MIDLE HELMUT I (US)
MIDLE HELMUT I (US)
US4169714A | 1979-10-02 | |||
US4699633A | 1987-10-13 | |||
US5332562A | 1994-07-26 |
1. | Apparatus for scavenging in a gas stream fine particles having a first particle size distribution, said gas stream having a first concentration of large particles therein having a second particle size distribution larger than said first particle size distribution, said apparatus comprising means for electrically charging said fine particles to a first polarity; and means for increasing the concentration of large particles in said gas stream relative to said first concentration by introducing into said gas stream scavenger particles having a larger particle size distribution than said first particle size distribution, said scavenger particles having first been electrically charged to a second polarity opposite said first polarity, said scavenger particles scavenging said fine particles by causing said fine particles to agglomerate to said scavenger particles. |
2. | The apparatus of claim 1, further comprising means for removing the agglomerated particles from said gas stream. |
3. | The apparatus of claim 3, wherein said means for removing said agglomerated particles comprises an electrostatic precipitator. |
4. | The apparatus of claim 3, wherein said means for removing said agglomerated particles comprises a baghouse. |
5. | The apparatus of claim 3, further comprising means for classifying the size of particles precipitated by said electrostatic precipitator, and wherein a portion of said scavenger particles are obtained as a result of said classification. |
6. | The apparatus of claim 1, wherein said scavenger particles comprise carbon. |
7. | The apparatus of claim 1, wherein said fine particles range in size from 0.2 to lμm. |
8. | The apparatus of claim 1, wherein the number of said charged large particles introduced to said gas stream is greater than or equal to the number of said fine particles in said gas stream, multiplied by: the square of the radii of said fine particles divided by the square of the radii of said large particles. |
9. | The apparatus of claim 1, wherein said fine particles and said large particles in a quasi uniform field and DC voltages and superimposed pulses are applied. |
10. | Apparatus for scavenging in a gas stream fine particles having a first particle size distribution, said gas stream having a first concentration of particles having a particle size distribution larger than said first particle size distribution, said apparatus comprising: first separating means through which said gas stream passes for causing particles having a particle size distribution larger than said first particle size distribution to separate from said gas stream; means for electrically charging to a first polarity said fine particles having said first particle size distribution and having exited said first separating means m said gas stream without having separated from said gas stream; means for electrically charging to a polarity opposite said first polarity a plurality of large particles having a particle size distribution larger than said first particle size distribution; means for introducing to said gas stream having exited said first separating means said plurality of charged large particles so that said gas stream has a higher concentration, relative to said first concentration, of particles having a particle size distribution larger than said first particle distribution; an agglomeration region downstream from said first separating means for agglomerating said fine particles in said gas stream to said large particles; and second separating means through which said gas stream passes and in which said agglomerated particles separate from said gas stream. |
11. | The apparatus of claim 10, wherein said first separating means comprises an electrostatic precipitator. |
12. | The apparatus of claim 11, wherein said second separating means comprises an electrostatic precipitator. |
13. | The apparatus of claim 10, wherein said first separating means comprises a baghouse . |
14. | The apparatus of claim 13, wherein said second separating means comprises a baghouse. |
15. | The apparatus of claim 10, further comprising classifying means in communication with said first and second separating means for classifying the particles separated therefrom according to size. |
16. | A method of removing fine particles having a first particle size distribution from a gas stream having a first concentration of large particles having a second particle size distribution larger than said first particle size distribution, comprising: passing said gas stream through first separating means in order to separate from said gas stream particles having a particle size distribution larger than said first particle size distribution; electrically charging to a first polarity said fine particles having said first particle size distribution and having exited said first separating means in said gas stream without having separated from said gas stream; electrically charging to a polarity opposite said first polarity a plurality of large particles having a particle size distribution larger than said first particle size distribution; causing said fine particles to agglomerate to said charged large particles by introducing to said gas stream having exited said first separating means said plurality of charged large particles so as to increase the concentration of particles in said gas stream having a particle size distribution larger than said first particle size distribution to a concentration higher than said first concentration; and causing the resulting agglomerated particles to separate from said gas stream. |
17. | The method of claim 16, further comprising classifying the separated particles according to size. |
18. | The method of claim 16, wherein said first separating means is an electrostatic precipitator. |
19. | The method of claim 16, wherein said first separating means is a baghouse. |
20. | The method of claim 16, wherein the number of said charged large particles introduced to said gas stream is greater than or equal to the number of said fine particles in said gas stream, multiplied by: the square of the radii of said fine particles divided by the square of the radii of said large particles. |
BACKGROUND OF THE INVENTION
One of the principal means for controlling emission of
small particles from power plant exhausts is electrostatic
precipitation. This is a well-established method, which has
been in use since the early years of this century. However,
the effectiveness of conventional electrostatic precipitation
decreases with a decrease in particle size, and for particles
of lμm diameter and smaller, the effectiveness of conventional
electrostatic precipitation has decreased to the point that it
is not adequate to meet anticipated standards. The range of
particle size (approximately) from .2μ to lμ is a particular
concern because: (1) electrostatic precipitation is not
effective in this range; (2) exhausts from power plants - and
other plants - often have significant emissions in this range;
and (3) particles of this size are not effectively filtered by
the human respiratory system and consequently these particles
- when present as suspensions in the air - pass readily into
the throat and lungs.
Large particles are more easily removed from the air (or
other gases) than small particles. Particles having diameters
of 50μm, or greater, will settle quite rapidly simply under
the action of gravity. In addition, the effectiveness of
electrostatic precipitation decreases for particles of smaller
diameter. These well known facts have stimulated various
proposals to agglomerate particles, and thereby assist in the
removal of particles from the air. Some experiments have been
performed to accomplish agglomeration by acoustic means (see,
for example Report to the EPA, Midwestern Research Institute,
1975, and T. Watanabe, J " . Institute of Electri c Discharge of
Japan, , U 133 (1991) ) , presented a quadrupole field as a
means for assisting the agglomeration of charged particles.
However, most proposals involve bipolar agglomeration, which
was studied by N.A. Fuchs, Zeitschπft fur Physik m 1934.
This subject was taken up again by Eliasson, Egli and Hirth
(B. Eliasson, W. Egli and M. Hirth, Helvetica Phsyikalische
Acta ϋj), 1035 (1986)) and Hughes and Richardson (J.F. Hughes &
R.B. Richardson, Poce . 3rd ICESP, p. 337 (1987)) , beginning in
the late 1980' s.
A fundamental weakness of those bipolar schemes which
simply split the exhaust stream into two equal channels - one
to be charged to one polarity and the other to the opposite -
has been discussed by Eliasson, et al . (B. Eliasson, W. Egli,
J.R. Ferguson and H. Jodeit, Journal Aerosol Sci . , _18_, 869
(1987)) . The problem arises because the exhaust stream,
handled in this way, clearly will yield charged particles
whose size distributions are more or less identical for both
polarities (what has come to be called "symmetrical" bipolar
agglomeration) . In this case, as demonstrated by Eliasson and
co-workers, agglomeration occurs more readily for the largest
charged particles, so the agglomeration process shifts the
particle-size distribution toward finer particles. It is shown
that in this case the concentration of fine particles may be
reduced by only a factor of two or three, even after multiple
stages of the process. To overcome this poor performance of
the "symmetrical" bipolar process, Eliasson and Egli (B.
Eliasson & W. Egli, Journal Aerosol Sex . , 22, 429 (1991))
proposed that the exhaust first be processed in a cyclone type
particle separator, which could be arranged to separate the
particles into two distinct size distributions; one containing
particles which are mainly of diameter less than a certain
value dc, and one containing particles which are mainly of
diameter greater than dc. The two, separated size
distributions would then pass through separate channels in the
precipitator - one stream being charged to one polarity and
the other stream to the opposite polarity. Recombined in an
agglomeration chamber, one should find a process in which
large particles are combining predominantly with smaller
particles. (Eliasson and Egli call this "asymmetric" bipolar
agglomeration.) Koizumi, et al . (Y. Koizumi, et al . , Proc .
ESA-IEJ Joint Sy p . Electrosta tics , p. 66 (1994)) made
calculations based on a computerized model for small-particle
motion in a gas. They modeled both the agglomeration of
uncharged particles by random diffusion and the agglomeration
of a mass of charged particles, half of which were charged to
one polarity and half to the opposite polarity. A homogeneous
inter-mixture of these particles is assumed and the
calculations follow the agglomeration process from this
assumed initial state. Koizumi et al . present calculations of
the "symmetrical" and the "asymmetrical" bipolar processes.
Their work confirms that of Eliasson and co-workers, but shows
significant agglomeration in very short time; that is, times of the order of 0.01 seconds. Koizumi et al . do not present
any experimental results, as was done by Eliasson et al .
Many processes in industrial plants require substantial
input of air. After partaking in the process, the air flow
must be returned to the atmosphere. The quintessential example
of this is the power plant burning fossil fuel. The input air,
having supplied oxygen for combustion, must be returned to the
atmosphere, along with the "products of combustion." The
latter are predominantly C0 2 gas, but particulate matter may be
entrained in the exhaust gas; and especially so if solid fuel
(principally coal) is being burned. Plant exhausts can contain
a very wide spectrum of particle sizes. However, particles of
50μm to lOOμm diameter, and larger, are generally too heavy to
be suspended in the exhaust atmosphere and tend to precipitate
rapidly. This can be enhanced by baffles, filters and circular
flow patterns in the exhaust pipework, or flue. It is
particles of diameter less than 50μ which tend to be carried
into the atmosphere in untreated exhausts; and especially
particles of diameter a few microns - or less - which can
remain suspended indefinitely in gases at normal temperatures
and pressures.
Electrostatic precipitation is a widely used conventional
means of removing small particles from plant exhausts. The
electrostatic precipitation process electrically charges the
particles by exposing them to a stream of ions in the presence
of a substantial electric field - all within the exhaust
stream. The electric field causes ions in the gas to drift
with the field lines, in the course of which they are
intercepted by particles in the gas and in this way the
particles become charged. (This process is called
"Field-charging".) Then, by means of transverse electric
fields, the charged particles are swept across the exhaust
duct and out of the gas stream, where they are captured on
collection plates of the precipitator. The transverse drift or
migration velocity, w, experienced by the particle in the
transverse collecting field, is a parameter of fundamental
importance to the process. Throughout the duct space, between
the collection plates, charged particles drift toward the
plates, each with their particular value of w - depending upon
their charge and their average diameter. The particles have a
distribution in size and they are spatially distributed over
the width of the duct. Particles with higher migration
velocities clearly have a much higher probability of being
collected. For a precipitator operating at given potentials,
it can be shown (see, for example, Section 6.1 in Harry J.
White, Industrial Electrostatic Precipi ta tion, Addison-Wesley,
1963) that, when the field charging process is operative, w is
proportional to the average diameter d of the particle. In
other words, larger particles will have higher drift
velocities, w, and will more likely be collected.
There are two complexities to this situation which should
be mentioned at this point: (1) For particles having d » .2μm,
and less, charging in an electrostatic precipitator (ESP)
occurs primarily by diffusion of ions to the particles, rather
than by directed streams of ions which constitute the
field-charging process. Diffusion charging occurs at a rate
which increases only approximately linearly with the particle
diameter d in contrast to field charging where the rate of
charging is proportional to the square of d. Further, in
diffusion charging, there is no well-defined saturation value
as in field charging. Charging will continue so long as the
particle remains suspended in a gas containing ions. However,
in an actual ESP, charging time is limited by the size of the
precipitator and by the velocity of the exhaust and, in
practice, diffusion charging is significantly less effective
than field charging. (2) Beginning with d < .2μm, the motion
of the particle through the gas becomes less that of a
particle moving through a viscous fluid (as described by
Stokes' Law) and begins to have the aspects of a particle
moving amongst molecules (as described by Kinetic Theory) . The
consequence of this is that for d < .2μm, the migration
velocity w, begins to increase with decreasing d, as shown in
the theoretical curves of Figure 1.
The problem may be summarized by reference to Figure 1.
The effectiveness of conventional electrostatic precipitators
declines with decreasing particle size, reaching a minimum in
the range of particle diameters between .2μm and lμm. In fact,
throughout this range, the migration velocity w is too low to
permit effective particle collection in conventional ESP
equipment, as illustrated in Figure 2. Figure 2 presents the
theoretical collection efficiency as function of the particle
size for three different ratios of collection area versus gas
velocity. Figure 2 clearly shows, that the uncollected or
emitted fraction might be on the order of 30% for fine
particles while under the same conditions less than 0.1% are
uncollected for particles with lOμm diameter.
Increasing the operating electric field, E, or increasing
the size of the precipitator plates and reducing the gas
velocity will permit collection of smaller particles. However,
there exist limitations to all three options. The amplitude of
the electric field is limited by the breakdown strength of the
gas between corona wire and collection plate and cost imposes
boundaries on the size of the collection area and minimum gas
velocity.
What is needed is a new concept which would circumvent
the practical limitations on size and operating voltage in
conventional ESP's. Changing the size distribution of the
entrained particles towards larger particles could constitute
such a new concept .
If very small particles in the exhaust stream could be
caused to agglomerate and thus form larger particles, the
small-particle performance of electrostatic precipitators
could be improved to exactly the extent that agglomeration
could be achieved. Such a concept has been proposed and
experimental and analytical results have been published (N.A.
Fuchs, Zeitschrift fur Physik; B. Eliasson, W. Egli and M.
Hirth, Helvetica Physikalishce Acta jϋ, 1035 (1986) ; J.F.
Hughes & R.B. Richardson, Proc . 3rd ICESP, p. 337 (1987) ; B.
Eliasson, W. Egli, J.R. Ferguson and H. Jodeit, Journal
Aerosol Sci . , 18., 869 (1987) ; B. Eliasson & W. Egli, Journal
Aerosol Sci , 22., 429 (1991) ; T. Watanabe, J. Institute of
Electric Discharge of Japan , J 3, 133 (1991) ; Kanazawa et al . ,
Proc . Inst . of Electrosta tics Japan, 16, 323 (1992) ; Y.
Koizumi et al . , Proc . ESA-IEJ Joint Symp . Electrosta tics , p.66
(1994) ) . Calculations by various of these workers suggest that
agglomeration by simple diffusing together of the smaller
particles would require times of the order of ten seconds to
several minutes, depending on the assumptions made. In any
case, this mechanism is evidently too slow to be applicable in
electrostatic precipitation. The average residence time of an
entrained particle in an electrostatic precipitator is on the order of 2 to 10 seconds.
The agglomeration process could be greatly accelerated if
the small particles to be agglomerated were of oppositely
charged streams of equal particle size distribution (B.
Eliasson, W. Egli and M. Hirth, Helvetica Physikalishce Acta
59. 1035 (1986) ; J.F. Hughes & R.B. Richardson, Proc . 3rd
ICESP, p. 337 (1987) ; B. Eliasson, W. Egli, J.R. Ferguson and
H. Jodeit, Journal Aerosol Sci . , 18, 869 (1987) ; Kanazawa et
al . , Proc . Inst . of Electros tatics Japan , 16., 323 (1992)) . The
conditions for this so-called "symmetric bipolar agglomeration" could be achieved - for example - by dividing
the exhaust stream into two channels, in each of which corona
charging of respectively opposite polarities took place. The
two channels would then merge into an "agglomeration chamber. "
This approach achieves agglomeration in much shorter times
than uncharged agglomeration, but a fundamental difficulty
arises from the fact that the larger particles from the two
streams quickly merge and form inactive, electrically neutral
particles. As a consequence, symmetric bipolar charging
reduces the concentration of the fine particles by only a
factor of two or three, even after a passage through a
multistage, bipolar precipitator (B. Eliasson, W. Egli, J.R.
Ferguson and H. Jodeit, Journal Aerosol Sci . , 18 . , 869 (1987)) .
An alternative method would be to divide the smaller and
larger particles within the flue gas stream into two separate
gas streams, i.e. all particles below a critical diameter dc
would be in one stream and all particles above dc would be m
the other stream. The particles within the two gas streams
would then be charged with opposite polarities and afterwards
allowed to merge and agglomerate. This so-called "asymmetric
bipolar agglomeration" was analyzed by Eliasson and Egli (B
Eliasson & W. Egli, Journal Aerosol Sci , 22, 429 (1991)) for a
typical size distribution of particulates in a flue gas
stream. This distribution is shown m Figure 3.
The results were encouraging if the critical diameter dc
was on the order of lμ and minimum overlap in the two size
distributions existed. For dc larger than 8μm, the asymmetric
bipolar agglomeration was inferior to the symmetrical case.
The shortcomings of the reported asymmetric bipolar
agglomeration were principally due to the fact that the
process was based on the size distribution existing at the
inlet to a typical ESP.
SUMMARY OF THE INVENTION
The method disclosed herein overcomes the limitations of
previous agglomeration schemes by utilizing the following six
features:
1. Introduction of large particles of approximately 10-50μm
in diameter from external sources.
2. Charging these large particles with the opposite polarity
to the charge on the entrained particles.
3. Introducing these large particles at a point in the
precipitator where most of the entrained particles have
already been collected and primarily small particles are left
in the stream.
4. The large particles are charged just prior to their entry
into the ESP where they attract the fine particles already
entrained in the gas stream and form agglomerated particles.
5. The resultant exhaust stream containing the agglomerated
particles would pass through a final stage of conventional ESP
or baghouse .
6. The scavenger particles collected in the hopper of the
outlet section are separated from the fines and prepared for
reuse .
Thus, the present invention relates to an apparatus and
method for agglomerating fine particles in a gas stream.
Larger particles are introduced into the apparatus and
imparted with an electrical charge opposite in polarity to the
charge imparted to the fine particles to be agglomerated. The
difference in charge polarity causes the fine particles to
agglomerate to the larger particles, and the resulting
agglomerated particles are then removed from the gas stream by
precipitation.
BRIEF DESCRIPTION OF THE DRAWINGS
Figure 1 is a graph showing the theoretical migration
velocity as a function of particle diameter for field and
diffusion charging;
Figure 2 is a graph of collection efficiency for various
particle size fractions;
Figure 3 is a graph of density, surface and mass
distribution of fly ash;
Figure 4 is a graph of expected particle size
distribution for three hoppers of an ESP in conventional
operation;
Figure 5 is a block diagram of an agglomeration system in
accordance with the present invention;
Figure 6 is a schematic diagram of an agglomeration
system in accordance with the present invention; and
Figure 7 is a cross-sectional view of means for achieving
a more uniform electric field in accordance with the present
invention.
DETAILED DESCRIPTION OF THE INVENTION
Large charged particles in the gas stream quickly
scavenge smaller particles which had previously been charged
to the opposite polarity by passing the exhaust through the
inlet sections of a conventional ESP. Because of their high
charge and large surface area, a single large scavenging
particle should be capable of accumulating a very large number
of small particles. For example, the saturation charge of a
50μm size particle is 50 = 2,500 times larger than the charge
on a lμm size particle.
The large scavenger particles can be charged positive by
field charging while the input stream can be charged
negatively, as is conventional m ESP' s. This choice
facilitates the adoption of the invention to conventional
wire-plate precipitators.
The method of deliberately introducing large particles to
scavenge the very fine particles is applied at a section of a
conventional precipitator where only a small fraction of the
original dust loading are present and the remaining particles
are predominantly fine particles which the conventional ESP
was unable to collect, as shown in Figure 4. Thus the large
scavenger particles introduced do not become attached to the
relatively large and medium size particles of opposite charge
in the exhaust stream. They remain available to agglomerate
large numbers of fine particles. Introducing the large
scavenger particles at this location keeps the consumption of
the scavenger particles to a minimum.
Assuming, for example, an inlet dust loading of lOgm/N
and that 1% of the inlet loading remains at the point of
scavenger particle injection, one would deal with
approximately lOOmgm/Nm of fine particles. To neutralize this
number of fine particles, - assuming that the scavengers are
solid (not hollow) particles and of the same specific gravity
as the fines - would require a number that is larger by the
ratio of the radii between scavengers and fines. For a ratio
of 50 one would then arrive at a required scavenger mass of
5gm/Nm 3 . If one further uses the approximate relationship that
lMWel corresponds roughly to 1 Nm /sec, one would then arrive
at a scavenger demand of 18kg/(hr,MW) . While this would be a
large amount to bring to the site on a daily basis, it should
certainly be feasible to reuse the scavenger particles which
will have collected primarily in the last hopper. Since the
relative size of the scavengers and fines is so large, it
should be easy to separate the two fractions from the ash.
Using smaller size or hollow scavengers would reduce the
weight, but might make it more difficult to reuse the
scavengers .
Scavenger particles might be obtained from sources
outside the power station, but in many instances it will be
possible to use particles from the fly-ash collected in the
various sections of the ESP. Figure 5 shows a system where
fly-ash particles are collected from the hoppers of section
ESP No. I and ESP No. II and then sorted according to size by
a classifier. The large particles are then utilized as
scavenger particles and the small ones discarded with the ash
flow.
ESP No. I is not necessarily limited to the first ESP
section, but represents a section of the ESP where most of the
particles (and especially the large ones) have been collected
and primarily small ones are left in the stream. Conversely,
ESP No. II can be more than one ESP section. Utilizing
collected fly-ash not only from ESP No. I but also from ESP
No. II allows for a very large variation m particulate
loading.
Scavenging particles also could be made of carbon or
carbon composition. In this embodiment they perform a dual
service. On one hand they attract fine particles and on the
other hand they also absorb mercury or mercuric chloride from
the flue gas stream.
To merge the scavenger particles with the stream of fine
particles, one skilled in the art could utilize various
arrangements. One possible arrangement is shown in Figure 6.
Fines entrained in a gas stream flow through the various
precipitator sections until they arrive at the agglomeration
zone. Large scavenger particles are charged inside the
injector ducts and emerge from the nozzles with a speed
matching the velocity of the stream of fine particles. In the
agglomeration zone the fines attach themselves to the large
scavenger particles and proceed as agglomerated particles
towards the outlet section or sections of the ESP where they
become recharged and collected.
As the rate of agglomeration is directly proportional to
the charge on the small and large particles, a substantial
benefit could be obtained if the particles could be more
highly charged. Consequently, it is of utmost importance to
maximize the electric charge on the fine and scavenger
particles. Maximum electric charge can be obtained by
generating the highest possible electric field over the entire
particle charging region. One possible way to achieve this is
by rendering the electric field as uniform as possible in the
charging zone. This, however, tends to limit generation or
corona current. To overcome this shortcoming, both pulsed and
dc electric fields are applied. Figure 7 shows one possible
geometry in which particle charging is accomplished by causing
the gas stream to pass through a space of concentric-
cylindrical cross-section; this concentric cylindrical space
consists of (a) an outer cylindrical metal wall; (b) an inner
cylindrical wall made of a dielectric material; (c) a
conducting grid, cylindrical in shape and placed
concentrically between the said inner and outer walls. A
voltage consisting of a dc base voltage and superimposed pulse
voltage is applied between the outer conducting wall and the
cylindrical grid lying within said outer wall. The voltage so
applied is of sufficient magnitude to cause electrical corona
in the gas within the outer cylindrical wall. A similar, if
much simpler setup can be utilized in a typical ESP
configuration, where negatively charged discharge wire of
small diameter are located between parallel plates. These
discharge wires are typically very far apart from each other,
thus creating a very non-uniform electrical field around the
wire and within most of the ESP volume. A more uniform field
configuration could be achieved by placing the discharge wires
much closer to each other.
The large particles are charged just prior to their entry
into the agglomeration zone by the above described means. The
fine particles which are already charged by traversing the
preceding electrostatic precipitator sections (s) will also
receive a booster charge just prior to their entry to the
agglomeration region.
The idea of deliberately adding particles to the exhaust
stream, when the objective is to remove particles is contrary
to conventional wisdom. However, (1) the proposed
particle-agglomeration scheme includes the recovery and re-use
of the particles deliberately introduced as scavengers.
Therefore, fresh particles will be added at only a fraction of
the rate at which the scavenger-particles are actually used in
agglomeration with fine particles. (2) The large particles
deliberately introduced in the proposed scheme having in many
instances been obtained from the collected ash and do not
contribute another waste material which must be disposed in
some way.
Next Patent: CHEMICAL FRACTIONATION OF MINERAL PARTICLES BASED ON PARTICLE SIZE