U.S. patent number 3,825,175 [Application Number 05/367,684] was granted by the patent office on 1974-07-23 for centrifugal particle elutriator and method of use.
This patent grant is currently assigned to The United States of America as represented by the United States Atomic. Invention is credited to Walter K. Sartory.
United States Patent |
3,825,175 |
Sartory |
July 23, 1974 |
CENTRIFUGAL PARTICLE ELUTRIATOR AND METHOD OF USE
Abstract
A method and apparatus for carrying out centrifugal elutriation
using a rotatable cylinder having an annular cavity within. Samples
are introduced into the cavity at a central part thereof. A
suspending liquid is introduced into the cavity at the centrifugal
side. A first portion of particles within the sample moves in the
centripetal direction with the flowing liquid and a second portion
of larger particles moves in the centrifugal direction. Exit ports
at the centripetal and centrifugal sides of the cavity provide a
means for continuously removing the separated first and second
portions of particles.
Inventors: |
Sartory; Walter K. (Oak Ridge,
TN) |
Assignee: |
The United States of America as
represented by the United States Atomic (Washington,
DC)
|
Family
ID: |
23448183 |
Appl.
No.: |
05/367,684 |
Filed: |
June 6, 1973 |
Current U.S.
Class: |
494/27; 494/37;
494/36 |
Current CPC
Class: |
B04B
5/0442 (20130101); B04B 5/06 (20130101); B04B
2005/0471 (20130101) |
Current International
Class: |
B04B
5/04 (20060101); B04B 5/06 (20060101); B04B
5/00 (20060101); B04b 003/00 (); B04b 005/06 () |
Field of
Search: |
;233/2,26,27,28,21,16,15,31 |
References Cited
[Referenced By]
U.S. Patent Documents
Foreign Patent Documents
Primary Examiner: Krizmanich; George H.
Attorney, Agent or Firm: Horan; John A. Zachry; David S.
Hardaway; John B.
Claims
What is claimed is:
1. A method for separating particles which are suspended within a
suspending liquid, comprising the steps of:
continuously introducing a sample comprising said particles and
said suspending liquid into a central portion of a bound rotating
cavity, a first portion of said particles having different settling
velocities from a second portion of said particles within said
suspending liquid;
flowing a liquid, which is the same liquid as said suspending
liquid of said sample, from the centrifugal side of said cavity
toward the centripetal side of said cavity at a velocity which is
intermediate the settling velocities of said first and second
portion of said particles, whereby the faster settling portion of
said particles move in the centrifugal direction and the slower
settling particles move in the centripetal direction along with
said flowing liquid;
removing said faster settling particles and suspending liquid from
the centrifugal side of said cavity; and
removing said slower settling particles and suspending liquid from
the centripetal side of said cavity.
2. The method according to claim 1 wherein said sample is whole
blood, said slower settling particles are white blood cells, said
faster settling particles are red blood cells and said suspending
liquid is plasma.
3. A centrifugal elutriator, comprising:
a rotor housing (1) enclosing a right toroidal cavity (6)
concentrically located about an axis of said housing, said cavity
having a centrifugal boundary and a centripetal boundary, said
centrifugal boundary being located at a radial distance from said
axis which is greater than the radial distance of said centripetal
boundary from said axis.
first conduit means (7) communicating with said cavity at a point
adjacent said centrifugal boundary,
second conduit means (9) communicating with said cavity,
third conduit means (10) communicating with said cavity at a point
centripetally located from said second conduit means and generally
centrally located on a radius of said cavity,
fourth conduit means (8) communicating with said cavity at a point
centripetally located from said third conduit means and adjacent
said centripetal boundary, said first, second, third, and fourth
conduit means communicating with the exterior of said housing;
and
a pervious baffle (2) concentric with said centrifugal and
centripetal boundaries axially traversing at least a portion of
said cavity and attached to said housing at a radius intermediate
said first and third conduit means whereby fluid entering through
said first conduit means flows through said baffle to reach any of
said conduit means.
4. The apparatus according to claim 3 further comprising a second
pervious baffle (4) located between said third and fourth conduit
means.
5. The apparatus according to claim 3 wherein said pervious baffle
extends across the entire axial height of said cavity.
6. The apparatus according to claim 3 wherein said baffle extends
across only a portion of said cavity and a concentric partition
extends from said pervious baffle to said centrifugal boundary,
whereby said first conduit means communicates with said cavity
within the space defined by said pervious baffle, said partition
and said centrifugal wall and said second conduit means is located
centrifugally of said pervious baffle and on the opposite side of
said cavity from said first conduit means.
Description
BACKGROUND OF THE INVENTION
This invention was made in the course of, or under, a contract with
the U.S. Atomic Energy Commission. It relates generally to the art
of centrifugal elutriation.
The prior art in many areas of technology has used elutriation as a
means of separating particles of similar densities but of different
effective diameters. The process is based generally upon an
application of Stokes Law of sedimentation. The process is applied
to particles smaller than about 100 microns. When particle sizes
are below approximately 40 microns centrifugation has been used to
speed up the settling process.
In the field of blood separation centrifugation has been used in a
batch type operation for separating the various constituents. One
such prior art technique is that of Lindahl et al., IVA. Tidskrift
for Teknisk Vetenskoplig Forskning 26, 309 (1955). This apparatus
comprises a cone-shaped inclined cavity within a rotating disc,
with a side loop attached to the cavity. The inclination and side
loop serve the purpose of minimizing recirculation currents and
thus mixing. However, even with this design recirculation currents
and mixing still occur.
Another such apparatus is described by McEwen et al., Analytical
Biochemistry 23, 369-377 (1968). This apparatus comprises a
rotatable disc having a kite-shaped cavity in a radial portion
thereof. The sample to be separated is pumped into the centrifugal
side of the cavity while the disc is rotating. The slower settling
particles are thus pumped out of the centripetal side of the cavity
while the faster settling particles are retained within the cavity.
By varying the speed of rotation, various size particles can be
pumped out of the cavity one at a time.
Another prior art technique involves the use of a suspending liquid
whose viscosity is varied over time. The settling rate of the
particles being separated is effected by the viscosity of the
suspending medium in accordance with Stokes Law.
The above prior art techniques generally utilize the concept of
flow through a finite void within a rotating disc. Several inherent
disadvantages result from such operation. In the above techniques
the flowing contents of the cavity come into contact with radial
walls during the separation process. This gives rise to Coriolis
force effects which cause turbulence along the wall fronting
rotation and mixing of the particles which are being separated.
Another problem with the above prior art is that the fluid is
introduced into the cavity at the section of smallest cross section
and moves in the centripetal direction into sections of increased
cross section. This causes the overall velocity to decrease as the
fluid moves in the centripetal direction. It is known from the
technology of fluidization that a high fluid velocity leads to a
low particle concentration and, therefore, to a low suspension
density. As a result, the suspension density within the cavity
tends to be low at the outer radius, and to increase in the
centripetal direction. Such a density configuration is unstable
(like trying to suspend a layer of mercury above a layer of water
in a beaker) and will lead to turnover and turbulent mixing. In
addition, since laminar flow exists at the radial boundaries of the
void, the central portion of the fluid has a greater velocity than
that of the fluid in the laminar flow of the boundaries. This tends
to cause convective mixing.
A particular problem with the above prior art processes as they are
applied to blood separation, as well as to other separations, is
that there is a density gradient in the particlees due to the
varied velocities in the different cross section area regions of
the void. This results in turbulent mixing of the particles.
Another result of the radial velocity gradient is that different
shear conditions exist in regions of different velocity. Blood
particles are composed of aggregate particles. Under conditions of
high shear the aggregates are broken up into primary particles.
Under conditions of low shear the particles reaggregate and move in
the centrifugal direction only to again be broken up.
In addition to the above problems which militate against achieving
any separation at all, the processes are only applicable to batch
operation. Thus such systems would not be amenable to a continuous
process wherein a particular blood constituent is removed from the
blood of a donor, and the remaining plasma and blood constituents
are returned to the donor in a single continuous operation.
SUMMARY OF THE INVENTION
It is thus an object of this invention to provide a new method and
apparatus for centrifugal elutriation in which the fluid does not
come into contact with axially extending radial walls.
It is a further object of this invention to provide a method of
centrifugal elutriation wherein shear conditions are such that
there is no inversion of aggregate particles.
These and other objects are accomplished by introducing a sample to
be separated into a toroidal cavity concentrically located within a
rotating disc at a point intermediate the centrifugal and
centripetal boundaries of the cavity, evenly flowing a suspending
medium from the centrifugal boundary of the cavity toward the
centripetal boundary removing faster settling solids and suspending
medium from the centrifugal portion of the cavity and removing
slower settling particles and suspending medium from the
centripetal portion of the boundary.
BRIEF DESCRIPTION OF THE DRAWINGS
FIG. 1 is a sectional oblique drawing of a rotor housing according
to this invention.
FIG. 2 is a sectional view of an alternative construction of a
rotor housing according to this invention.
FIGS. 3 and 4 are graphs used in determining the overall geometry
of a rotor housing according to this invention.
DETAILED DESCRIPTION
According to this invention it has been found that axially
extending radial walls may be completely dispensed with in a
centrifugal elutriator. A cross section view of the elutriator of
this invention is shown in FIG. 1. The elutriator is comprised of a
housing (1) having a right toroidal cavity (6) enclosed within it.
Conduit means (7), (8), (9), and (10) communicate with the cavity
at various locations. Conduit means (7) serves as an introductory
port for suspending fluid used in the process of this invention.
Conduit means (10) serves as a sample introduction port. Conduit
means (8) and (9) are respectively the centripetal and centrifugal
exit ports. The conduit means are pipe-like orifices which pass
from the central entrance to their respective openings in the
cavity. For small centrifuges (less than about 15 centimeters in
radius) a conduit means every 30.degree. or 12 conduit means for
each of those illustrated in FIG. 4 is sufficient for satisfactory
flow. However, any other arrangement, such as disc-shaped cavities,
which allows for uniform flow may be used.
Pervious baffles (2) and (4) through which suspending medium and
particles can flow are provided at the centrifugal and centripetal
sides of the cavity. Outer baffle (2) is necessary for assuring
that the suspending medium, which is introduced through conduit
means (7), flows into the central portion of the cavity at an even
and uniform velocity around the cavity. Such even flow minimizes
mixing effects which would otherwise be present. Inner baffle (4)
is not absolutely necessary for the successful operation of the
apparatus. However, it is preferred to incorporate baffle (4) into
the apparatus so as to minimize and evenly distribute any suction
effects which may arise from conduit means (8).
The pervious baffles may be in the form of wire mesh or perforated
sheet. It is preferred, however, that the baffles be constructed of
porous material having open porosity with a size on the order of
the material being separated. Porous polytetrafluoroethylene having
a pore size of about 25 microns, which is commercially available,
is desirable for use when blood is being separated. The baffles may
also be in the form of a packed bed of beads.
Rotor (1) is of the type of construction as is conventional with
centrifuges. Appropriately grooved and drilled stacked plates of
stainless steel bolted at the periphery provide a suitable
construction. However, when blood is being separated it is
necessary for the stainless steel to be coated with an inert
material such as polytetrafluoroethylene.
Conventional temperature control and rotating means may be
employed. For example, the control system used in the K series
centrifuge may be employed with the rotor of this invention. Such
means are described by Brantley et al. in "K-Series Centrifuges,"
Analytical Biochemistry 36, 434-442 (1970).
An alternate form of construction is shown in FIG. 2. In this
alternative embodiment, pervious baffle (2') extends only partially
across cavity (6) and partition (13) intersects baffle (2') so as
to define a flow path for liquid flowing through conduit means (7)
through pervious baffle (2'). In this case, conduit means (9') is
displaced centrifugally from pervious baffle (2') in areas where no
counterflow occurs. Such an arrangement provides for a higher
degree of packing of faster settling particles prior to
removal.
The process of this invention is generally applicable to particles
within the size range of from about 100 microns to 100 A. Although
a broad spectrum of particle sizes may exist within the above
range, the process of this invention is designed to divide the
particles into two groups, one of which is larger than the dividing
size and the other of which is smaller than the dividing size. The
process of this invention is carried out by the continuous
introduction of a sample comprising particles and a suspending
liquid into the cavity (6) through conduit means (10) while
simultaneously flowing suspending liquid through conduit means (7)
while rotating housing (1) at an appropriate velocity. The
particles introduced through port (10) tend to move toward
centrifugal boundary (12) at varying velocities due to the
centrifugal field existing within the rotating housing. Different
size particles tend to settle toward centrifugal boundary (12) at
different velocities generally as is predicted from Stokes Law.
Suspending liquid flowing through conduit means (7) is forced
through cavity (6) at a velocity which is intermediate the settling
velocities of the particles introduced through conduit means (10).
Thus, particles which are settling at a velocity which is greater
than the velocity of suspending fluid entering through conduit
means (1) move in the centrifugal direction and out through conduit
means (9). Particles which are settling at a velocity which is less
than the velocity of the flowing suspending liquid move in the
centripetal direction and out through conduit means (8). In
carrying out the process of this invention there are four flow
rates which must be monitored and regulated to achieve satisfactory
results. The four flow rates are as follows.
First, the flow of incoming sample through conduit means (10);
Second, the flow of suspending medium through conduit means
(7);
Third, the flow of slower settling particles and suspending medium
through conduit means (8); and
Fourth, the flow of rapidly settling particles and suspending
medium through conduit means (9).
The first and second flow rates are determined by geometry
considerations which are discussed below. The third and fourth flow
rates are best determined by regulating the fourth flow rate so as
to maintain the radial separation interface of the fast and slow
settling particles between conduit means (10) and inner pervious
baffle (4). This can be done by observing the separated products or
by providing transparent windows in the rotor housing so that the
interface may be observed either visually or photometrically. The
interface is preferably located centrally between conduit means
(10) and inner pervious baffle (4).
In carrying out the present invention the overall geometry of the
apparatus must be based upon the particular fluid particle system
upon which the apparatus will operate. As an example, an apparatus
designed to separate while cells from 1.0 cm.sup.3 /sec. of whole
blood with a typical red cell volume fraction of 0.45 is described
as follows. A maximum volume of cavity (6) is stipulated as 500 cc
since this is a safe volume to remove from a donor.
The sedimentation coefficient of white cells in plasma at
37.degree.C is about
S.sub.w = 12 .times. 10.sup.-.sup.8 sec.
The sedimentation coefficient of red cells depends on the degree to
which individual cells combine to form large aggregates. This
tendency varies from individual to individual. Shearing the blood
just before sedimentation tends to break up the larger aggregates
and thus to reduce the sedimentation velocity. We consider here the
value
S.sub.r = 12 .times. 10.sup.-.sup.7 sec.
which should be readily attainable with blood from most individuals
if severe shearing is avoided. This value allows for a moderate
amount of shearing in the tubes and seals which deliver the blood
to the separation apparatus.
The volume fraction of white cells (C.sub.W) in blood is normally
about 0.002. This small value makes possible a convenient
approximation that C.sub.W is too small to appreciably affect the
sedimentation velocities of either red or white cells. ith the aid
of this approximation, the plots of FIGS. 3 and 4 have been
prepared to aid in determining the size of the apparatus required
and the amount of flow which must be pumped through the porous or
perforated baffles.
In FIG. 3, the ordinate is defined as:
red cell throughput = FC.sub.R.sup.F /.omega..sup.2 r.sub.F.sup.2
2.pi.lS.sub.R
where
F = volumetric flow rate of blood in the stream feeding the
separator (in cm.sup.3 /sec.)
C.sub.r.sup.f = concentration of red cells in the stream feeding
the separator (volume fraction)
r.sub.F is the radial location of conduit means (10) (cm)
l is the axial length of the separator cavity (cm)
In FIG. 4, the ordinate is defined as:
"Elutriation flow" = E/.omega..sup.2 r.sub.F.sup.2
2.pi.lS.sub.R
where
E = volumetric flow rate of plasma through pervious baffle (2)
(cm.sup.3 /sec.)
In both FIGS. 3 and 4, the abscissa is the concentration of red
cells in the stream feeding the separator, C.sub.R.sup.F.
Since the capacity as shown in FIG. 3 is increased by using lower
feed concentrations, we dilute the whole blood to a concentration
of C.sub.R.sup.F = 0.30 before introducing it to the separator. We
choose a rotor speed of 700 rpm and a feed port radius of r.sub.F =
10 cm. These values are convenient and lead to a radial
acceleration of about 55 times gravity which does not damage blood
cells.
From FIG. 3 at C.sub.R.sup.F = 0.30
Fc.sub.r.sup.f /.omega..sup.2 r.sub.F.sup.2 2.pi.lS.sub.R =
0.076
The axial length of the cavity required is then
l = 1.9 cm.
From FIG. 4, at C.sub.R.sup.F = 0.30
E/.omega..sup.2 r.sub.F.sup.2 2.pi.lS.sub.R = 0.195
The volumetric throughput of plasma through the porous baffles is
then
E = 1.16 cm.sup.3 /sec.
Typical dimensions for an elutriator under the above conditions
would then be:
radius of centripetal wall (11) 6 1/2 cm.
radius of centripetal baffle (4) 7 1/2 cm.
interface of red and white cells 8 1/2 cm.
conduit means (10) 10 cm.
centrifugal baffle (2) 10 1/2 cm.
centrifugal wall (12) 11 1/2 cm., and
axial height 1.9 cm.
The above equations and approximations can, of course, be used to
determine the elutriator geometry for any system in which
separation is desired. The process and apparatus of this invention
may also be used in more than one stage. For example, red and white
cells may be separated in a first stage and plasma separated from
the red and white cells in second and third stages. On the other
hand, the products of the first stage may be again separated to
achieve a higher separation quality. It is readily apparent that
additional stages may be built into the same rotor housing by
merely stacking the stages one against the other or that other
separate stages may be used.
* * * * *