CA 02531697 1999-12-16
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METHOD FOR DECREASING ELUTRIATION LOSS OF FINE IRON
ORE IN FLUIDIZED BED TYPE REDUCING OPERATION
FIELD OF THE INVENTION
The present invention relates to a method for
decreasing the elutriation loss of a fine iron ore in a
fluidized bed type reducing operation for reducing a fine
iron ore. More specifically, the present invention
relates to a method for decreasing the elutriation loss of
a fine iron ore in a fluidized bed type reducing operation,
in which an additive is fed together with the fine iron
ore, or the fine iron ore is coated with a sludge before
feeding it into a fluidized bed type furnace, thereby
decreasing the elutriation loss of the fine iron ore.
BACKGROUND OF THE INVENTION
Currently, the iron ore deposits show a particle size
of less than 8 mm in 80~ of them, and the iron producing
method using a f luidized bed is calling attention as the
next generation iron producing method. Therefore,
researches and developments are briskly carried out on this
method over the whole world including Europe, America,
Japan and Korea.
Large iron ore particles can be reduced by using the
conventional fixed bed type furnace, but in the case of a
fine iron ore particles, if the gas velocity is low as is
seen in the fixed bed type furnace, then the reducing
operation can be halted due to a sticking phenomenon or the
like. Therefore, there is necessarily adopted the
fluidized bed type furnace in which the ventilation can be
made efficient, and the gas velocity can be made high, so
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as to make the flow of the solid particles smooth.
Meanwhile, the smelting reduction method includes:
a pre-reducing process of reducing the solid iron ore
particles by using CO + Hz (the former being obtained from
the natural gas or from coal); and a smelting reduction
process of melting the pre-reduced iron ore and finally
reducing it.
In the pre-reducing process, an iron ore having a
wide particle size distribution is formed into a sintered
iron ore or a pellet iron ore, and it is used directly
without a pre-treatment like in the conventional blast
furnace. However, the sintering process is very
troublesome, and therefore, the skipping of the sintering
process is demanded.
In this manner, the limitation of the raw material
characteristics can be overcome, and the intermediate step
of agglomerating the fine iron ore as well as the facility
for doing it can be omitted. Thus the fine iron ore can be
directly used, and so, a considerable cost saving will be
realized.
In this fine iron ore reducing method using the
reducing gas, there are required a good permeability and
a uniform temperature distribution within the furnace,
while the contact areas of the particles have to be made
large. For this, the fluidized bed type furnace is a
necessity.
As the typical commercial processes for reducing the
iron ore by using the f luidized bed, there are DIOS of
Japan, and HISMELT and FIOR of Australia.
In the above mentioned processes, however, the
sticking of particles occurs during the reduction, and a
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degradation occurs resulting in that the fine iron ore
particles are flown away, and that the recovery rate-for
the reduced iron is decreased, these being the pending
problems.
An example of the reducing furnace using the fluidized
layer is Japanese Patent Application Laid-open No. Hei-6-
306432. This fluidized bed type furnace is illustrated in
FIG. 1. As shown in FIG. 1, the fluidized bed type
furnace 10 structurally consists of a cylindrical reducing
furnace 11 and cyclones 14 and 15. A reducing gas is
supplied through a gas supplying hole 13 of the bottom of
the cylindrical reducing furnace and through a gas
distributor 16. Meanwhile, a fine iron ore is charged
through a iron ore charging hole 12 into the furnace. Then
the iron ore particles are reacted with the high
temperature reducing gas so as for the iron ore to be
reduced. After elapsing of a certain time period, the
reduced fine iron ore is discharged through an iron ore
discharging hole 17.
However, if the particles are agitated in the
fluidized bed within the reducing furnace, then a
degradation occurs due to the collisions between the
particles and due to the frictions between the particles
and the furnace wall, thereby further making the particles
smaller. As the reaction progresses, the mentioned
phenomenon becomes severer de to the thermal impacts and
the variation of the internal structure.
According to the experiments of Sato et al, when the
fine iron ore particles are reduced at a high temperature
within the fluidized bed, the mentioned powderizing
occurs, leading to the result that the particle diameter
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is decreased to a small fraction of the initial diameter.
In this manner, the fine iron ore particles are increased.
These fine iron ore particles are recycled by a cyclone, or
captured by a dust collecting facility to be circulated
into the fluidized bed type furnace so as to be reduced.
Under this condition, however, the extremely fine
particles cannot be captured by the cyclone, but are flown
away causing a elutriation loss. Currently, in the DIOS
process, the elutriation loss amounts to 10 - 20~, and
therefore, if this process is applied to a commercial
furnace, a considerable problem will be encountered. In
consideration of the productivity in the commercial
reducing furnace, the allowable elutriation loss level is
about 5~.
Meanwhile, if the gas velocity within the furnace is
too high, the fine particle elutriation amount is
increased so as to lower the recovery rate. On the other
hand, if the flow velocity is too slow, then the coarse
particles are segregated to above the gas distributor,
thereby impeding the flow of the reducing gas. This leads
to a non-uniform reduction and a sticking, resulting in
that the reducing operation is halted. This sticking
phenomenon has been a serious problem in reducing the
coarse iron ore particles. In order to overcome this
problem, the iron ore particles are coated with an
additive or carbon, but in this case, an additional
process is required so as to cause a cost increase.
SUMMARY OF THE INVENTION
In order to solve the above described conventional
problems, the present inventors carried out researches and
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experiments, and came to propose the present invention
based on the results of the researches and experiments.
Therefore it is an object of the present invention to
provide a method for decreasing the elutriation loss of a
5 fine iron ore in a fluidized bed type reducing operation,
in which an additive is fed together with the fine iron
ore, or the fine iron ore is coated with sludge before
feeding it into a fluidized bed type furnace, thereby
decreasing the elutriation loss of the fine iron ore.
In achieving the above object, in the method for
decreasing the flight loss of fine iron ore particles in a
fluidized bed type reducing operation by using a fluidized
bed type reducing apparatus including: a fluidized bed
type furnace for receiving a fine iron ore and a reducing
gas (received through its bottom) to form a fluidized bed
so as to reduce the fine iron ore and so as to discharge a
reduced fine iron ore, and so as to discharge a discharge
gas; and a cyclone for capturing the fine iron ore
particles from the discharge gas to discharge the discharge
gas after its separation from the fine iron ore particles,
and to recirculate the fine iron ore particles to the
fluidized bed type furnace after their separation from the
discharge gas,
the method includes the step of: charging 3 - 6 volt
of lime stone ( CaC03 ) or dolomite ( CaC03, MgC03 ) together
with the fine iron ore into the fluidized bed type furnace.
In another aspect of the present invention, in the
method for decreasing a elutriation loss of fine iron ore
particles in a fluidized bed type reducing operation by
using a fluidized bed type reducing apparatus including:
a fluidized bed type furnace for receiving a fine iron ore
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and a reducing gas (received through its bottom) to form a
fluidized bed so as to reduce the fine iron ore and so ws
to discharge a reduced fine iron ore, and so as to
discharge a discharge gas; and a cyclone for capturing the
fine iron ore particles from the discharge gas to discharge
the discharge gas after its separation from the fine iron
ore particles, and to recirculate the fine iron ore
particles to the fluidized bed type furnace after their
separation from the discharge gas,
the method includes the steps of: adding 0.2 - 5.0
wt~ of sludge to the fine iron ore to mix them and to make
the sludge coated on the fine iron ore; drying them at a
temperature of 105 - 800°C for 1 - 24 hours; and charging
the fine iron ore (thus -coated with the sludge) into the
fluidized bed type furnace,
wherein the sludge has a composition composed of: 5-50% of T.Fe, 2-20% of
Si02, 3-30% of CaO, 2-11.5% of AI203, 1-3.5% of MgO, 2-9% of C, 1 % or less
of Ti02, 1 % or less of P205, 1.5% or less of K20, 0.1 % or less of Na20, and
1 % or less of S.
BRIEF DESCRIPTION OF THE DRAWINGS
The above object and other advantages of the present
invention will become more apparent by describing in detail
the preferred embodiment of the present invention with
reference to the attached drawings in which:
FIG. 1 is a schematic elevational view of the
conventional fine iron ore reducing fluidized bed type
furnace;
FIG. 2 is a schematic elevational view of the
experimental fine iron ore reducing fluidized bed type
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furnace according to the present invention;
FIG. 3 is a schematic elevational view of another
embodiment of the experimental fine iron ore reducing
fluidized bed type furnace according to the present
invention; and
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FIG. 4 is a graphical illustration showing the
variation of the elutriation rate with respect to the
addition amount of the additive.
DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS
The present invention provides a method for reducing
a fine iron ore in a fluidized bed type furnace with a
cyclone. In fact, however, the present invention can be
applied to a multi-stage fluidized bed type reducing
apparatus.
In the method for reducing a fine iron ore by using a
fluidized bed type furnace and a cyclone, the fine iron
ore is charged into the fluidized bed type furnace, and a
reducing gas is injected through the bottom of the furnace,
to reduce the fine iron ore while forming a fluidized bed.
Under this condition, fine particles loaded in the
discharge gas move to the cyclone. Then the fine particles
are separated from the discharge gas by the cyclone to be
circulated to the f luidized bed type furnace, while a part
of the fine particles together with large particles are
discharge through a discharging hole to the outside of the
reducing furnace.
In the case where a fine iron ore with a wide particle
size distribution is reduced in the fluidized bed type
furnace, the iron ore is degraded at the initial reaction
stage, and therefore, sometimes, the newly produced fine
particles occupy the greater part. Accordingly, the
circulating fine particles are more and more increased as
the time elapses. Consequently, if the capacity of the
cyclone is smaller than the circulating amount of the fine
particles, then the performance of the cyclone is
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drastically lowered. Further, in this case, the amount
of the elutriation loss becomes greater than the amount of
the fine particles which return to the reducing furnace.
Therefore, the circulating pipe may be clogged, with the
result that the total amount of the circulating fine
particles are discharged to the outside.
This in turn causes a secondary trouble to the
reducing furnace, to the gas purifying facility and to the
water treatment system, thereby leading to the halting of
the reducing operation.
In order to solve the above problems, the present
invention is carried out in such a manner that lime stone
particles or dolomite particles of 0.15 mm as an additive
are charged together with the fine iron ore into the
fluidized bed type furnace, thereby preventing the
elutriation loss of the fine iron ore particles and
preventing the degradation phenomenon.
The present invention will be described in more
details.
That is, the fine additive particles which are
charged together with the fine iron ore particles into the
reducing furnace have a smaller density, and therefore,
all of them depart from the fluidized bed to arrive at the
cyclone together with the fine iron ore particles. Then
the fine additive particles thus arrived at the cyclone
interact with the fine iron ore particles so as for the
fine iron ore particles to be coated with the additive
particles. Consequently, pseudo particle sizes are
increased, and these pseudo particle-sized iron ore
particles are recirculated to the reducing furnace. Thus
by charging the fine additive particles into the fluidized
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bed type furnace, the amount of the fine iron ore
particles which pass through the cyclone is stabilized to
a certain level, thereby maintaining the cyclone at a high
performance.
In the present invention, the charging amount of the
fine additive particles should be preferably limited to 3 -
6~. The reason is as follows. That is, if the charging
amount is less than 3$, then the addition effect is
insufficient, while if it exceeds 6~, then the internal
temperature of the furnace is liable to be lowered due to
the heat absorption decomposition reaction of the additive
with the reducing gas.
The particle size of the additive should be preferably
0.15 mm, and this is because the additive particles at
this particle size can be easily captured by the cyclone.
Meanwhile, after the powderizing of the fine iron ore
particles, the proportion of the particles of 0.1 mm or
less is increased to about 30$, this being the generally
known fact. Under an assumption that this is true, 10 to
20~ of the additive has to be added relative the total
amount of the iron ore particles of 0.1 mm or less. It was
confirmed by the experiments of the present inventors that
this addition range is preferable in view of the decrease
of the flight loss of the fine iron ore particles.
In another embodiment, the present invention provides
the following method. That is, sludge is added to the
fine iron ore in an amount of 0.2 - 5.0~, and a mixing is
carried out to coat the fine iron ore particles with the
sludge. Then a drying is carried~'~out at a temperature of
105 - 800°C for 1 - 24 hours. Thus the fine iron ore
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particles with the sludge coated thereon are charged into
the fluidized bed type furnace, thereby preventing the
elutriation loss of the fine iron ore particles and
preventing the degradation phenomenon.
5 The sludge which is usable in the present invention is
first the melting furnace sludge which is obtained by
water-capturing the dusts of the discharge gas which is
discharged from a melting furnace. Second it is the sludge
which is obtained by water-capturing the dusts of the
10 discharge gas which is discharged from a fluidized bed type
furnace. The typical molten iron manufacturing process
includes the COREX*process and the FINEX process.
The preferable composition of the sludge which is
usable in the present invention includes: 5-50$ of T.Fe,
2-20$ of Si02, 3-30~ of CaO, 2-11.5 of A1Z03,. ~ 1-3.5~ of
MgO, 2-9~ of C, 1~ or less of TiOz, 1$ or less of P205,
1.5~ or less of K20, 0.1~ or less of NazO, and 1$ or less
of S.
Among the above ingredients, CaO, MgO, X1203 and C
prevent the growth of the cellular iron and the consequent
sticking between the particles. Further, Ca0 and Mg0
prevent the elutriation of the fine iron ore particles,
thereby improving the iron recovery rate.
Although CaO, Mg0 and A1203 are effective in preventing
the sticking phenomenon, if their contents are excessive,
then the prestige of the finally reduced iron is lowered,
and therefore, .their contents should be properly adjusted.
Further, C is a strong sticking preventing agent,
and the higher its content, the more effective it is.
Further, it produces a reducing~~~gas (C + COZ - 2C0) to
increase the reducing capability, while it also acts as a
* trademarks
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heat source and as a reducing gas in the melting furnace so
as to make it possible to decrease the use of coal.
Meanwhile, S is an ingredient for prompting the
sticking, and therefore, it should be limited to 1$ or
less.
Meanwhile, the sludge which is coated on the fine
iron ore particles should preferably occupy 0.2 - 5.0 wt~
of the total amount of the fine iron ore particles. If the
amount of the sludge is less than 0.2~, the effect for
preventing the sticking and the degradation becomes
insufficient. On the other hand, if the amount of the
sludge exceeds 5.0~, then the dried sludge is degraded to
be flown to the outside of the reaction vessel, thereby
possibly causing an operation stop or failure.
In the present invention, by using a rotary kiln
device or the like, the above mentioned amount of a sludge
suspension fluid is mixed into a raw fine iron ore. Thus
the fine iron ore particles are coated with the sludge,
and then, a drying is carried out, before charging the
coated fine iron ore particles into the reducing furnace.
In the present invention, the above mentioned drying
is carried out a temperature of 105 - 800°C for 1 - 24
hours.
If the drying temperature is too low and/or if the
drying time is too short, then a sufficient drying cannot
be realized. Therefore, if the coated particles are
charged into the furnace, then the coated particles are
agglomerated, resulting in that the pipes are clogged,
and that the fluidizing of the particles within the
fluidized bed type furnace is not efficient, thereby
possibly leading to an operation stop.
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As described above, by coating the fine iron ore
particles with the sludge, there can be prevented the
degradation of the iron ore particles due to mechanical or
thermal impacts. Further, the sticking which occurs over
the gas distributor can be effectively prevented, and the
productivity loss due to the elutriation loss of the fine
iron ore particles can be drastically decreased. That is,
if the fine iron ore particles are charged into the
fluidized bed type furnace after coating them with the
sludge according to the present invention, then the
powderizing of the iron ore particles and the consequent
elutriation loss and the sticking phenomenon can be
prevented awing to the presence of carbon (C), lime stone
(Cao) and alumina (A1Z03). Further, owing to the
generation of the reducing gas (C + C02-~ 2C0) caused by C,
the reaction of the solid fine iron ore particles is
promoted. Further, C is the heat source, and therefore,
the coal consumption can be decreased, thereby improving
the economy.
Meanwhile, in the present invention, the degradation
at the initial stage of the reduction can be effectively
tackled by charging an additive together with the fine iron
ore, or by charging the coated iron ore particles, into
a first reducing furnace (for example, - a first pre-heating
or pre-reducing furnace in a 3-stage f luidized bed type
reducing apparatus).
Now the present invention will be described more
specifically based on actual examples.
<Example 1>
A reducing apparatus illustrated in FIG. 2 and having
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a size of Table 1 was used to carry out a reduction at
conditions set forth in Tables 1 to 6. In this situation,
the fine iron ore was charged through a hopper 23 into a
fluidized bed type furnace 21, while the additive was
charged through an additive hopper 24 into the fluidized
bed type furnace 21. The additive was charged at the pre-
reducing stage while varying its amount from 1 wt$ to 10
wt~.
Then the pre-reduced iron ore was recharged into the
fine iron ore hopper 23 by utilizing a movable bin 25,
thereby carrying out the final reduction. Referring to
FIG. 2, reference code 22 indicates a cyclone, 28
indicates a gas distributor, and 29 indicates a
circulating pipe.
After carrying out the pre-reduction and the final
reduction in the above described manner, the variation of
the elutriation rate with respect to the addition amount of
the additive was checked, and the checked results are
shown in Table 4 below.
<Table 1> Height and inside diameter of the fluidized bed
type reducing furnace
Diameter of gas distributor: 0.3m
Height of reducing furnace: 6m (above gas distributor)
<Table 2> Composition and size distribution of raw fine
iron ore particles
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10
_
Chemical composition (wt~): T.Fe: 62.17, FeO: 0.51, j
Si02: 5.5, Ti02: 0.11, Mn: 0.05, S: 0.012
P: 0.65, Crystalline water: 2.32
article size distribution (wtg): -0.05 mm: 4.6
0.05-0.15 mm: 5.4, 0.15-0.5 mm: 16.8
0.5-4.75 mm: 59.4, 4.75-8 mm: 13.8
<Table 3> Composition and size distribution of lime stone
Chemical composition (wt~): Si02: 2.27, A1203: 0.58,
CaO: 53.28, MgC:~ 0.71, Zn: 0.12, Na203: 0.01,
Crystalline water: 2.63
article size distribution: -0.05 mm:60, 0.05-0.15 mm:40
<Table 4> Composition and size distribution of dolomite
Chemical composition (wt~): SiOz: 1.20, A1203: 0.34,
CaO: 32.01, MgO: 18.38, FeO: 1.46, K20: 0.048,
NaZO: 0.010, Crystalline water: 3.0
article size distribution: -0.05 mm:47, 0.05-0.15 mm:53
<Table 5> Composition, temperature and pressure of reducing
gas
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1. Gas composition (volt):
Pre-reduction: CO: 40, Hz: 20, COZ: 35, N': 5
Ffinal reduction: CO: 65, H2: ?5, CO,: S, Nz: 5
2. Reaction time:
Pre-heating/pre-reduction: 20 minutes
Final reduction: 30 minutes
3. Temperature: Pre-reduction: 800C
Final reduction: 850C
i
4. Pressure: Pre-reduction: 1.8 Kgf/cm2
Final reduction: 2 .0 Kgf/cmz
<Table 6> Gas velocity within fluidized bed type furnace
s velocity: velocity at gas distributor: 2.0 mm
As shown in figure 4, if the amount o~ the
additive was too small, the elutriation rate was to high.
In the case where the additive addition corresponded to the
range of the present invention, the elutriation rate was
very low. Further, if the additive addition amount was
too large, the elutriation rate was rather high.
Meanwhile, in the case where there was added no additive,
a elutriation loss of about 40$ could be observed.
Meanwhile, The presence and absence of the sticking
before and after the additive addition together with the
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average reduction rate are shown in Table 7 below. As set
forth in Table 7, in the case where no additive was added,
particle agglomerations occurred in 1 hour after start of
the reduction experiment, and therefore, a stable
operation could not be carried out due to the non-uniform
particle fluidizing, and due to a severe variation of the
pressure. On the other hand, in the case where the
additive was added, no particle agglomeration occurred
owing to the smooth fluidizing of the particles, thereby
making it possible to carry out a stable operation.
However, it was seen that in the case where the additive
was added, the average reduction rate was somewhat
lowered. As described above, this can be attributed to
the drop of the temperature by the addition of the
additive.
<Table 7> Presence and absence of sticking before and
after the addition of additive, and variation of average
reduction rate
Additive Sticking Reduction
~ rate ($)
4.5-hr 3-hr Pre- final
1-hr~
I ~ reduction reduction
No I
~
additive - None Yes 24-28 81-87
~ Yes
i
Additive Lime stone None None None 22-26 ~ 78-85
added
I I
Dolomite None None INonei 22-26 ; 77-85
I y
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<Example 2>
The reducing apparatus 30 of FIG. 3 was used, and a
sludge and a raw fine iron ore was mixed together within a
rotary kiln to coat the fine iron ore particles with the
sludge. Then a drying was carried out, and the dried
coated particles were charged through the hopper 33 into
the fluidized bed type furnace 31. Then the charged iron
ore particles were pre-reduced while forming a fluidizing
layer of bubbles and the particles. Under this condition,
the mixed amount, of the sludge was 2.5~ of the total iron
ore, and the drying temperature within the rotary kiln
was 550°C.
The pre-reduced iron ore was recharged into the fine
iron ore hopper 33 by using a movable bin 35, thereby
carrying out a final reduction. The reducing apparatus of
FIG. 3 was basically same as that of FIG. 2, except the
fact that there was used the rotary kiln.
The compositions of the sludge and the fine iron ore
which were used in this example are as shown in Tables 8
and 9 below. Otherwise, the reduction and operating
conditions were same as those of Tables 1, 2, 5 and 6.
<Table 8>
Sludge composition
T.Fe: 25.3, SiOz: 8.7$, CaO: 8.4~, A1203: 5.5~,
I
I~igO: 4.1~, C: 43.2, TiOz: 0.4~, PZOS: 0.3$, KZO: 0.9~,
NazO: 0.5~, 5:0.7, others: 2~ I
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<Table 9>
Chemical composition of raw fine iron ore
~T.Fe: 63.49$, FeO: 0.49$, Si02: 4.32$, TiCZ: 0.112$,
~Mn: 0.05$, P: 0.65$, Crystalline water: 3.96$
After carrying out the experiment with the above
mentioned apparatus and at the above mentioned operating
conditions, the particle size distribution of the
particles which have been captured by the cyclone 32 was
measured, and the results are shown in Table 10 below.
Further, the elutriation losses and the elutriation
rates before and after the sludge coating were measured,
and the measured results are shown in Table ZO below.
Further, before and after the sludge coating,
measurements were carried out on the presence of sticking,
the average reduction rate, and the carbon content of the
finally reduced iron. The results are shown in Table 11
below.
As could be seen in Table Z0, when the elutriation
rate was measured at the cyclone 32, the particle size
range of the particles which had been flown from the
furnace and were detected at the cyclone was 0.005 mm or
less. However, as to the amount of the particles which
had been flown away to the outside, there was shown a
elutriation loss of 40 - 45~ in the case where the sludge
was not mixed. In contrast to this, in the case where the
sludge was mixed, the flight loss was as low as 10 - 15$.
Meanwhile, as shown in Table 11, in the case where
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the sludge was not mixed, particle agglomerations occurred
in 1 hour after the start of the reduction experiment, and
therefore, a stable operation could not be carried out due
to the non-uniform fluidizing bed and due to a severe
variation of the pressure. In contrast to this, in the
case where the sludge was mixed, no particle
agglomerations occurred, and therefore, a stable
operation could be carried out owing to the smooth
fluidizing of the particle fluidizing bed. Accordingly,
the reduction rates at the respective stages were improved
to a significant degree.
After the experiment, the carbon content of the
finally reduced iron was measured, and the results were as
follows. That is, in the case where the sludge was mixed,
the carbon content was increased by 30 - 40 times compared
with the case where the sludge was not mixed. This will
lead to the advantage that the carbon input can be saved
during the charging of the fine iron ore.
<Table 10> Degradation rate and elutriation rate with
respect to particle size distribution before and after
sludge coating
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Particle size Size distri-~ Size distri-, Size distri-
bution of ore b~,:tion with bution with
no sludge sludge after
5 after experimt experiment
(accumu wt$) (accumu wt$) (accumu wt$)
0.005 mm or lessi4.6 6.9 6.0
0.15 mm or less 10.0 ~ 51.6 41.3
f
10 0.6 mm or less ~ 26.8 85.6 69.8
4.75 mm or less 86.2 95.6 91.8
8 mm or less i00 ~ 100 100
I
Elutriation loss ~ 40 - 45 10 - 15
15
<Table 11> Occurrence of stickir_g, average reduction rate
and variation of carbon content before and after the sludge
coating
Sticking Reduction Carbon
rate
($) content
within
Pre- Final reduced
0.5-hr 1-hr 3-hr reduction reduction iron
With no
sludge None Yes Yes ~ 24-28 81-87 0.1-0.4
i
With sludge
fixed None None None 30-35 92-96 ~ 3-6
i I
According to the present invention as described above,
an additive is fed together with the fine iron ore, or the
fine iron ore is coated with a sludge before feeding it
into a fluidized bed type furnace, thereby decreasing the
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elutriation loss of the fine iron ore. In this manner,
the degradation and sticking of the iron ore particles are
prevented, and the elutriation loss of the fine iron ore
particles is decreased.
