The document discusses bag filters, including: 1. The mechanisms of particle capture in bag filters including impaction, diffusion, electrostatic forces, and cake building. 2. Common cleaning methods for bag filters such as collapse, shaking, reverse air pulse, and reverse air jet. 3. Key factors in bag filter design like temperature limitations, fabric choice, filtration velocity, and sizing considerations.

1. 35
BAG FILTERS
Return To T.O.C
J RUSHWORTH

2. BAG FILTERS
CONTENTS
1. INTRODUCTION
2. THE MECHANXSMOF PARTICLE CAPTURE
3. CLEANING MEITIODS
4. TEMPERATURE LIMITATIONS
5. BAG FILTER SIZING
5.1 Filtration Velocity
5.2 EstimatingDedustingAir Flow Rates
6. CHOICE OF CORRECT FABRIC FOR APPLICATION
7. TROUBLE SHOOTING
8. COMMENTS ON APPLICATION
9. RECENT DEVELOPMENTS
Appendix 1: Hmd Design

3. 1. INTRODUCTION
Fabric filtration has been applied for many years on both industrial and domestic fronts.
In essence, a dust bearing gas is intercepted by a permeable fabric in such a manner
that all the gas passes through the fabric whilst the dust impinges on the fibre of the
fabric and is thereby retained.
As the dust accumulates on the fabric a ‘cake’ is formed, which aids filtration by
improving particle capture and improves the collection efficiency. At the same the,
however, the resistance to gas flow increases and in order to maintain the same gas
flow rate as at start Up the system fan has to work harder.
When the resistance to gas flow reaches an unacceptable level, the fabric has to be
cleaned to dislodge the cake. The pressure drop across the fabric will always be greater
than the initial value, that is with new fabric, because some of the dust particles will
become permanently lodged in the fabric. Provided steady state conditions between the
fabric and the quantity of trapped dust is reached in a reasonably short time the effect
is beneficial, but if the quantity of trapped dust increases after every cleaning cycle,
then ultimately bIinding will occur.
2. THE MECHANISM OF PARTICLE CAPTURE
The filtration process is extremely compkx and invohms a combination of impaction,
diffusion, thermal, molecular and electrostatic forces. Of these, the most important
are:-
q ImRaction - which occurs when a particle, because of its momentum, crosses the
fluid streamlines and strikes a fibre. The larger the particle and the smaller the
fibre, the greater are the chances of impaction by particle inertia.
q Diffusion - which is the primary collection mechanism for particles below 0.5
micron.
q Electrostatic Forces - which affect particles below 0.5 micron.
The early stages of filtration occur with the capture of individual particles by
single fibres as a result of any combination of the above mentioned mechanisms.
The particles which deposit on fibres projecting into the gas stream then act as
additional sites for the capture of further particles and eventually chain like
aggregates r-ult. As the process continues, a complete matrix, or cake, of dust
particles is built up until finally particle capture is effected by true surface
filtration, or sieving, and the function of the fabric, apart from acting as a
support, becomes nominal. Following a cleaning action, further particles in the
gas stream attach themselves to particles which have remained on the fibres and
the cake building process recommences.
1

4. Fibres used in the manufacture of fabrics for filtration are almost exclusively synthetic
and they are either woven or needle felted - see Figure 1. Woven fabrics are smoother
and more easily cleaned than felts and sometimes, at low loads, no cleaning devices are
needed because the fabric is self cleaning. On the other hand they often camot be
cleaned too vigorously because this would break down the entire dust cake and force the
dust between the fibres so that the dust emission would be high. Needle felts are less
permeable than woven fabrics, but they can be operated at considerably higher filtration
velocities. The pores in needle felts are very small compared with woven fabrics, so
dust penetration is low.
Generally, the filter elements, whether of woven or felted fabric, are cylindrical, but
some manufacturers have adopted flat panel, or envelope elements.
3. CLEANING MEITIODS
The removal of the accumulated layer of dust from the filter fabric can be achieved in
many ways including collapse of the filter element, mechanical shaking, reverse air
flow, reverse air pulse and reverse air jet. Any one, or combination of these methods
may be employed but, as a generalisation, the reverse air pulse and reverse air jet are
usually associated only with filters having needle felted elements.
Cleaning by collapse of the fiker element - see Figure 2 is a method used when the
fabric is relatively weak, as is the case with glass fibre, and when cake release is
relatively easy. Stronger fabrics and the necessity for a more vigorous action in order
to dislodge the cake leads to shake cleaning, often with the assistance of a reverse air
flow, see Figure 3.
During the collapse of the filter ekment, or the shake or reverse air period, the gas
flow must be stopped in order to allow the dust cake to fall away from the fabric.
Thus, a filter plant must be made up of a sufficient number of separate compartments,
each containing a group of filter elements, to allow one compartment to be taken out
of service at a time for cleaning. If there are only a few compartments in the filter,
then taking one off stream will markedly increase the flow, and consequently the
pressure drop across the others, and this factor must be taken into account at the design
stage.
With reverse air pulse cleaning, moderately pressurised air from a secondary blower is
introduced into the element, often by means of a traveling nozzle (refer to Figure 4).
The reverse air jet method utilises a high pressure jet of air which is injected into the
element for a time intwwai of about 0.1 second - see Figures 5 and 6. Cake release is
accomplished by a combination of fabric deformation, due to the shock of air blast, and
flow reversal. Both cleaning methods remove the dust with only a brief interruption in
the gas flow and both invariably use needle felt fabrics.
Figure 7 shows the relationship between pressure drop and time both for a sectionalised
continuously rated filter and for a filter of the reverse air puise/jet type.
2

5. 10 TIMES
F PARTICLES
WOVEN CLOTH NEEDLE FELT
CROSS SECTION OF
WOVEN AND FELTED FILTER FABRIC
Fig.
3

6. f
~~ l!= —
AIR/CLEANED
*
*.
‘4 :, . ..
. ;V
).
.’
.;
.. ..*
..
“,.
. .
h.. ...
!
* ..
.. ,.
.-... #
t .. ...
y
,
‘
..-
..
: t
I
~LLAPSING
~! 1
...
FAN
.,. ..
COLLAPSING
.“. . -. :AN DIRTY
..
.. # AIR TO
Ku I %...
-., . +
OTHER
W
‘.
.=*:
J .,
smoNs
!
-. . ,~
.’ ..41
I
. .. . .. . . . s.
DIRTY y....p.
‘1
:,” , :
,., ..<.:. >
~
GAS
DIRTY GAS
OUTLET IO
COLLAPSING
FAN CLOSED FAN OPEN
4 +
COLECTED DUST COLLECTED DUST
FILTERING CLEANING
FABRIC FILTER WITH COLLAPSE BAG CLEANING
Fig. 2
4

7. REVERSE BAG SHAKING REVERSE BAG SHAKING
All? FAN, /DEvlcE-OFF AIR FAN DEVICE -ON
C&EANED
Am
99 -0
GAS 1-
/
REVERSE AIR REVERSE AIR-
.
INLET cLOSED INLET OPEN
CLEANED GAS CLEANED GAS
OUTLET OPEN ,.
$ : ;$ OUTLET CmSED
., + .. .
t. .
. .
. . :..
.
t ? f< I y . t
.. . -.
. q
4 .
.
*.. . 1.
. :.
.. :
.
. - . ,%
.
.
. .“.
. . :4
. -1
~: : ,.
A
.
q .! #
-“ .
,“ < q
---- F .-7 .& : h
..
.-
DIRTY DIRTY AIR TO
~)+ER +
GAS
SECTIONS
COLLECTED DUST COLLECTED OUST
FILTERING CLEANING
FABRIC FILTER WITH
SHAKE AND REVERSE AIR CLEANING
Fig. 3

8. ,REVERSE AIR
FAN
/TRAVELLING
w
AIR TUBE
CLEANED GAS*
DIRTY GAS +
b
FILTER BAG WITH_
DUST LAYER
(RLTER CAK=
1! - FILTER BE BEING
BUILDING UP CLEANED AIRW
BRIEF LYREVERSED
INFLATES BAG &
BAG SUPPORT~ O SLODGES DUST
!-. . ..
COLLECTED DUST
FABRIC FILTER WITH
PULSE AIR CLEANING AND CYLINDRICAL BAGS
F@ 4

9. DIAPHRAGM VALVES
~.H=~ ‘iR
- (Co 100 R S.I.)
JET TUBE
CLEANED GAS ~
DIRTY GAS e
l--
5
INJECTI ?4G
BURST OF
COMPRESSED
AIR INTO
‘FILTER BAG
-
FILTER BAG WITH
DUST LAYER
1- PILOT VALVES
&/OR TIMERS
CFILTER CAKE) FILTER BAG BEING
8UILDING UP CLEANED AIRmW
BRIEFLY REVERSED
INFLATES B=&
DIS~DGES DUST
BAG SUPP9RT—
-—
8
COLLECTED DUST
FABRIC FILER WITH PULSE
J= CLEANING AND CYLINDRICAL BAGS
Fig. 5

10. 01 RT Y ~ CLEANED GAS
pox
F LTER BAG —
--RT —JETTUBE
AIR VALVES &
TIMERS
COUECTED
& DUST
BAG SUP POllT—
f
FILTER BAG WITH “i
DUST
(FILTER
LAYER
CAKE)
,4
1 . . . :. . .. !. ..-... -.-+. : : :..-. l.; ..,....-
BUILDING UP.
J1’
FILTER BAG BEING ,
JET TUBE INJECTING
CLEANED AIRFLOW
BRIEFLY REVERSED ‘..~>
.-.
.. BURST OF COMPRESSED
AIR INTO FILTER BAG
lNFLA~S BAG & -7..:.
:’> ;’
DKLODGES DUST.
* ““””--..-.-”.
/’ ‘.:%-
I ‘
FABRIC FILTER WITH PULSE JET CLEAN!NG AND FLAT BAGS.
Fig.

11. I COMPLETE i
F[LTER [
kLEANING CYCLE 1
I I
I I
PRESSURE
DROP
~3RD. SECTION CLEANEO
I -2ND. SECTION CLEANED
fs7. SECTION CLEANED
TIME
SECTIONALISED CONTINUOUSLY RATED F[LTE R
PRESSURE
DROP
TIME
CONTINUOUSLY RATED FILTER
PRESSURE DROP VARIATION
WITH FILTER CAKE BUILD UP.
Fig. 7
9

12. Temoerature Mmitatiom and cknkal res istance of filter fabrics
Key to ChemicaI Resistance:-
Not very good Good Excellent
Fig. 8
10

13. 4. TEMPEMTURE LIMITATIONS
Two of the most important factors in determining the life and efficiency of a filter are
the choice of the correct type of f ibre and how it is woven into a fabric. These are
normally chosen according to the type of dust to be filtered and the operating
temperature and nature of the gas being treated. The maximum temperatures at which
various filtration materials can be operated continuously are shown in Figure 8.
Minor temperature excursions above these values may be tolerated, but fabric life would
be reduced. Significant increases in temperature above these levels would result in
damage to the filtration material. In the case of glass f ibre, which is generally silicone
treated, this coating decomposes. Once this has happened the fibres rub against one
another during the cleaning cycle and mechanical failure quickly follows. To limit
operating temperatures to safe values, it is sometimes necessary to provide
automatically controlled fresh air inlets or water spray systems.
Conversely, excessively low temperatures can also influence the life of the fabric, since
such conditions are conducive to condensation of acids or alkalis on the fabric.
Condensation can also cause the dust to adhere so strongly to the fabric that the
cleaning device is unable to remove it. This rapidly leads to complete blinding of the
fabric and the necessity for its replacement.
The chemical resistance of various filtration materials is also shown in Figure 8. The
chemical resistances shown are based on dry gas conditions. When water vapour is
present, degradation of susceptible fabrics will be accelerated.
11

14. 5. BAG FILTER SIZING
5.1 Filtration Velocity >* .
?’
This is the velocity of the dust and its carrier gas close to the surface of the filter ,
fabric. It is the value of the gas flow rate divided by the area of filter cloth surface ,
through which it passes.
Filtration velocity, or air to cloth ratio, dictates the size of filtration area necess~
for a particular volume flow rate of gas. The type of fabric and its cleaning mechanism
limits the range of filtration velocities that can be achieved by that particular unit.
Table 1 gives base values of air to cloth ratios for various types of filter for %ormal
“ dusts. These values relate to ordinary types of dust in moderate concentrations for
“normaltf application. These values may be increased by Up to 10% when the dust is
known to be easy to filter. An example of this would be clinker dust which is generally
coarsely sized. These values should be reduced by up to 20% for “difficult!? dusts. Fine
dusts such as coal dust, alkali-enriched flue dust and additives such as silica fume are
examples of difficult dusts.
TABLE 1: Base Values of Air to Cloth Ratio for Various T vtws of Filter Plant
for “Normal” Dus@
Rang e of Base
TvDe of Fabric Filter ; Values of A/C
i.e. Method of Self-Cleaning Protrietarv Examnle metres/minut~
Mechanical shaker visco-Beth; 0.65 to 1.0
Spencer-Halstead
Mechanical shaker with low Visco-Beth; 0.75 to 1.0
pressure reverse air Norblo
Medium pressure reverse air SIM Luhq 1.2
Medium pressure pulsating Luhr 1.8
>
reverse air
High pressure reverse jet
(a) Envelope bags DCE 1.5
(b) Cylindrical bags <3m long Airmasteq MikroPul 1.8
(c) Cylindrical bags >3m long Cibel, AAF, Flakt, Joy,
First :. 3m GBE, etc 1.8*
Next 3m 100*
I
* Value for illustration only; depend heavily upon details of air purge system.
12’”

15. 5.2 Estimating Dedusting Air Flow Rates
The recommended reference on this subject is “Industrial Ventilation” published by the
American Conference of Government Hygienists. Some guideline values are summarised
below;
Belt conveyor transfers: 323 cfin per foot of belt width for belt speeds
< or = 3.3 ft/sec.
Belt wipers: 215 cfin per foot of belt width.
Vibrating screens: 66 cfrn per square foot of screen area.
6. CHOICE OF CORRECT FABRIC FOR APPLICATION
Table 2 indicates what filtration materials have been found to perform best in different
applications within the cement manufacturing process. The base filtration velocities have also
been indicated for each application. Gore-Tex fabrics and their “lookalikes” appear to be able
to operate at high filtration velocities. However the surfaces of these fabrics are very delicate,
and at high gas velocities may be eroded. The fabric property would then revert to that of the
base fabric, a normal needle felted medium. These fabrics do have excellent dust release
properties and should be used where dust release is a problem.
13

16. TABLE 2: The Right Fabric for the Right Dust
(Subject to Temperature Limitations)
“BASE” VALUE OF
DUST/PROCESS FABRIC AIR TO CLOTH RATIO*
(std/min) (R/rein)
Cement transport systems PP; PE 1.5 4.9
Cement raw materials PE; NX 1.5 4.9
Whiting (CaCO~) Dry: PE; moist: DT 1.25 4.1
Kiln BE Dust transport Dry: PP or PE 1.25 4.1
Enriched alkali precip-dust PP; possibly DT; NX 1.25 4.1
Clinker transport PE or NX 1.5 4.9
Clinker cooler waste air NX or other high temp 1.5 4.9
fabric
Clinker cooler waste air with PE or NX as design 1.65 5.4
heat exchanger .—— —
Furnace gases Glass NF; PTFE; Ryton 1.4; 1.5; 1.5? 4.6,4 .9,4.9
Raw meal transport PP; PE 1.4tol.5 4.6 to 4.9
Coal PF or dry raw coal PE; DT; PEAV 600 1.25 4.1
Coal mill (Epitropic or + 5% SS)
Kiln BE gases Woven glass; ?Tefaire 0.65 to 0.9; ? 2.1 to 2.95
NX questionable, has
been used 1.5 4.9
Additives, extenders,
Limestone, Gypsum PP; PE 1.5 4.9
CAF2, SiO~, fime PP; PE 1.25 4.1
Cement/Raw mill 1.0 3.2
High effeciciency separator
filter
Cement/Raw mill vent filters 1.2 3.9
r
* Air to cloth ratio for DCE type filter. Add up to approximately 20% for pulse jet filters with
cylindrical bags < 3m long (see Table 1).
Key: PP = Polypropylene PE = Polyester DT = Dralon T NX = Nomex
PEAV 600 = special fabric, do not speci@ without finther advice
SS = stainless steel fibre NF = Needle felt

17. ‘7. TROUBLESHOOTING
If a filter is consistently failing for whatever reason it is worthwhile obtaining the
original design data and comparing this with the current operating conditions. Several
modifications may have been carried out over the years on the plant being de-dusted
and these could have drastically changed the filter duty.
Increased emission levels are usually caused by broken filter bags. If the increased
emission level has been indicated by a dust monitor and not visually, it would be
worthwhile first checking the emission visually if this is possible. If this is not possible,
the operation of the dust monitor should then be checked. This may require that a dust
emission test be carried out to check the accuracy of the monitor.
In smaller filters broken bags are usuaily located by checking each individual bag. This
would be a very arduous task however on a larger filter. For filters with long
cylindrical bags suspended from a tubesheet, a broken bag can sometimes be detected
by a pile of dust on top of the tube sheet next to the broken bag. It is therefore
important to clean the tubesheet after each maintenance. For older filters with bags
that are not supported by tubesheets the task can be more arduous. It is possible tO
locate the compartment or compartments that have broken bags by selectively isolating
each compartment in turn and noticing the change in dust emission, especially if a dust
monitor has been installed.
Increased dust emissions can also be caused by leaks in the tubesheet or internal
chambers. Unless the crack or hole is relatively large the locations of these leaks are
not always easy to find. Making use of fluorescent powder and a UV lamp can greatly
assist in locating the leaks. A few kilograms of fluorescent powder are introduced in
to the intake of the filter whilst it is in operation. The filter is then run for a few
minutes to allow the powder to work its way through. The filter is then stopped and
inspected internally with a W lamp.
Increased pressure drop across a filter is usually caused by blinded bags. If the pressure
drop suddenly increases or reduces, a similar change on the exhaust fan current drawn
may also be observed. If this is not observed and the dust emission has not increased,
then the pressure tappings should be checked to see if they are blocked. Blinded bags
usually result from problems with the cleaning mechanism. This could result from a loss
in compressed air pressure for pulse-jet filters. For product collecting filters on
cement milIs it is normal to interiock the compressed air supply line pressure to mill
operation. If the air pressure drops the mill is tripped out. Low air pressure apart from
compressor fauits, can be caused by faulty water traps which have resulted in the line
filters blocking. Excessive oil or water entrained in the air is often the cause of failure
of the air management system and is an indication of faulty compressor operation.
Blinded bags can also result from operating below the dew point of the gas resulting
in condensation on the bags, which can render the bag cleaning device ineffective. Poor
gas distribution through a filter can also be detrimental to its operation with high flow
areas causing re-entrain.ment of the dust and excessive pressure loss across the filter.
15

18. Short bag life can be caused by poor gas distribution. Areas with high gas velocities can
result in rapid bag wear due to excessive impingement of dust on the bags. High gas
velocities can cause attrition between individual bags also resulting in wear.
Short bag life can result from incorrect fabric choice for the application; high gas
temperatures and chemical attack are also causes of premature failures.
8. COMMENTS ON APPLICATION
As mentioned above major problems can result if condensation occws leading to blinding
of a fabric. Maintaining gas temperatures below the rating of the filter fabric is also
important to avoid it being overheated. These factors must be borne in mind when
deciding whether or not a fabric filter should be used to de-dust the gases from any
particular process. It is possible, though not necessarily practicable, to alter the
condition of unsuitable gases if the use of a fabric filter is essential.
When the moisture content of the gases is high at relatively IOW temperatures, as is the
case with the exhaust streams from wet and semi-dry process kilns, an electrostatic
precipitator would be the obvious first choice. A fabric filter could be used if
supplementary heaters were installed in order to pre-warm the filter.
In the case of dry process, suspension preheater or precalciner kilns, the waste gases are
naturally dry and at first sight might seem to be suited for a fabric filter. However,
the temperature of these gases is too high for the use of bag fiIters and cooling would
be necessary. This is best carried out by the evaporation of water into the hot gases
in a conditioning tower. The increased moisture content of tie gas makes it more
favorable to use electrostatic precipitation. A further factor to support this arises
when use is made of the waste gases in the milling/drying circuit. Contact with the raw
materials increases its moisture content and reduces the gas temperature.
Electrostatic precipitators are the preferred equipment for dust removal from kiln
waste gases in U.K. and most of Europe. This is not the case in the U.S. A., where
fabric filters on cement kiln exhausts are much more commonplace. The reasons for
this were mainly political when there were serious air quality problems in the Lehigh
Valley region and others. Other possible reasons may be a history in the U.S.A. of badly
designed electrostatic precipitators, which gave rise to the impression that high
efficiency gas cleaning could not be achieved by electrostatic precipitators.
The installation of large fabric filters entail lower capital costs than electrostatic
precipitators (although running costs are higher).
In some cases the chimney, or exhaust stack, can be dispensed with.
The latter point is of particular interest since, for example, in the U.K. the Alkali
Inspectorate demand that the waste gases be exhausted to atmosphere via an exhaust
stack of a defined height. In the U.S.A. louvre openings in the roof of the filter housing
16

19. are currently acceptable. It has been suggested that the louvre discharge system
facilitates the location of a faulty bag, whereas when a chimney iS used the task is more
difficult. This is likely to change as new environmental legislation in the U.S.A.
requires exhaust stacks to be installed on existing and new bag filter installations. This
is to enable the whole exhaust stream to be measured.
A large quantity of water is required to cool the gases from a dI’Yprocess kiln (about
200g of water per kg of clinker) and in some parts of the world such quantities are not
available. Electrostatic precipitation can be extremely difficult k these circumstances
(due to high dust resistivity) and a fabric filter then could be considered. Its size
however would be excessive as the gas would be cooled by ambient air and thus result
in an increase in the quantity of gas to be treated. The filter medium, which is
invariably glass fibre for such applications, demands a low fikration velocity for
satisfactory operation - typically 0.5 -0.6 metres per minute and this also dictates a
large sized filter plant.
The waste air stream from a grate type of clinker cooler is very (h’y and the resistivity
of the dusts is generally high. The gas temperature of this stream is typically about
300*C but this can increase to 500°C during a kiln flush. To enable the use of a filter
fitted with Nomex or polyester needle felt bags a method of cooling the gas is required.
Gas was cooled in the past using water sprays but most modern installations incorporate
an air to air heat exchanger. A cold air bleed may also be incorporated in the circuit
for emergency use during a kiln flush. The coarse nature of the dust permits a filtration
velocity of about 1.5 m/min, thus making the filter relatively compact.
Experience with water spray systems on existing clinker cooler applications has not been
encouraging and where fabric filters have been used, temper~ture control by the
automatic introduction of fresh air has been opted for.
Fabric filters and electrostatic precipitators have both been used to de-dust cement mill
exhaust streams for many years. The trend is towards larger closed circuit milling
operations with separate mill and separator ventilation circuits. Fresh feed to the mill
is partially cooled by the coarse returns from the separator. This together with
improved mill ventilation results in less cooling water being required during the milling
process. Hence most recent cement mill installations have opted for bag filters to de-
dust the mill and separator circuits instead of precipitators.
The fabric filter finds its greatest application, in the cement manufacturing process,
in the removal of dust from ambient air. Examples of these are at conveyor transfer
points, on rail wagon tipplers, de-dusting loading chutes and venting silos. All these
applications can be successfully de-dusted with correctly sized filters. Problems have
been encountered de-dusting clinker conveyors due to the passage into the filter of
glowing particies, which burn the filter elements. A satisfactory solution would seem
17

20. <
FIGURE 9
18

21. to be the installation of an inertial collector before the filter in order to remove the
glowing particles before they enter the filter. Ceramic fibre filters are to be tested
for this application.
9. RECENT DEVELOPMENTS
DCE Ltd and Neu Engineering Limited manufacture a rigid self-supporting element
which can also be retrofitted to an existing Dalamatic type filter or installed in new
filters. An element and the way it is installed in a filter is shown in Figure 9. These
elements are moulded from sintered plastic granules and have a profiled outer surface
which is treated with a permeable coating of PTFE.
The duty of each module is greater than a similar sized fabric filter due to the
increased surface area developed by the profiling. The base filtration velocity for these
elements still remains at 1.5 m/min.
At present the filter medium is limited to a maximum operating temperature of 60°C.
The manufacturers are currentiy looking at methods of raising this operating
temperature.
There is a growing number of areas where sintered ceramic fibre filter elements may
have applications within the cement indus~. These filter elements are suited to very
high temperature applications and therefore do not require protection in the same way
as a bag filter. Their disadvantages are primarily the high cost of the individual
elements, the relatively small dimensions of the individual filter elements and the high
cost of the resulting filter unit. Further developments in this area may change the
economic viability of this type of filter for high temperature applications.

22. Appendmi
3. Hood Design
Once the processes of identification and whence the capture VdOcity is produced, must
quantification have been carried o@ a dust also be taken into consideration.
control engineer may plan his campaign both
from the engineering and economic viewpoint Unfortunatdy d] too often the economic and
engineering irnpo~nce of the available*
Rarely can a particdar dust source be regardi~ the siting of CX&UXX hoods is either
completely eliminated, although the dust ignored or completely misunderstood by-
control engineer and the process engineer of those concerned in the specificationand
should consider whether any change of purchase of dust controI plant The fbllowing
production technique can minim- if not brief excursion intothefieldofhtid~
eliminate, the problem. The reduction of a mayhelpinkktif@g the-m~
particular emission source by either
suppression or containment is, in practice,
Muchoftheavaiktkdata -tothesiting
often possible and usually repays investigation.
ofexhausthoods is based onw*atiti
The next step is to design the exhaust in the 1930’s by DaIlaWk and nearly 50 yeZWS
enclosure. Formulae for hood design do exis4 later by Fletck By measuring contour
although experience counts for a great deal in Velocities in fiontofaninletm formula can
their application. The starting point for a hood bederivedforthe centreiineairflow
design calculation is determining the emission relatbmhip. From these formulae the ~
rate or velocity of the liberated d- From this onthecentre lineinfrontofa hood~
a capture velocity maybe decided upon which expressed asapcmtage of thehoodface
willalso be influenced by the type of dust velocityReference tdg.lo
showsthe
FinaIfy the siting of the capture ~ from terminoiogyused inthevarious formulae
FIGURE 10
Face areaX = W x ‘U Facevekityisthe average
exeftedoverfaceofhood-%
Equivalent
diameter ‘D*
XWXL
J 47
w ~ conveying
velocity
=Q
‘: ..:../ Areaf duct
o
,,. . -
-...
--:-------
q
k
Emission _,; ~u; ;,,.
,. , -
:...
veloc@ source$~..-
y.”..“...... . .....
: ‘:.. ...:
/ . ..:-: “.:”;..’.
“. ...:..
.:<,. lblume Q = q
A x faceVelocii
j. .?.,:
.. .“
-
i
Di&nce from dustsource
capture tohoodface=’X
Veiocityv
‘

23. Appendix z Cont.
The formuia of DallaVaile,(fig. 11), is a relatively an experienced dust contmi engineer can
sirnpie one. Although satisfactory where the make an accurate prediction as to the overall
hood mouth is eitk circuiar or square it coUection efficiency of the ckvice. The closer
should not be used when the hood mouth is the hood is to the dw generation Point the
~guiar and where the aspect radio is any more economical the system is,,and generally
other than one to one. any capture hood that is sited more than 0.7
diameters away from the dust source could be
Cakuiation for the required volume of air regarded as poorly positioned and
for round or square hinds, according to uneconomic. To demonstrate in real terms the
DallaVaile:- inmiicatioriof this factoz the followingexample
(fig.13) shows the difference in air tilumes
Q = V(10X2 + A) required for the same collection problem
Where: for two alternative distices between hood
Q = Quantity of air and dust source.
V = The capture velocity at the dust
The necessary air volume when a hood of
X = The distance from hood mouth to 400mm dia. is placed 320mm from a
dust source dust source where a capture velocity of
A = The open face area of the hood 150m per minute is required is-
Q = V(10X2+ A) - DaUaWle
Fig. 11 Formula of DallaVaIle
q
= 150(10 x 0322+ rr x 022 )
Fletcher’s formula, which is more compiex = 1723m3 per mm.
does however take into regard varying _ Kthesamehoodi snowm_ed
ratios and use of his nomogram, (fig. 12),will 200mm from the dust source and the
give a much more accurate resdtfor anygiven __~@~_~e~
problem. IRAlmebecomes
Howeverthe simpler DaUaVaUe equation can Q=15010x022+rrx O~)
provide the practical engineer with an = 79m!l per *
immediate indication as to the likelyc-
vekityofanexhaust~tiba~n F@.13- CakuMons allowingimportanced
position relativeto the dust SOUME.
F- * ---
LOO~
,
1
0s ~
0.4-
03- -0.!0
A
02- s
P
o.ls- E
c
T
0.10-
0.07-
.
0.06-
O.M “ -0.4
0.03-
-030
O.oa -
Om -
0.015+
0.01“ -1.00
.
.
Oms ~ X = Distance from face of hood to dust source
A= Openareaofhoodface