
to entry into the chamber or in the chamber itself.
When streams of gas are employed for suspending the fibers and for
generating turbulence in the suspension, impregnating agents may be
admixed to the gas outside the chamber in an obvious manner, rather
than introduced into the chamber itself. Gases other than air may
be employed if so desired.
The relatively dense, turbulent fiber layer which is thought to be
essential for the rapid formation of globular fiber conglomerates
in the method of the invention is readily observed, and other
process variables have to be adjusted accordingly. The specific
conditions of agitation described above have been found
satisfactory for a chamber of the illustrated shape and the
described dimensions when processing lignocellulose defibrator
stock. The necessary modifications for operation under other
conditions have to be determined experimentally.
The angle between the driving surfaces of the blades 7 and a radial
plane may have to be reduced to as little as 5.degree., and the
blades illustrated in FIGS. 1 and 2 are adjustable over this range
by means of nonillustrated threaded studs, nuts, and slots employed
for fastening the blades to the diametrical arms in a basically
conventional manner. The dwell time of the fibrous material in the
chamber is closely related to the blade angle and to the rotary
speed of the shafts 6.
Under otherwise unchanged conditions, the dwell time, and
particularly the time spent by the fibers in the turbulent, dense,
top layer determines the diameter of the fiber balls formed which
is readily varied between 2 and 30 mm., being approximately 15 mm.
in the material produced in Examples 1 to 7.
The oblique position of the blades 7 also has been found to cause
individual fibers to turn about their longitudinal axes while they
are being propelled upwardly in the central zone of the chamber.
Rapid conglomeration of fibers is thought to be due to this turning
movement.
In the apparatus illustrated in FIGS. 1 and 2, the desired
turbulent fiber layer is formed at circumferential blade velocities
of approximately 2 to 5 meters per second. At rotary speeds too low
to result in a circumferential velocity of 2 m./sec., an effective
turbulent layer is not formed. At blade velocities higher than 5
m./sec., conglomerates formed by turbulence tend to be broken up by
the blades or by collision with other conglomerates traveling at
the same velocity as the blade circumference. Most rapid
conglomeration is normally achieved at a blade velocity of about 3
m./sec.
In the pneumatic agitation system shown in FIG. 3, the amount of
air supplied, the cross section and direction of the nozzles 14 are
adjusted in such a manner that the fibers move upwardly in the
central chamber zone at a velocity similar to that achieved in the
mechanical system, that is, at 2 to 5 meters per second, and
preferably at about 3 meters per second.
* * * * *