ISIJ Int. 51(8): 1353-1359 (2011)ISIJ International, Vol. 51
(2011), No. 8, pp. 1353–1359
Effect of Coke Diameter and Oxygen Concentration of Blast on Cupola
Operation
Natsuo ISHIWATA, Yuki IWAI, Ryota MURAI, Yoshitaka SAWA and
Michitaka SATO
Ironmaking Research Dept., Steel Research Laboratory, JFE Steel
Corporation. E-mail:
[email protected],
[email protected],
[email protected],
[email protected],
[email protected]
(Received on March 9, 2011; accepted on May 23, 2011)
Because the cupola does not require a reducing agent, CO2
generation can be greatly reduced in com- parison with the blast
furnace process. Moreover, because the latent heat of the cupola
off-gas can be utilized effectively in steel plants by blast
furnace gas recovery equipment, the cupola was introduced in JFE
Steel East Japan Works. In this report, the effects of coke
diameter and oxygen concentration of blast on the reaction rates of
coke combustion, coke gasification and carburization in the cupola
were studied. Operation was simulated from the viewpoints of these
reactions and heat transfer between coke/scrap and shaft gas. In
addition, the changes in the off-gas composition, coke rate, hot
metal composition, were observed in an operating small cupola under
several conditions of coke diameter and oxygen concentra- tion of
blast.
KEY WORDS: cupola; coke rate; oxygen concentrations of blast;
solution loss; carburization; simulation; shaft furnace.
1. Introduction
Reduction of CO2 emissions is the most important pur- pose of iron
making research. Processes, which satisfy both environmental
protection and cost efficiency are also demanded in the steel
industry. Innovative processes such as COURSE50 (CO2 Ultimate
Reduction in Steel making pro- cess by innovative technology for
cool Earth 50) are cur- rently developed.
Utilization of scrap, which already exists in the market, is an
effective measure for reducing CO2. The cupola can produce molten
pig iron from cold iron or steel. In the cupo- la process, scrap,
cast pig iron, and similar materials are used as raw materials, and
foundry coke (large lump/low reactivity coke) is used as the heat
source.1–6) Due to the simplicity of this process, it is used in
small and medium- scale casting shops. Because the cupola does not
require a reducing agent, CO2 generation can be greatly reduced in
comparison with the blast furnace process. Moreover, because the
latent heat of the off-gas can be used effectively, cupolas have
been introduced in integrated steel works.6)
In integrated steel works, a larger-scale cupola is con- structed
to secure a large amount of hot iron. Blast furnace coke
(metallurgical coke), which is smaller in diameter than foundry
coke, and oxygen, which is produced for decarbur- ization of iron,
are also actively utilized in cupola operation.
Therefore, in the present research, the effect of changes in the
coke diameter and the oxygen concentration of blast on cupola
operation was studied, considering the combus- tion and
gasification reactions from the viewpoint of reac- tion rate
theory. Operation was also performed with a high
charging rate of small diameter coke and high oxygen con-
centration. The changes in the off-gas composition, coke rate, hot
metal composition, etc. were observed.
2. Outline of Cupola
2.1. Outline of Cupola Process Figure 1 shows a schematic diagram
of the cupola. Nor-
mally, a cupola has a furnace height of 6–8 m and a furnace
diameter of 2–4 m, and has a production capacity of 500– 2 000 t/d.
Scrap/coke are charged from the furnace top, and the traveling time
in the furnace is 30–40 min. Operation is
Fig. 1. Schematic diagram of cupola (features and main specifica-
tions).
© 2011 ISIJ 1354
ISIJ International, Vol. 51 (2011), No. 8
normally performed with a 1-stage tuyere, but in some rare cases,
secondary combustion (post-combustion) is actively performed using
a multi-stage tuyere system.2) Air is gener- ally supplied as hot
blast with a temperature of around 600°C. Oxygen enrichment is
performed during periods of increased production.1) Raw materials
are charged by a charging tube method, and leakage of CO from the
furnace top is prevented by suction of the off-gas. A siphon method
is employed for continuous tapping of melted iron and slag.
Various types of scrap are used. H2, which is a represen- tative
type of scrap, has a length of 1.2 m or less and thick- ness of 6
mm or less. Pig iron-type raw materials such as cast pig iron are
also used. “Foundry coke” has a diameter approaching 200 mm and low
reactivity. In some cases, blast furnace coke screened to a size of
60 mm or larger is also used.
The general operating parameters of the cupola are shown in Table
1. In comparison with the blast furnace, the tapping temperature is
the same or somewhat higher, and the carbon concentration of the
tapped hot metal is approximately 1% lower. The coke rate (130
kg/t) and slag ratio (approx. 50 kg/t) are both much lower. The
unit values for blast and off- gas are approximately half those of
the blast furnace. The gas utilization ratio is on the order of
40%, and the off-gas temperature is approximately 250°C.
2.2. Reactions in Cupola In the cupola, combustion of coke occurs
directly in front
of the tuyere, and the scrap is melted by heat exchange with the
high temperature gas generated by combustion of the coke. The
important phenomena in the furnace are (1) the coke combustion
reaction, (2) the coke gasification reaction, (3) gas-scrap heat
exchange and (4) the scrap carburizing reaction.
2.2.1. Coke Combustion Reaction The carbon contained in the coke is
oxidized to carbon
dioxide by the oxygen introduced into the furnace from the turyere.
Various mechanisms of coke combustion by oxygen
gas7) have been proposed. However, a reaction rate equation (Eq.
1), which considers boundary film resistance and the chemical
reaction, was used in the present research.
.......................................... (1)
Figures 2 and 3 show the relationship between tempera- ture and
coke diameter and the coke combustion reaction rate obtained from
(Eq. 1). Because the combustion tem- perature of coke normally
reaches a high temperature exceeding 2 000°C, it is considered that
the boundary film resistance, and not the chemical reaction, is the
rate-control- ling process. At a temperature of 1 700°C, the
reaction rate is inversely proportional to the 1.5 power of the
coke diam- eter. Thus, it can be understood that the coke diameter
has a large effect on the reaction rate at this temperature.
2.2.2. Coke Gasification Reaction The gasification reaction of coke
is also called a solution
loss reaction, and occurs after substantially all oxygen has
disappeared. It is known that this gasification reaction is an
endothermic reaction, which removes heat from the hot shaft gas and
the shaft gas volume is increased. Numerous
Table 1. Representative operating conditions.
Productivity 6.9 kg/s
Tap C 3.70%
Blast consumption 565 Nm3/t-pig
O2 consumption 5.5 Nm3/t-pig
Blast temperature 550°C
Gas utilization ratio 41%
Off-gas temperature 250°C
Heat loss 600 MJ/t-pig
Fig. 3. Effect of particle diameter on coke combustion rate.
R Dp k k
ISIJ International, Vol. 51 (2011), No. 8
1355 © 2011 ISIJ
researches on the solution loss reaction of coke in the blast
furnace also exist.8) It is necessary to study the reaction at a
comparatively high temperature. In the present research, boundary
film resistance and the chemical reaction were considered
.......................................... (2)
Figures 4 and 5 show the relationship between tempera- ture and
coke diameter and the coke gasification reaction rate obtained from
(Eq. 2). These results suggest that the gasification reaction rate
is controlled by the reaction rate and boundary film resistance at
around 1 500°C, at which it actually occurs. As the reaction rate
is inversely propor- tional to the 1–1.5 power of the coke
diameter, it can be understood that the coke diameter has a large
effect on the reaction rate.
2.2.3. Gas-scrap Heat Exchange Gas-scrap heat exchange occurs by
counterflow. The
basic equation of convective heat exchange is shown by (Eq. 3).
Thus, an analytical solution can be obtained. β is inverse- ly
proportional to the 1.5 power of the scrap diameter and inversely
proportional to the 0.5 power of the gas flow velocity. The furnace
temperature (distribution) is changed by the function of α and β.
According to this analysis, the furnace temperature distribution is
a function of the heat flux ratio (α) and the heat exchange
coefficient (β ).
.......................................... (3)
Figure 6 shows the relationships amang heat transfer effi- ciency
and the heat flux ratio (α) and heat exchange coeffi- cient (β )
for a system in which heat loss does not occur. Here, heat transfer
efficiency is expressed by (Eq. 4). When calculated using ordinary
values for α and β, the thermal efficiency in normal operation
exceeds 90%. Heat transfer efficiency (scrap heating efficiency)
can be improved by various techniques, such as reducing the scrap
thickness, etc.
................ (4)
An example of the heat flux ratio in an actual cupola is shown in
Table 2. As shown in this table, the heat flux ratio in the cupola
did not exceed 1. To estimate the actual tem-
perature distribution in a cupola, it is also necessary to cor-
rect for heat loss. Here, the corrected heat flux ratio shown in
(Eq. 5) was used for simplicity. The heat loss of this cupola is
400 MJ/t-iron. Because the corrected heat flux ratio becomes 20%
bigger (α ’>1), it is considered that the cupola temperature
curve has a concave shaped bottom.
..................... (5)
2.2.4. Scrap Carburizing Reaction When scrap is carburized, the
melting point of the metal
is reduced. The temperature of the molten metal is increases only
slightly after dripping, because the heat exchange time of the
droplets and gas is reduced. The dripping start tem-
R Dp k DpE k
T P
C G dT
G Dp
pg g
g g= − ⋅
+6 1 2 0 0 6 1 2 1 3( ) ( . . ( ) Pr )/ /ε
μΦ
Fig. 5. Effect of particle diameter on coke gasification
rate.
Fig. 6. Effects of heat flux ratio (α) and heat exchange
coefficient (β ) on heat transfer efficiency (efficiency of heat
transfer to material).
α , = ACpsGs+Q / Ts(0)
ISIJ International, Vol. 51 (2011), No. 8
perature has a large effect on the tapping temperature. Carburizing
reactions comprise solid carburizing and gas
carburizing. Figure 7 shows the change in the CO/CO2 tem- perature
in the cupola. Because the oxygen potential in the cupola is high
in comparison with that in the blast furnace, the carburizing
reaction in the cupola is considered to occur by direct contact
with the coke.9)
Therefore, a simulation of the carburizing reaction of scrap was
attempted. Assuming the shape of the scrap is a round bar with a
diameter of 20 mm, coke was assumed to be in contact with 20% of
the circumference of this shape. It was assumed that ash does not
adhere to the solid-solid contact surface and there is no
resistance to mass transfer. It was also assumed that the carbon is
diffused in a solid state, and after reaching the melting point, it
is transferred by flow at 0.1 m/s. For temperature, the furnace
temperature distribution obtained in a previous simulation
(increase from room temperature to 1 500°C in approximately 30 min)
was assumed.
Figure 8 shows the carbon concentration distribution in the round
bar at each temperature. According to this figure, if the
temperature does not reach at least 1 450°C, carbon is not
transferred to the whole bar. As a result, the scrap does not reach
the melting point, and melting and dripping of molten scrap do not
occur. From this simulation, it was concluded that the molten scrap
is carburized to the saturation carbon concentration. However, in
actual cupolas, carburization is limited to a carbon concentration
of approximately 3.5–4%. Although, this phenomenon is inexplicable,
there is a possi- bility that the carburization reaction is reduced
due to the high oxygen potential in the furnace or/and the presence
of ash on the contact surface, which suppresses
carburization.
2.3. Case Study of 1-Dimensional Simulation Model 2.3.1. Method of
1-Dimensional Simulation Model
In the cupola, the various reaction and heat exchange pro- cesses
must be considered. The simplest 1-dimensional
steady state cupola model was prepared, and the effects of the coke
diameter and oxygen concentration of blast on operation were
studied.
This model was created so as to treat the coke phase, scrap phase,
and gas phase. In heat exchanges between these phases, only
gas-solid transfer was considered, and solid- solid transfer was
ignored. Among the reactions in the fur- nace, the coke combustion
reaction (Eq. 1) and solution loss reaction (Eq. 2) were treated by
reaction rate theory. At this time, the change in coke diameter due
to the reactions was considered. The carburizing region was defined
as from 1 350°C to 1 450°C, and within this region, linear change
of the carbon concentration from 0% to 3.7% was assumed.
Parameters of the following items are determined by fit- ting
simulation results on actual operating data. • Coke shape
coefficient (from data of off-gas analysis) • Heat exchange
coefficient between gas and scrap (from
data of molten iron temperature) • Heat exchange coefficient
between gas and furnace wall
(from actual data for heat loss)
2.3.2. Results of Prediction by Simulation Model (1) Simulation
results of furnace temperature and gas com- position
distribution
Figure 9 shows the simulation results of the furnace tem- perature
and gas composition distribution. It can be under- stood that the
O2 concentration remains up to a fairly high
Table 2. Heat flux ratio in cupola top and bosh.
Unit Top Bosh
CO % 16.6 0
CO2 % 11.5 21.1
H2 % 1.0 0
H2O % 0.4 1.5
N2 % 70.6 77.3
Scrap kg/t 1 000 1 000
Coke kg/t 130 96
Limestone kg/t 20 20
Mass heat capacity of solid kJ/t·K 638 865
Heat flux ratio 0.73 0.93
Fig. 7. CO/CO2 concentration distribution in cupola.
Fig. 8. Results of simulation of carbon concentration in
scrap.
ISIJ International, Vol. 51 (2011), No. 8
1357 © 2011 ISIJ
position in the furnace, and disappears at the highest point of CO2
concentration. This is attributed to the large diameter and low
reactivity of the coke in comparison with the blast furnace.
It can be understood that the CO concentration also rises
simultaneously with the disappearance of O2, becoming constant in
the region higher than approximately 2.5 m, and the solution loss
reaction occurs in this region. The temper- ature of the solution
loss reaction is from 1 500°C to 2 200°C. Thus, this temperature is
higher than that in the blast furnace.
CO gas is not utilized for reduction, as it is in the blast
furnace, because a raw material containing reducible oxy- gen, such
as DRI, is not charged. An off-gas, which contains a large amount
of latent heat is released from this furnace.
Above the solution loss reaction region, around approxi- mately 1.8
m, the temperature of the scrap exceeds 1 450°C, and melting and
dripping occur. Solid scrap does not exist below this level, and
the lower part of the furnace becomes a packed bed consisting of
only coke. Therefore, substan- tially the entire solution loss
reaction occurs in this region. (2) Effect of oxygen concentration
of blast and coke diam- eter on operation
Using this model, the effects of the oxygen concentration of blast
and coke diameter on cupola operation were studied. Here, the blast
rate and oxygen concentration were set so as to obtain a constant
off-gas volume, and the coke rate was adjusted to maintain a
constant hot metal temperature. Two cases were studied, in which
the ratio of small diameter coke was set at 50% or 100%, while
changing the oxygen con- centration of blast in the range from 21%
to 50%.
Figures 10–12 show the oxygen concentration dependen- cy of changes
in the furnace top temperature, coke rate, and CO2/(CO+CO2),
respectively. The furnace top temperature decreases due to the
increasing heat flow ratio, and the solu- tion loss region, where
the temperature is high and only coke, and no scrap exists, also
becomes smaller, thereby increasing CO2/(CO+CO2).
On the other hand, when oxygen concentration is increased to more
than 40%, the solution loss region also
becomes smaller. However, the temperature of the solution loss
region becomes excessively high, and this is considered to cause
activation of the solution loss reaction. As a result, the
CO2/(CO+CO2) deteriorates.
It can also be understood that the gas utilization ratio and coke
rate deteriorates as the coke diameter becomes smaller, because the
solution loss reaction occurs more easily.
Fig. 9. Calculated results of gas composition and temperature dis-
tribution in furnace.
Fig. 10. Effect of oxygen concentration on furnace top tempera-
ture (simulation results).
Fig. 11. Effect of oxygen concentration on coke rate (simulation
results).
Fig. 12. Effect of oxygen concentration on CO2/(CO+CO2) (simu-
lation results).
© 2011 ISIJ 1358
ISIJ International, Vol. 51 (2011), No. 8
3. Actual Cupola Test of Effect of Changes in Coke Diameter and
Oxygen Concentration of Blast
3.1. Test Method Operation using a high ratio of small diameter
coke and
high oxygen concentration of blast was performed in an operating
small-scale cupola. The Table 3 shows the speci- fication of
cupola, which is used for this experiment. The two types of coke
used were large lump coke with a har- monic mean diameter of 192 mm
and small diameter coke with diameter of 57 mm. Operation was
performed with the blending ratio of the small diameter coke
changed in the range from 40% to 100%. As iron sources (cast pig
iron, return scrap, steel scrap, etc.) were used. The blending
ratio of pig iron-type raw materials was 35%. In addition to the
above materials, lime and ferrosilicon were also used. Tables 4–6
show the diameter of the coke, the diameter and composition of the
lime, and the diameter and composition of the ferrosilicon,
respectively. An experiment was also performed with oxygen
concentration increased to a maxi- mum concentration of 36%.
As suggested by the model, in actual operation, there were large
changes in the temperature of the hot metal when operation
conditions were changed. In this experiment, the coke rate and
other operating conditions were adjusted so as to maintain a
virtually constant tapping speed, hot metal temperature, and carbon
concentration of iron. Operation was continued for a sufficiently
long period, which could be regarded as the steady state, and the
average coke rate, fur- nace top gas composition, heat loss, etc.
were observed.
3.2. Effect of Oxygen Concentration of Blast on Cupola
Operation
The relationship of oxygen concentration of blast and heat loss is
shown in Fig. 13. The relationship of oxygen concentration and heat
transfer efficiency is shown Fig. 14. Heat loss decreases and heat
transfer efficiency increases as oxygen concentration increases.
When the oxygen concen- tration is increased, the heat flux ratio
inevitably increases, and the scrap melting position moves to a
lower level in the furnace. Provided an eccentric gas flow
(channeling) or oth- er abnormal phenomenon does not occur, it is
considered that heat transfer efficiency will increase and the
furnace top temperature will decrease.
The relationship between the concentration and gas utili- zation
ratio is shown in Fig. 15. According to the operation- al results,
gas utilization can be improved by increasing the oxygen
concentration of blast. The cause of this phenome- non is
considered to be the same as in simulation results.
According to the operational results, gas utilization can be
improved by increasing the oxygen concentration. The cause of this
phenomenon is considered to be the same as in simulation
results.
3.3. Effect of Coke Diameter on Cupola Operation The relationship
between the small diameter coke blend-
ing ratio and the coke rate is shown in Fig. 16. It can be
understood that the coke rate increases as the amount of small
diameter coke blending is increased. In this operation, the tapping
temperature did not change greatly, and there was virtually no
change in heat loss or heat transfer efficien-
Table 3. The specification of cupola for the experiment.
Furnace diameter 2.1 m
Table 4. Property of BF coke and fondly coke.
Harmonic mean diameter Coke ash
Blast furnace coke particle diameter (small) 57 mm 12%
Foundry coke particle diameter (large) 192 mm 10%
Table 5. Particle diameter and composition of lime.
Diameter (mm) CaO (%) SiO2 (%) Al2O3 (%) MgO(%) Fe2O3 (%)
30–60 55.6 0.16 0.05 0.53 0.05
Table 6. Particle diameter and composition of ferrosilicon.
Diameter (mm) Si (%) Al (%) P (%) S (%) C (%)
30–60 76.4 1.34 0.019 0.0003 0.082
Fig. 13. Effect of oxygen concentration on heat loss.
Fig. 14. Effect of oxygen concentration on heat transfer
efficiency.
ISIJ International, Vol. 51 (2011), No. 8
1359 © 2011 ISIJ
cy. The relationship between the change in the coke rate and the
gas utilization ratio is shown in Fig. 17.
It can be understood that gas utilization ratio decreases in the
case of a high coke rate. It is considered that the use of small
diameter coke, which has a larger specific area, increased the
solution loss reaction. Because this reaction is endothermic, some
other heat source must be supplied and it is considered that this
led to an increase in the coke rate.
4. Conclusions
In order to investigate the effect of coke diameter and oxygen
concentration of blast on cupola operation, a 1- dimensional steady
state cupola model was made. Experi- mental operation was also
performed with a small-scale cupola by varying the small diameter
coke rate and the oxy- gen concentration of blast.
The following conclusions were obtained. (1) Increasing the oxygen
concentration of blast reduces
heat loss and the coke rate and increases thermal efficiency. The
high temperature region in the furnace is reduced due to the
increased heat flux ratio accompanying oxygen con- centration, and
the time available for the solution loss reac- tion is shortened
due to the smaller high temperature region.
(2) Increasing the blending ratio of small diameter coke decreases
the gas utilization ratio and increases the coke rate. These change
are attributed to the increase in solution
loss reaction due to the increased specific area of the coke when
smaller diameter coke is used.
Rb: Combustion reaction rate (kg-coke/m3s) Rs: Gasification
reaction rate (kg-coke/m3s)
Dp: Coke diameter(m) Φ: Shape factor (–) kf: Boundary film
resistance factor (m/s) kc: Combustion reaction factor (m/s) ks:
Gasification reaction factor (m/s) Ef: Effective gasification
reaction coefficient (–)
PCO2: Partial pressure of CO2 (kg/m·s2) PO2: Partial pressure of O2
(kg/m·s2) Qm: Sensible heat of molten iron/slag Qg: Sensible heat
of off-gas A: Area of cross section of cupola (m2)
Cps: Heat capacity of sold matters (kJ/kg·°C) Cpg: Heat capacity of
gases (kJ/kg·°C) Gs: Mass flow of solid matters (kg/m2·s) Gg: Mass
flow of gases (kg/m2·s) Ts: Solid matter temperature (°C) Tg: Gas
temperature (°C) H: Heat transfer coefficient (kJ/s·°C) L: Furnace
hight (m) ε: Porosity ratio (–) μ: Viscosity coefficient
(kg/m·s)
Pr: Prandtl Number (–) Q: Heat loss of cupola (kJ/s) α: Heat flux
ratio (–) β: Heat exchange coefficient(–)
REFERENCES
1) T. Ishino: Cupola, Shinnihoncyuuzoukyoukai, Osaka Japan, (1985),
69.
2) T. Ishino: Cupola, Shinnihoncyuuzoukyoukai, Osaka Japan, (1985),
129.
3) A. Proctor: Foundryman, 91 (1998), 127. 4) S. Matsuba: J. Jpn.
Foundry Eng. Soc., 71 (1999), 548. 5) M. Inadomi and K. Saitou: J.
Jpn. Foundry Eng. Soc., 69 (1997),
1065. 6) C. B. Varnbueler, M. Lemperle and H. J. Rachner: Metal
Plant
Technol. Int., (2005), 30. 7) Y. Iwanaga and K. Takatani: J. Comb.
Soc. Jpn., 68 (1989), 290. 8) I. Muchi and A. Moriyama:
Metallurgical reaction Engineering,
Yokendo, Tokyo, (1972), 232. 9) X. Zhang, R. Takahashi, T.Akiyama
and J. Yagi: Tetsu-to-Hagané,
83 (1997), 299.
Fig. 15. Effect of oxygen concentration on gas utilization
ratio.
Fig. 16. Relationship of BF coke blending ratio and coke
rate.
Fig. 17. Relationship of corrected coke rate and
CO2/(CO+CO2).
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/DAN
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/DEU
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/ESP
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/FRA
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/ITA
<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>
/KOR
<FEFFc7740020c124c815c7440020c0acc6a9d558c5ec0020ace0d488c9c80020c2dcd5d80020c778c1c4c5d00020ac00c7a50020c801d569d55c002000410064006f0062006500200050004400460020bb38c11cb97c0020c791c131d569b2c8b2e4002e0020c774b807ac8c0020c791c131b41c00200050004400460020bb38c11cb2940020004100630072006f0062006100740020bc0f002000410064006f00620065002000520065006100640065007200200035002e00300020c774c0c1c5d0c11c0020c5f40020c2180020c788c2b5b2c8b2e4002e>
/NLD (Gebruik deze instellingen om Adobe PDF-documenten te maken
die zijn geoptimaliseerd voor prepress-afdrukken van hoge
kwaliteit. De gemaakte PDF-documenten kunnen worden geopend met
Acrobat en Adobe Reader 5.0 en hoger.) /NOR
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/PTB
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/SUO
<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>
/SVE
<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>
/ENU (Use these settings to create Adobe PDF documents best suited
for high-quality prepress printing. Created PDF documents can be
opened with Acrobat and Adobe Reader 5.0 and later.) /JPN
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>> /Namespace [ (Adobe) (Common) (1.0) ] /OtherNamespaces [
<< /AsReaderSpreads false /CropImagesToFrames true
/ErrorControl /WarnAndContinue /FlattenerIgnoreSpreadOverrides
false /IncludeGuidesGrids false /IncludeNonPrinting false
/IncludeSlug false /Namespace [ (Adobe) (InDesign) (4.0) ]
/OmitPlacedBitmaps false /OmitPlacedEPS false /OmitPlacedPDF false
/SimulateOverprint /Legacy >> << /AddBleedMarks false
/AddColorBars false /AddCropMarks false /AddPageInfo false
/AddRegMarks false /ConvertColors /ConvertToCMYK
/DestinationProfileName () /DestinationProfileSelector
/DocumentCMYK /Downsample16BitImages true /FlattenerPreset <<
/PresetSelector /MediumResolution >> /FormElements false
/GenerateStructure false /IncludeBookmarks false /IncludeHyperlinks
false /IncludeInteractive false /IncludeLayers false
/IncludeProfiles false /MultimediaHandling /UseObjectSettings
/Namespace [ (Adobe) (CreativeSuite) (2.0) ]
/PDFXOutputIntentProfileSelector /DocumentCMYK /PreserveEditing
true /UntaggedCMYKHandling /LeaveUntagged /UntaggedRGBHandling
/UseDocumentProfile /UseDocumentBleed false >> ] >>
setdistillerparams << /HWResolution [1200 1200] /PageSize
[596.000 795.000] >> setpagedevice