The present invention relates to a molten iron manufacturing method
and a molten iron manufacturing apparatus, and more particularly, to a molten
iron manufacturing method and a molten iron manufacturing apparatus capable
of increasing reducing power of a reducing gas and decreasing coal
consumption by improving a discharge gas reforming circulating device of a
fluidized-bed reduction reactor.
【Background Art】
In a smelting reduction process, a fluidized-bed reduction reactor for
reducing iron ore and a melter-gasifier for melting iron ore are employed.
When the iron ore is melted by the melter-gasifier, coal briquettes obtained by
agglomerating coal as a heat source for melting the iron ore are charged to the
melter-gasifier. Herein, reduced iron is melted in the melter-gasifier, and then
is converted into molten iron and slag to be discharged to the outside.
A discharge gas discharged from the fluidized-bed reduction reactor is
cooled by passing through a water collector. Some of the discharge gas is
branched and compressed by using a discharge gas reforming circulating
device, and carbon dioxide is removed therefrom. Then, the discharge gas is
mixed with a reducing gas discharged from the melter-gasifier, and the mixed
3
reducing gas is additionally supplied to the fluidized-bed reduction reactor.
Accordingly, reduction efficiency of the iron ore in the fluidized-bed reduction
reactor is improved. However, since a large amount of nitrogen is included in
the additionally supplied reducing gas, there is a limit in improving the reducing
power of the reducing gas.
【DISCLOSURE】
【Technical Problem】
The present invention has been made in an effort to provide a molten
iron manufacturing method having advantages of being capable of improving
reducing power of reduced iron in a reduction reactor by generating a reformed
gas with a hydrocarbon gas. The present invention has also been made in an
effort to provide a molten iron manufacturing apparatus having advantages of
being capable of improving reducing power of reduced iron in a reduction
reactor by generating a reformed gas with a hydrocarbon gas.
【Technical Solution】
An exemplary embodiment of the present invention provides an molten
iron manufacturing method including: i) supplying a discharge gas from a
reduction reactor that converts iron ore to reduced iron; ii) supplying a mixed
gas that is obtained by mixing some branched discharge gas and a
hydrocarbon gas; iii) supplying a reformed gas by reforming the mixed gas; and
iv) injecting a reducing gas, discharged from a melter-gasifier connected with
the reduction reactor to receive the reduced iron, and the reformed gas, into the
4
reduction reactor, wherein the supplying of the reformed gas includes supplying
some of the reduced iron as a reforming reaction catalyst, and reforming the
mixed gas by using the reforming reaction catalyst.
The reduced iron may be directly supplied from the reduction reactor in
the supplying of the reduced iron as the reforming reaction catalyst. The
molten iron manufacturing method may further include agglomerating the
reduced iron by compressing it, and the reduced iron may be agglomerated and
supplied in the supplying of the reduced iron as the reforming reaction catalyst.
The molten iron manufacturing method may further include recovering the
reduced iron used as the reforming reaction catalyst and supplying it to the
melter-gasifier.
The reformed gas may be generated in at least one reformer to which
the reduced iron in the supplying of the reformed gas is charged, and nitrogen
may be supplied to the reformer. The mixed gas may be annularly rotated in
the reformer and injected in a circumferential direction. The reformed gas may
be generated in a plurality of reformers to which the reduced iron is charged to
be used as the reforming reaction catalyst in the supplying of the reformed gas,
and the reformers may include a first reformer and a second reformer. The
reduced iron may be charged into the second reformer after charging of the
reduced iron into the first reformer is completed. When a differential pressure
of the first reformer is equal to or higher than a predetermined value, an inflow
of the mixed gas into the first reformer may be blocked, and a reformed gas
may be generated in the second reformer by supplying the mixed gas to the
second reformer. When a differential pressure of the first reformer is equal to
5
or higher than a predetermined value, the reformed gas may be externally
outputted. After the reformed gas of the first reformer is discharged, the first
reformer may be purged, the reforming reaction catalyst included in the first
reformer may be discharged, and the reduced iron may be supplied to the first
reformer. In the supplying of the reformed gas, the reduced iron may be
continuously charged to and discharged from the reformer that generates the
reformed gas.
The supplying of the reformed gas may include: i) providing a plurality of
reduced iron charging hoppers connected to the reformer in front thereof and a
plurality of reduced iron discharging hoppers connected to the reformer in back
thereof; ii) adjusting a differential pressure between the reduced iron charging
hoppers; iii) charging the reduced iron to the reformer through the reduced iron
charging hoppers; iv) adjusting a differential pressure between the reduced iron
discharging hoppers; and v) discharging said some reduced iron from the
reformer through the reduced iron discharging hoppers.
The molten iron manufacturing method may further include: performing
primary heating on the mixed gas by allowing it to indirectly contact the
discharge gas; and performing secondary heating on the mixed gas by using
oxygen. The discharge gas may be cooled and cleaned in the supplying of the
discharge gas. The mixed gas may be heated to 1000 °C or less in the
performing of the primary heating on the mixed gas. The mixed gas may be
heated in a range of 1100 °C to 1200 °C in the performing of the secondary
heating on the mixed gas. The reduction reactor may include a packed-bed
reduction reactor or a plurality of fluidized-bed reduction reactors in the
6
supplying of the discharge gas. When the reduction reactor includes the
fluidized-bed reduction reactors, a mixture obtained by mixing the reducing gas
and the reformed gas may be supplied to each of the fluidized-bed reduction
reactors.
An exemplary embodiment of the present invention provides an molten
iron manufacturing apparatus including: i) a reduction reactor configured to
reduce iron ore into reduced iron; ii) a melter-gasifier connected with the
reduction reactor to manufacture molten iron by receiving the reduced iron and
to supply a reducing gas to the reduction reactor; iii) a discharge gas pipe
connected with the reduction reactor to pass a discharge gas discharged from
the reduction reactor therethrough; iv) a discharge gas branch pipe connected
with the discharge gas pipe to pass another discharge gas that is branched
from the discharge gas, and to receive a hydrocarbon gas and supply a mixed
gas obtained by mixing the hydrocarbon gas with the discharge gas; v) at least
one reformer connected with the reduction reactor to receive some of the
reduced iron, and connected with the discharge gas branch pipe to supply a
reformed gas by reforming the mixed gas by said some reduced iron; vi) a
supply gas pipe configured to supply the reducing gas to the melter-gasifier by
connecting the reduction reactor with the melter-gasifier; and vii) a reformed gas
pipe configured to connect the reformer with the supply gas pipe, and to supply
a mixture obtained by mixing the reformed gas with the reducing gas to the
melter-gasifier.
The molten iron manufacturing apparatus may further include a heat
exchanger connected with the discharge gas pipe and the discharge gas branch
7
pipe, to heat the mixed gas by the discharge gas. The molten iron
manufacturing apparatus may further include a compacted iron manufacturing
device connected with the reduction reactor and the melter-gasifier, to supply
compacted iron obtained by agglomerating the reduced iron to the meltergasifier,
and connected with the reformer to supply said some reduced iron as
the compacted iron.
The molten iron manufacturing apparatus may further include: a
compacted iron supplying pipe configured to connect the compacted iron
manufacturing device with the reformer, and to supply the compacted iron to the
reformer; and
a compacted iron returning pipe configured to connect the compacted
iron manufacturing device with the reformer, and to return other compacted iron
that has completely been used to the compacted iron manufacturing device.
The molten iron manufacturing apparatus may further include: a first heater
connected with the heat exchanger and the discharge gas pipe to heat the
mixed gas by receiving and combusting the discharge gas; and a second heater
connected with the first heater to re-heat the mixed gas by receiving oxygen.
The reformer may include a plurality of reformers including a reforming
reaction catalyst, and the reformers may include a first reformer and a second
reformer. The molten iron manufacturing apparatus may further include: i) a
mixed gas supplying pipe configured to connect the heat exchanger with the
first reformer and the second reformer; ii) a purge gas supplying pipe connected
to the first reformer and the second reformer; and iii) a discharge gas pipe
connected to the first reformer and the second reformer. The molten iron
8
manufacturing apparatus may further include: i) a pressure gauge mounted in
each of the first reformer and the second reformer to measure each internal
pressure of the first reformer and the second reformer; ii) a differential pressure
gauge mounted in each of the first reformer and the second reformer to
measure a difference between pressures of upper portions of the first reformer
and the second reformer and an internal pressure of the mixed gas supplying
pipe by connecting the upper portions thereof with the mixed gas supplying
pipe; and iii) a level meter mounted in each of the first reformer and the second
reformer to measure a height of the reforming reaction catalyst.
The molten iron manufacturing apparatus may further include: i) a
plurality of reduced iron charging hoppers disposed in front of the reformer and
connected in series with the reformer; and ii) a plurality of reduced iron
discharging hoppers disposed in back of the reformer and connected in series
with the reformer. The molten iron manufacturing apparatus may further
include an inert gas injecting pipe mounted in at least one of the reduced iron
charging hoppers and the reduced iron discharging hoppers to pressurize an
inside of the hopper by injecting an inert gas into the hopper.
The reformer may include an annular mixed gas supplier to surround a
center of the reformer, a plurality of openings may be separately formed at a
predetermined interval in the mixed gas supplier, and the mixed gas may be
injected into the reformer through the openings. The reduction reactor
includes a packed-bed reduction reactor or a plurality of fluidized-bed reduction
reactors. When the reduction reactor includes the fluidized-bed reduction
reactors, the supply gas pipe may be configured to connect each of the
9
fluidized-bed reduction reactors with the melter-gasifier.
【Advantageous Effects】
It is possible to reduce coal consumption by using a molten iron
manufacturing apparatus. Further, since a reducing gas is additionally
supplied to a fluidized-bed reduction reactor by reforming a hydrocarbon gas, it
is possible to efficiently prevent nitrogen integration in the reducing gas. As a
result, it is possible to improve reduction operation efficiency of iron ore of the
fluidized-bed reduction reactor. In addition, in the molten iron manufacturing
apparatus, iron-manufacturing coal and the hydrocarbon gas are used together
to additionally provide a means for economically producing molten iron by using
a hydrocarbon gas, and thus it is possible to more flexibly select a molten iron
manufacturing process depending on a fuel condition and a raw material
condition for each region in the world.
【Description of the Drawings】
FIG. 1 schematically illustrates a molten iron manufacturing apparatus
according to a first exemplary embodiment of the present invention.
FIG. 2 schematically illustrates a reformer included in the molten iron
manufacturing apparatus shown in FIG. 1.
FIG. 3 is a cross-sectional view schematically illustrating an inside of a
reformer taken along a line III-III of FIG. 2.
FIG. 4 is a graph illustrating a conversion rate of hydrocarbon to a
reducing gas according to passage of a contact time with reduced iron.
FIG. 5 schematically illustrates a modification of the reformer included in
the molten iron manufacturing apparatus shown in FIG. 1.
10
FIG. 6 schematically illustrates a molten iron manufacturing apparatus
according to a second exemplary embodiment of the present invention.
FIG. 7 schematically illustrates a molten iron manufacturing apparatus
according to a third exemplary embodiment of the present invention.
【Mode for Invention】
The terminologies used herein are used just to illustrate a specific
exemplary embodiment, but are not intended to limit the present invention. It
must be noted that, as used in the specification and the appended claims, the
singular forms used herein include plural forms unless the context clearly
dictates the contrary. It will be further understood that the term "comprises" or
"includes", used in this specification, specifies stated properties, regions,
integers, steps, operations, elements, and/or components, but does not
preclude the presence or addition of other properties, regions, integers, steps,
operations, elements, components, and/or groups.
Spatially relative terms such as "below" and "above" and the like may be
used herein for ease of description to describe one element or feature's
relationship to another element(s) or feature(s) as illustrated in the figures. It
will be understood that spatially relative terms are intended to encompass
different orientations of the device in use or operation in addition to the
orientation depicted in the drawings. For example, if the device in the figures
is turned over, elements described as "below" other elements or features would
then be oriented "above" the other elements or features. Thus, the exemplary
term "below" can encompass both an orientation of above and below.
Apparatuses may be otherwise rotated 90 degrees or by other angles, and the
11
spatially relative descriptors used herein are then interpreted accordingly.
Unless otherwise defined, all terms (including technical and scientific
terms) used herein have the same meaning as commonly understood by one of
ordinary skill in the art to which this invention belongs. It will be further
understood that terms, such as those defined in commonly used dictionaries,
should be interpreted as having a meaning that is consistent with their meaning
in the context of the relevant art, and will not be interpreted in an idealized or
overly formal sense unless expressly so defined herein.
A term "carbonaceous material" used hereinafter indicates a material
containing carbon. Accordingly, examples of the carbon material may include
all materials containing carbon, such as coal, coke, and carbon dust.
A "hydrocarbon gas" used hereinafter indicates all gases containing a
hydrocarbon. Accordingly, the hydrocarbon gas may be a gas exclusively
formed of a hydrocarbon or may be a gas containing a hydrocarbon.
The present invention will be described more fully hereinafter with
reference to the accompanying drawings, in which exemplary embodiments of
the invention are shown. As those skilled in the art would realize, the
described embodiments may be modified in various different ways, all without
departing from the spirit or scope of the present invention.
FIG. 1 schematically illustrates a molten iron manufacturing apparatus
100 according to a first exemplary embodiment of the present invention. The
molten iron manufacturing apparatus 100 shown in FIG. 1 is merely an example
for describing the present invention, and the present invention is not limited
thereto. Accordingly, the molten iron manufacturing apparatus 100 may be
12
modified to another form.
As shown in FIG. 1, the molten iron manufacturing apparatus 100
includes a fluidized-bed reduction reactor 10, a compacted iron manufacturing
device 20, a melter-gasifier 30, a reformer 40, a heat exchanger 50, and
heaters 60 and 62. If necessary, the molten iron manufacturing apparatus 100
may further include other devices. Detailed internal structures of such devices
can be easily understood by those skilled in the art to which the present
invention pertains, and a detailed description thereof will be omitted.
Molten iron is manufactured in the melter-gasifier 30. Oxygen is
injected through a tuyere 301 of the melter-gasifier 30, and coal and reduced
iron are charged through an upper portion of the melter-gasifier 30. The coal
forms a coal-packed bed in the melter-gasifier 30. Coal briquettes, a lump
carbonaceous material, or the like may be employed as the coal, and lump coal
may be employed as the lump carbonaceous material.
Coal charged to the melter-gasifier 30 is combusted by using oxygen
injected though the tuyere 301. Thus-generated combustion heat is used for
manufacturing molten iron. Further, a high-temperature reducing gas such as
CO or H2 is supplied to a dome-like portion of the melter-gasifier 30 by passing
through the packed bed formed in the melter-gasifier 30. The hightemperature
reducing gas is discharged from the melter-gasifier 30 and passes
through a dust circulation device 32. The dust circulation device 32 separates
a large amount of carbon-containing dust included in the high-temperature
reducing gas from other materials, and re-injects the separated carboncontaining
dust to the melter-gasifier 30. The reducing gas from which the
13
carbon-containing dust is removed is supplied to the fluidized-bed reduction
reactor 10.
Meanwhile, a water collector 36 branches some of the gas separated
from the carbon-containing dust in the dust circulation device 32 to cool and
clean the branched gas. Further, a gas-circulating cooler 37 additionally
cleans some of the gas which is cooled and dust-removed in the water collector
36. A temperature of the reducing gas supplied to the fluidized-bed reduction
reactor 10 is controlled by heating the gas and circulating it as the reducing gas
supplied from the melter-gasifier 30. In addition, an excess gas discharging
device 38 additionally dust-removes some of the gas which is cooled and dustremoved
in the water collector 36, and discharges it depending on a pressure of
the melter-gasifier 30 in order to adjust an internal pressure of the meltergasifier
30.
Iron ore is reduced in the fluidized-bed reduction reactor 10. The
fluidized-bed reduction reactor 10 is formed to include a plurality of stages,
which are sequentially connected to reduce fine ore to reduced iron. A
bubbling fluidized bed is formed in each stage of the fluidized-bed reduction
reactor 10. Accordingly, in the fluidized-bed reduction reactor 10, reduced iron
may be manufactured by fluidizing and reducing fine ore. Meanwhile, a submaterial
may be further mixed to prevent the fine ore from adhering to an inside
of the fluidized-bed reduction reactor 10.
The compacted iron manufacturing device 20 includes a reduced iron
storage tank 201, a pair of rolls 203, a disintegrator 205, and a distributing chute
207. In addition, the compacted iron manufacturing device 20 may further
14
include other components if necessary. The reduced iron storage tank 201
temporally stores the reduced iron supplied from the fluidized-bed reduction
reactor 10. Compacted iron is prepared by receiving reduced iron from a pair
of rolls 203 and compressing it in order to prevent scattering and acquire air
permeability at the melter-gasifier 30. The disintegrator 205 disintegrates the
compressed compacted iron to a predetermined size. The distributing chute
207 appropriately distributes the compacted iron to a plurality of compacted iron
storage tanks (not illustrated).
A high-temperature equalizing & relief system 34 is disposed between
the compacted iron manufacturing device 20 and the melter-gasifier 30. The
high-temperature equalizing & relief system 34 is mounted over the meltergasifier
30 in order to adjust a pressure. An internal pressure of the meltergasifier
30 is high, and thus the high temperature equalizing & relief system 34
can readily charge the compacted iron to the melter-gasifier 30 by uniformly
adjusting the pressure. As a result, when the compacted iron is supplied to the
melter-gasifier 30, a supply pressure thereof is appropriately adjusted while
passing through the high temperature equalizing & relief system 34.
A supply gas pipe 70 supplies a reducing gas discharged from the coalpacked
bed of the melter-gasifier 30 to the fluidized-bed reduction reactor 10.
As a result, iron ore can be converted into reduced iron in the fluidized-bed
reduction reactor 10 by a supply gas supplied through the supply gas pipe 70.
As shown in FIG. 1, a discharge gas discharged from the fluidized-bed
reduction reactor 10 passes through the heat exchanger 50, which has an
exhaust heat recovery function for recovering a sensible heat of the discharge
15
gas. A dry dust collector 80 is disposed in back of the heat exchanger 50 to
separate and remove dust included in the discharge gas. Further, a water
cooling device 82 is disposed in back of the dry dust collector 80 to cool the
discharge gas.
A discharge gas branch pipe 92 is disposed in back of the water cooling
device 82 to branch and transport some of the discharge gas. A compressor
84 compresses the branched discharge gas. A hydrocarbon gas supplying
pipe 86 is connected to the discharge gas branch pipe 92 in back of the
compressor 84 in order to supply a mixed gas obtained by mixing hydrocarbon
gas into the discharge gas. The mixed gas is heated while passing through
the heat exchanger 50, and is supplied to a first heater 60 through a gas pipe
94. Meanwhile, the gas pipe 94 is branched from a discharge gas pipe 90 and
is connected to the first heater 60 to heat the mixed gas by supplying the
discharge gas as a fuel. Further, air is supplied to the first heater 60 for
combustion. Herein, the first heater 60 may adjust a temperature of the mixed
gas to 1000 °C or less. If the temperature of the mixed gas is too high, e.g., is
higher than 1000 °C, a heating tube formed of a heat-resisting metal included in
the first heater 60 may be damaged. Accordingly, it is required to adjust the
temperature of the mixed gas to 1000 °C or less.
A second heater 62 is disposed in back of the first heater 60. The
second heater 62 partially combusts the mixed gas heated by the first heater 60
by injecting oxygen thereinto. As a result, the mixed gas is secondarily heated
in a temperature range of 1100 °C to 1200 °C. If the secondary heating
temperature is too high, compacted iron contacting the mixed gas may be
16
adhered to an inside of the reformer 40. If the secondary heating temperature
is too low, there is no sense for the secondary heating. Accordingly, it is
required to adjust the secondary heating temperature of the mixed gas in the
aforementioned range.
The mixed gas that is additionally heated by the first heater 60 and the
second heater 62 is supplied to the reformer 40 through a mixed gas pipe 93
connected to the reformer 40. The reformer 40 receives the high-temperature
mixed gas and reforms components of CO2 and H2O included in the
hydrocarbon and the discharge gas included in the mixed gas into components
of the reducing gas. The reformed gas treated by the reformer 40 is mixed
with a coal-based reducing gas generated in the melter-gasifier 30 to be
supplied to the fluidized-bed reduction reactor 10 through the gas pipe 94 which
is connected to the dust circulating device 32 in back thereof.
Meanwhile, the reformer 40 is connected with the compacted iron
manufacturing device 20 through a compacted iron supplying pipe 22 and a
compacted iron returning pipe 24. The compacted iron supplying pipe 22
supplies the compacted iron manufactured in the compacted iron manufacturing
device 20 to the reformer 40. The compacted iron returning pipe 24 returns
other compacted iron that has been completely used as a reforming reaction
catalyst in the reformer 40 to supply it to the compacted iron manufacturing
device 20 and the melter-gasifier 30. Although not shown in FIG. 1, some of
the reduced iron discharged from the fluidized-bed reduction reactor 10 may be
directly supplied to the reformer 40. In this case, since a particle size of some
reduced iron is small, surface areas thereof are increased. Accordingly, it is
17
possible to improve efficiency in which the reduced iron is used as a reforming
reaction catalyst. Hereinafter, an operating process of the molten iron
manufacturing apparatus 100 shown in FIG. 1 will be described in further detail.
The operating process of the molten iron manufacturing apparatus 100 is
merely an example of the present invention, and the present invention is not
limited thereto.
First, a high-temperature discharge gas discharged after iron ore is
reduced in the fluidized-bed reduction reactor 10 passes through the heat
exchanger 50, and dust included in the discharge gas is separated and
removed in the dry dust collector 80. Thereafter, the discharge gas is cooled
to room temperature in the water cooling device 82. Some of the discharge
gas of the reactor 10 that is dust-removed and cooled is branched and is
pressurized by the compressor 84 to be mixed with the hydrocarbon gas. As a
result, some discharged gas is supplied as a mixed gas. The mixed gas is
heated by contacting the discharge gas in the heat exchanger 50, and is
introduced into the first heating furnace 60 to be primarily heated by indirectly
contacting a high temperature gas by combusting the discharge gas of the
reactor 10 that is dust-removed and cooled. The mixed gas is secondarily
heated in the second heating furnace 62. In the second heating furnace 62,
the mixed gas is heated by directly injecting oxygen into the mixed gas and
combusting it. As a result, a temperature of the mixed gas is controlled
depending on a reaction heat for converting the mixed gas into a reducing gas
and a sensible heat required for acquiring a temperature of the converted
reducing gas, in the reformer 40. In the reformer 40, the mixed gas heated in
18
the second heater 62 is converted into the reducing gas such as CO or H2 by a
chemical reaction represented by Chemical Formula 1.
[Chemical Formula 1]
CH4 + CO2 → CO + 2H2
CH4 + H2O → 2CO + 3H2
The reduced iron is employed as a catalyst for catalyzing the
aforementioned reaction in order to increase a speed of the reforming reaction
and a reaction amount. The compacted iron manufacturing device 20 is
connected to the reformer 40 to supply compacted iron serving as reduced iron
to the reformer 40, and receives the completely used reduced iron from the
reformer 40. Specifically, the compacted iron manufacturing device 20 is
connected with the reformer 40 through the compacted iron supplying pipe 22
and the compacted iron returning pipe 24. A reformed gas generated by the
reduced iron in the reformer 40 is transported through the gas pipe 94, which is
connected to the supply gas pipe 70 through which the reducing gas discharged
from the melter-gasifier 30 is supplied to the fluidized-bed reduction reactor 20.
FIG. 2 schematically illustrates a reformer 40 included in the molten iron
manufacturing apparatus 100 shown in FIG. 1. A structure of the reformer 40
shown in FIG. 2 is an example for describing the present invention, and the
present invention is not limited thereto. Accordingly, the reformer 40 may have
another structure. For example, the reformer 40 may be mounted to have a
plurality of units.
The reformer 40 includes a first reformer 401 and a second reformer
403. The first reformer 401 and the second reformer 403 have the same
19
structures. Accordingly, one of the first reformer 401 and the second reformer
403 may be employed, and the other one may remain as backup. When one
of the reformers is being repaired or fails, the other reformer may be used. As
described above, a plurality of valves are closed or opened in order to
alternately employ the first reformer 401 and the second reformer 403.
The compacted iron supplying pipe 22 is connected to a distributing
chute 23 disposed over the reformer 40 to supply reduced iron through the
distributing chute 23. The reduced iron is selectively supplied to one of the first
reformer 401 and the second reformer 403 through the distributing chute 23.
The reduced iron supplied to the first reformer 401 or the second reformer 403
serves as a reforming reaction catalyst, and a reformed gas obtained by
reforming a mixed gas supplied through the mixed gas pipe 93 can be supplied
through the reformed gas pipe 94. Meanwhile, the reduced iron that has been
completely used as the reforming reaction catalyst is returned to the compacted
iron manufacturing device 20 through the compacted iron returning pipe 24.
Although not shown in FIG. 2, the compacted iron completely used may be fed
to the outside of the first reformer 401 and the second reformer 403 by using a
screw feeder device or the like.
Meanwhile, when valves 231 and 233 are closed, the first reformer 401
and the second reformer 403 are sealed without gas leakage therefrom. The
valves 231 and 233 are opened and closed to supply reduced iron to the first
reformer 401 or the second reformer 403. Further, when valves 241 and 243
are closed, the first reformer 401 and the second reformer 403 are sealed
without gas leakage therefrom. The valves 241 and 243 are opened and
20
closed to control an amount of the reduced iron discharged from the first
reformer 401 and the second reformer 403 through the compacted iron
returning pipe 24.
The mixed gas is selectively supplied to the first reformer 401 or the
second reformer 403 through the mixed gas pipe 93. Values 931 and 933 are
used to selectively supply the mixed gas to the first reformer 401 or the second
reformer 403
The mixed gas is converted into a reformed gas in the first reformer 401
or the second reformer 403, and is discharged to the outside through the gas
pipe 94. Valves 941 and 943 are respectively mounted in the gas pipe 94 in
back directions of the first reformer 401 and the second reformer 403 to control
an amount of the reformed gas discharged to the outside.
Further, if necessary, discharge gas pipes 47 and 48 are respectively
mounted in the first reformer 401 and the second reformer 403 to discharge an
internal gas, and valves 471 and 481 are respectively mounted in the discharge
gas pipe 47 and 48. Meanwhile, nitrogen supplying pipes 405 and 407 are
respectively mounted in the first reformer 401 and the second reformer 403 to
supply nitrogen when the first reformer 401 or the second reformer 403 is
purged.
Pressure gauges 41 and 42 are respectively mounted in the first
reformer 401 and the second reformer 403 to measure internal pressures of the
first reformer 401 and the second reformer 403. Internal states of the first
reformer 401 and the second reformer 403 may be monitored by measuring the
internal pressures of the first reformer 401 and the second reformer 403.
21
Differential pressure gauges 43 and 44 are respectively mounted in the first
reformer 401 and the second reformer 403 to measure a differential pressure by
gas flows generated in the first reformer 401 and the second reformer 403. It
is possible to recognize whether the reduced iron is appropriately operated as
the reforming reaction catalyst by measuring ventilation resistance of the
reduced iron from the differential pressure. Meanwhile, level meters 45 and 46
are respectively mounted in the first reformer 401 and the second reformer 403
to measure heights of reduced iron formed in the first reformer 401 and the
second reformer 403.
FIG. 3 is a cross-sectional view schematically illustrating an internal
cross-sectional structure of a reformer 403 taken along a line III-III of FIG. 2.
The internal cross-sectional structure of the reformer 403 shown in FIG. 3 is
merely an example for describing the present invention, and the present
invention is not limited thereto. Accordingly, the reformer 403 may have
another internal cross-sectional structure.
As shown in FIG. 3, a plurality of openings 4035 are separately formed
at a predetermined interval in a circumferential direction in a mixed gas supplier
4033 of the reformer 403 to be connected with an inside thereof. Accordingly,
as indicated by arrows, a mixed gas flows into the reformer 403 through a pair
of mixed gas inlets 4031 and is rotated along the annular mixed gas supplier
4033. The mixed gas inlets 4031 are formed to face each other. The mixed
gas is annularly rotated toward a reformer center 403c through the openings to
be injected into the reformer 403 in the circumferential direction. As a result, it
is possible to efficiently reform a mixed gas by using a reforming reaction
22
catalyst.
Hereinafter, the operating process of the reformer 40 (see FIG. 1) will be
described in further detail with reference to FIG. 2 and FIG. 3. This operating
process of the reformer 40 is merely an example for describing the present
invention, and the present invention is not limited thereto. Accordingly, the
reformer 40 may be operated according to another operating process.
When the distributing chute 23 (see FIG. 2) selects a charging direction
of the reduced iron supplied from the compacted iron manufacturing device 20
(see FIG. 2) as a direction of the first reformer 401 (see FIG. 2), the valve 231
(see FIG. 2) is opened to charge the reduced iron into the first reformer 401
through the compacted iron supplying pipe 22. When the level meter 45
senses that the height of a packed bed formed by the reduced iron in the first
reformer 401 reaches a predetermined value, the distributing chute 23 changes
the charging direction of the reduced iron to a direction of the second reformer
403 (see FIG. 2)
Accordingly, the valve 231 is closed, and the valve 233 (see FIG. 2) is
opened to charge the reduced iron into the second reformer 403. Further,
when the level meter 46 (see FIG. 2) senses that the height of a packed bed
formed by the reduced iron in the second reformer 403 reaches a
predetermined value, the valve 233 (see FIG. 2) is closed, and the charging of
the reduced iron through the compacted iron supplying pipe 22 is stopped.
Next, the valve 931 (see FIG. 2) is opened to introduce a mixed gas
passing through the mixed gas pipe 93 (see FIG. 2) into the first reformer 401
through the mixed gas inlet 4031 (see FIG. 3). When it is sensed by the
23
pressure gauge 41 (see FIG. 2) that a pressure of the first reformer 401 is equal
to or greater than a predetermined value, the valve 941 is opened to discharge
the reformed gas through the gas pipe 94. The reformed gas that is uniformly
supplied into the first reformer 401 is catalyzed by the action of the catalyst of
the reduced iron in the first reformer 401 to contain a large amount of CO and
H2 by Chemical Formula 1. Meanwhile, in the first reformer 401, as a chemical
reaction of Chemical Formula 1 is performed, the reduced iron serving as the
compacted iron may be abraded or a carbon component may be precipitated by
a chemical reaction of Chemical Formula 2.
[Chemical Formula 2]
CH4 → C + 2H2
2CO → C + CO2
Accordingly, porosity of a reduced iron packed bed formed in the first
reformer 401 may be deteriorated to non-uniformly form a gas flow in the first
reformer 401. As a result, this may deteriorate a reaction rate of Chemical
Formula 1. This situation may be sensed by the differential pressure gauge 43.
When a differential pressure measured by the differential pressure gauge 43 is
equal to or higher than a predetermined value, the valves 931 and 941 (see FIG.
2) may be closed to block supply of the mixed gas to the mixed gas to the first
reformer 401, and the valve 933 may be opened to supply the mixed gas to the
second reformer 403. DeletedTexts As a result, the operation of the first
reformer 401 may be identically realized in the second reformer 403.
Meanwhile, the valves 931 and 941 are closed, and then the valve 471
(see FIG. 2) of the discharge gas pipe 47 (see FIG. 2) is opened to discharge
24
the internal gas of the first reformer 401 to the outside. When it is determined
by the pressure gauge 41 that the internal pressure of the first reformer 401 is
lower than the predetermined value by the gas discharge, nitrogen is injected
into the first reformer 401 through the nitrogen supplying pipe 405 (see FIG. 2)
to purge the remaining mixed gas. After nitrogen is injected for a
predetermined time and the purging is completed, the valve 241 of the first
reformer 401 is opened to discharge the reduced iron included in the first
reformer 401. The discharged reduced iron is recovered by the compacted
iron returning pipe 24 and is charged to the melter-gasifier 30 together with the
compacted iron manufactured in the compacted iron manufacturing device 10.
Further, when it is determined by the level meter 45 that all of the reduced iron
is discharged from the first reformer 401, the supply of nitrogen is stopped and
the reduced iron is re-charged to the first reformer 401.
Meanwhile, when the differential pressure sensed by the differential
pressure gauge 44 (see FIG. 2) is equal to or higher than the predetermined
value in the second reformer 403, the valves 933 and 943 (see FIG. 2) are
closed to block the supply of the mixed gas supplied to the second reformer 403,
and the valve 931 is opened to supply the mixed gas to the first reformer 401.
As a result, the reformed gas may be manufactured in the first reformer 401,
and the completely used compacted iron may be discharged from the second
reformer 403.
As described above, it is possible to switch and operate the first
reformer 401 and the second reformer 403 included in the reformer 40. As a
result, the process of converting the mixed gas to the reformed gas may be
25
performed by using the reduced iron to perform the reaction of Chemical
Formula 1 under a good catalyst condition.
FIG. 4 is a graph illustrating a conversion rate of hydrocarbon to a
reducing gas according to the elapse of a contact time with reduced iron.
As shown in FIG. 4, as a contact time during which hydrocarbon
contacts reduced iron passes, the hydrocarbon is converted into a reducing gas
by Chemical Formula 1. Herein, when the contact time reaches a
predetermined time, an amount of a carbon component generated by Chemical
Formula 2 and the like exceeds a predetermined level. Accordingly, converting
efficiency of hydrocarbon by Chemical Formula 1 deteriorates by 70 % or less.
Thus, as in the reformer 40 (see FIG. 2), the reduced iron included in the
reformer 40 may be substituted with new reduced iron in order to re-increase
the converting efficiency of the hydrocarbon.
FIG. 5 schematically illustrates a modification of the reformer 40
included in the molten iron manufacturing apparatus 100 shown in FIG. 1. The
reformer 49 shown in FIG. 5 is merely an example for describing the present
invention, and the present invention is not limited thereto. Accordingly, the
reformer 49 may have another structure. Further, the structure of the reformer
49 shown in FIG. 5 is similar to that of the reformer 40 shown in FIG. 2, so like
portions use like reference numerals and a detailed description thereof will be
omitted.
As shown in FIG. 5, in the reformer 49, reduced iron may be charged to
an upper side thereof in a gravitational direction and is discharged to a lower
side thereof, and a mixed gas may be reformed in a counter-current direction in
26
which it is supplied to the reformer 49 in an opposite direction to the
gravitational direction. Herein, the compacted iron supplying pipe 22, reduced
iron charging hoppers 491 and 493 connected in series to pass the reduced iron
therethrough, and valves 4910 and 4911 are disposed in front of the reformer
49 to be connected thereto. Herein, the valve 4910 is disposed between the
reduced iron charging hoppers 491 and 493 to adjust a differential pressure
between the reduced iron charging hoppers 491 and 493, and the valve 4911 is
disposed between the reduced iron charging hopper 493 and the reformer 49.
The reduced iron charging hopper 491 receives reduced iron from the
compacted iron supplying pipe 225 in order to charge the reduced iron to the
reformer 49 which is maintained to be higher than atmospheric pressure.
Further, the reduced iron charging hopper 493 uniformly adjusts a pressure
between the reduced iron charging hopper 491 and the reformer 49 to smoothly
charge the compacted iron to the reformer 49. The valves 4910 and 4911 may
be gas-sealed to efficiently charge the reduced iron to the reformer 49. Further,
upper level meters 4926 and 4928 and lower level meters 4927 and 4929 are
respectively mounted to the reduced iron charging hoppers 491 and 493 to
measure levels of the reduced iron stacked in the reduced iron charging
hoppers 491 and 493. In addition, a level meter 45 is mounted in the reformer
49 to continuously measure a height of the reduced iron stacked therein.
Meanwhile, the compacted iron returning pipe 24, reduced iron
discharging hoppers 495 and 497 to pass and discharge the reduced iron
therethrough, and valves 4917 and 4918 are disposed in back of the reformer
49 to be connected thereto. Herein, the valve 4917 is disposed between the
27
reformer 49 and the reduced iron charging hopper 495, and the valve 4918 is
disposed between the reduced iron charging hoppers 495 and 497 to adjust a
differential pressure between the reduced iron charging hoppers 495 and 497.
The reduced iron discharging hopper 495 discharges the reduced iron from the
reformer 49 which is maintained to be higher than atmospheric pressure to the
atmosphere. To that end, the reduced iron discharging hopper 497 uniformly
adjusts a pressure between the reformer 49 and the reduced iron discharging
hopper 495 to smoothly discharge the reduced iron from the reformer 49. The
valves 4917 and 4918 may be gas-sealed to efficiently discharge the reduced
iron from the reformer 49. Further, an upper level meter 4930 and a lower
level meter 4931 are mounted to the reduced iron discharging hopper 495, and
an upper level meter 4932 is mounted to the reduced iron discharging hopper
497. Accordingly, heights of the reduced iron stacked in the reduced iron
discharging hoppers 495 and 497 are measured.
A back-pressure line 4912, a pressurization line 4914, valves 4913 and
4915, a differential pressure gauge 4925 are mounted in the reduced iron
charging hopper 493. The back-pressure line 4912 discharges an internal gas
of the reduced iron charging hopper 493 by controlling the valve 4913 in order
to reduce a pressure of the reduced iron charging hopper 493. The
pressurization line 4914 injects an inert gas such as nitrogen into the reduced
iron charging hopper 493 while using the valve 4915 to pressurize it. Further,
a pressure difference with the reformer 49 is measured by using the differential
pressure gauge 125. A back-pressure line 4919, a pressurization line 4921,
valves 4920 and 4922, and a differential pressure gauge 4940 are mounted in
28
the reduced iron discharging hopper 495 to have the same functions. In
addition, an equalizing line 4950 and a valve 4951 are mounted between the
reduced iron discharging hopper 495 and the reformer 49. A gas analyzer
4941 is mounted in the reformed gas pipe 94 to monitor a composition of the
reformed gas discharged from the reformer 49.
Hereinafter, an operating process of the reformer 49 shown in FIG. 5 will
be described in further detail. This operating process is merely an example for
describing the present invention, and the present invention is not limited thereto.
Accordingly, the reformer 49 may be operated according to another process.
First, reduced iron transported through the compacted iron supplying
pipe 22 is charged into the reduced iron charging hopper 491. When it is
monitored by the upper level meter 4926 that the reduced iron is stacked up to
a portion of the upper level meter 4926 of the reduced iron charging hopper 491,
the supply of the reduced iron through the compacted iron supplying pipe 22 is
stopped. When it is monitored by the upper level meter 4926 that the stacked
height of the reduced iron is reduced below the portion of the lower level meter
4927, i.e., the reduced iron charging hopper 491 becomes empty, the reduced
iron is re-supplied through the compacted iron supplying pipe 22. When it is
monitored that the reduced iron is stacked up to the portion of the upper level
meter 4926, the supply of the reduced iron is stopped.
Further, when it is monitored by the lower level meter 4927 that the
reduced iron is stacked up to a portion of the lower level meter 4927, the valve
4913 is opened to perform a back pressure increase of the reduced iron
charging hopper 493 through the back-pressure line 4912. When it is
29
determined by the pressure gauge 4925 that an internal pressure of the
reduced iron charging hopper 493 reaches atmospheric pressure, the valve
4910 is opened to start to charge the reduced iron from the reduced iron
charging hopper 491 to the reduced iron charging hopper 493. Then, when it
is determined that the reduced iron is filled in the reduced iron charging hopper
493 through the upper level meter 4928, the valve 4910 is closed to stop the
charge of the reduced iron, and the value 4913 is closed.
Next, the valve 4915 is opened to pressurize the reduced iron charging
hopper 493 by injecting the inert gas into the reduced iron charging hopper 493
through the pressurization line 4914. Further, when the internal pressure of
the reduced iron charging hopper 493 measured by the pressure gauge 4925 is
the same as the pressure of the reformer 49, the valve 4915 is closed to stop
the pressurization of the reduced iron charging hopper 493. Then, the valve
4911 is opened to charge the reduced iron from the reduced iron charging
hopper 493 to the reformer 49. Meanwhile, when it is sensed by the lower
level meter 4929 that the reduced iron charging hopper 493 is empty, the valve
4911 is closed. This charging process is repeatedly performed until it is
sensed by the level meter 45 that the reduced iron is filled in the reformer 49 to
have a height that is equal to or higher than a predetermined level.
When the compacted iron is filled in the reformer 49, a valve 935 is
opened to supply the mixed gas to the reformer 49 through the mixed gas pipe
93 to reform it. A reformed gas generated in the reformer 49 is discharged to
the outside through the reformed gas pipe 94 by opening the valve 941.
Meanwhile, the reduced iron is discharged to the low side of the
30
reformer 49 and is re-charged to the reformer 49 at a predetermined time
interval in order to prevent deterioration of the reforming reaction efficiency
caused by Chemical Formula 2 and the like. The reduced iron is discharged
from the reformer 49 through a following process.
First, the valve 4922 is opened to inject an inert gas into the reduced
iron discharging hopper 495 through the pressurization line 4921. When an
internal pressure of the reduced iron discharging hopper 495 measured by
using the pressure gauge 4940 is the same as a sum of pressures of the
pressure gauge 41 of the reformer 49 and the differential pressure gauge 43,
the valve 4922 is closed to stop the injection of the inert gas. Then, the valve
4917 is opened to transport the completely used reduced iron from the reformer
49 to the reduced iron discharging hopper 495. In this case, while the reduced
iron is charged from the reformer 49 to the discharging hopper 495 by opening
the valve 4951, an equal pressure is maintained between the reduced iron
discharging hopper 495 and the reformer 49, thereby smoothly discharging the
reduced iron. Meanwhile, when it is determined by the upper level meter 4940
that the reduced iron is filled in the reduced iron discharging hopper 495, the
valve 4917 is closed to stop the charge of the reduced iron, and the valve 4951
is closed.
Next, the valve 4920 is opened to back-pressurize the reduced iron
discharging hopper 495 through the back-pressure line 4919. Then, when it is
determined by the pressure gauge 4940 that an internal pressure of the
reduced iron discharging hopper 495 is back-pressurized to a normal pressure
and when it is determined by the level meter 4932 that the height of the reduced
31
iron included in the reduced iron discharging hopper 497 is reduced to be lower
than the portion of the level meter 4932, the valve 4918 is opened to discharge
the reduced iron to the reduced iron discharging hopper 497. As described
above, some of the reduced iron included in the reformer 49 is discharged and
new reduced iron is supplied to the reformer 49 at a predetermined time interval.
Accordingly, the mixed gas is always converted into the reformed gas under a
good catalyst reaction condition by a packed bed formed of good quality
reduced iron.
FIG. 6 schematically illustrates a molten iron manufacturing apparatus
200 according to a second exemplary embodiment of the present invention.
The molten iron manufacturing apparatus 200 shown in FIG. 6 is merely an
example for describing the present invention, and the present invention is not
limited thereto. Accordingly, the molten iron manufacturing apparatus 200 may
have another form. Meanwhile, a structure of the molten iron manufacturing
apparatus 200 shown in FIG. 6 is similar to that of the molten iron
manufacturing apparatus 100 shown in FIG. 1, so like portions use like
reference numerals and a detailed description thereof will be omitted.
As shown in FIG. 6, a mixture of the reducing gases discharged from the
melter-gasifier 30 and the reformed gas discharged from the reformer 40 is
additionally supplied to each of a plurality of fluidized-bed reduction reactors 10.
In other words, the fluidized-bed reduction reactors 10 have different functions
for converting iron ore into reduced iron depending on a plurality of steps such
as pre-heating, heating, and final heating. Accordingly, in more detail, it is
possible to improve the functions of the fluidized-bed reduction reactors 10 at
32
each of the steps by mixing the reducing gas discharged from the meltergasifier
30 and the reformed gas discharged from the reformer 40 and supplying
a mixture to each of the fluidized-bed reduction reactors 10.
FIG. 7 schematically illustrates a molten iron manufacturing apparatus
300 according to a third exemplary embodiment of the present invention. The
molten iron manufacturing apparatus 300 shown in FIG. 7 is merely an example
for describing the present invention, and the present invention is not limited
thereto. Accordingly, the molten iron manufacturing apparatus 300 may have
another form. A structure of the molten iron manufacturing apparatus 300
shown in FIG. 7 is similar to that of the molten iron manufacturing apparatus
100 shown in FIG. 1, so like portions use like reference numerals and a detailed
description thereof will be omitted.
As shown in FIG. 7, a packed-bed reduction reactor 12 may be
employed as a reduction reactor. Specifically, molten iron can be
manufactured in the melter-gasifier 30 by using a packed bed which is formed
by charging iron ore to the packed-bed reduction reactor 12. In this case, in
the packed-bed reduction reactor 12, some of the reduced iron supplied to the
melter-gasifier 30 is supplied to the reformer 40 to be used as a reforming
reaction catalyst, and the completely used reforming reaction catalyst is
charged to the melter-gasifier 30 to thereby manufacture the molten iron.
In contrast with the aforementioned exemplary embodiment of the
present invention, according to a conventional art, the discharge gas is
compressed for circulation and reforming of the discharge gas and oxygen is
removed from therefrom. In this case, a large amount of energy is consumed.
33
Further, most of the aforementioned energy is consumed for compressing the
discharge gas. Accordingly, economic efficiency may be lost because a cost
to reform and circulate the discharge gas as compared with coal cost that is
reduced by using the aforementioned method is increased.
Further, in the molten iron manufacturing process, nitrogen gas mixed in
the reducing gas to prevent local cooling and powder clogging in the meltergasifier
and the reactor is not separated and removed in the circulating and
reforming of the discharge gas. As a result, nitrogen gas serving as an inert
gas among the reducing gas remains and is integrated, thereby deteriorating
the quality of the reducing gas supplied to the reduction reactor. Accordingly,
this deteriorates an effect of reducing coal consumption according to
reformation and use of the discharge gas and also increases energy consumed
to reform the discharge gas, i.e., to remove carbon dioxide, to deteriorate an
effect of removing carbon dioxide. Particularly, since the quality of the
reducing gas deteriorates depending on nitrogen integration, a supply of the
reducing gas obtained by reforming the discharge gas is required to be limited
to a predetermined level or less, thereby deteriorating the effect of reducing coal
consumption of the melter-gasifier.
The reason for reducing the coal consumption is a reduction of coal
reserves used for manufacturing the molten iron and a price increase caused by
a global coal consumption increase. An example of a base material for
manufacturing the molten iron, which can replace coal, may include a natural
gas mainly containing hydrocarbon. The natural gas field has been actively
developed, and the price of the natural gas is expected to be reduced and
34
stabilized in the long term since there is an increase in shale gas mining based
on the North America region. However, it is required to reform hydrocarbon
included in a natural gas into a reducing gas such as hydrogen and carbon
monoxide to use the natural gas when molten iron is manufactured, and there is
a problem in which a large amount of thermal energy is consumed in the
reforming process.
Accordingly, when the molten iron is manufactured by using a
hydrocarbon gas, the hydrocarbon gas is reformed into a reducing gas by using
high-temperature gas-reforming equipment. Next, iron ore is reduced from a
solid state thereof by using the reformed gas, and then is melted in an electric
furnace or the like. However, according to this method, a huge amount of
energy is consumed for the operation of the high temperature gas equipment
and melting of the reduced iron ore, and thus economic efficiency may
deteriorate due to a supply price variation of the natural gas depending on
locational conditions.
Further, a method of injecting the natural gas through a tuyere through
which an oxidizing agent is injecting to combust cokes or general coal is added.
According to this method, the hydrocarbon is reformed into a reducing gas by
using combustion heat of cokes or general coal and is supplied to a fluidizedbed
reduction reactor or the like connected with an upper portion of the blast
furnace and the melter-gasifier together with a reducing gas generated by the
combustion of cokes or general coal, thereby reducing consumption of cokes or
general coal. However, according to this method, an amount of heat
generated by combustion of cokes or general coal around a tuyere of the
35
melter-gasifier and the blast furnace due to energy consumed to reform the
hydrocarbon is lower than an amount of heat required to operate the blast
furnace and melter-gasifier. Accordingly, there is a limit in consumption of
cokes or general coal by injecting a natural gas.
In contrast with the aforementioned conventional art, according to an
exemplary embodiment of the present invention, the hydrocarbon is mixed with
a discharge gas of the reduction reactor and is reformed to be used. As a
result, reducing power of the reducing gas is increased, and the consumption of
coal required to manufacture molten iron is reduced. This will be described in
more detail by using the following experimental example. The experimental
example is merely an example for describing the present invention, and the
present invention is not limited thereto.
Experimental Example
A molten iron manufacturing apparatus having the same structure as
shown in FIG. 1 was examined. In the molten iron manufacturing apparatus,
180 tons of molten iron was manufactured. 18,500 Nm3/h of natural gas was
supplied as a hydrocarbon gas, and this natural gas was mixed with a discharge
gas of a fluidized-bed reduction reactor to manufacture 300,631 Nm3 of supply
gas. Then, it was supplied to the fluidized-bed reduction reactor. In further
detail, a mixed gas obtained by mixing 18,500 Nm3/h of natural gas with the
discharge gas was reformed to manufacture 97,020 Nm3 of reformed gas, and
then the reformed gas was mixed with 231,084 Nm3/h of reducing gas
generated in a discharge gas. The mixed gas was heated by using 5,061
Nm3/h of oxygen. Fine ore and a sub-material were charged at 308 ton/h to
36
the fluidized-bed reduction reactor, and reduced iron was manufactured as
compacted iron by using an agglomeration apparatus and was charged at 232
ton/h to the melter-gasifier together with 22 ton/h of flux. Coal was charged at
117 ton/h to the melter-gasifier. As a result, 180 ton/h of molten iron was
manufactured in the melter-gasifier.
Comparative Example
Without supplying the natural gas to the molten iron manufacturing
apparatus, the discharge gas discharged from the fluidized-bed reduction
reactor was reformed by using a reformer by, e.g., removing oxygen from the
discharge gas. Accordingly, a supply gas mixed into the reducing gas
generated in the melter-gasifier was supplied to the fluidized-bed reduction
reactor to reduce iron ore. Detailed information of the experiment is disclosed
in European Patent Laid-Open Publication No. 1,689,892, and may be easily
understood by a skilled person in the art, so it will be omitted.
Experimental result
Table 1 shows properties of reducing gas, reformed gas, and supply gas
according to the experimental example and properties of the supply gas
according to the comparative example.
[Table 1]
NO Properties
Experimental Example
Comparative
Example
reducing
gas
reformed
gas
supply
gas
supply gas
37
1 Flow rate (Nm3/h) 231,804 97,020 300,631 300,505
2 Temperature (°C) 1,050 720 720 720
3 Pressure (bar.g) 4.00 6.00 3.80 3.8
4
Gas
composition
(%)
CO 63.26 38.65 55.78 56.82
CO2 9.58 10.95 10.09 8.78
H2 17.15 34.48 22.86 16.75
H2O 4.64 5.86 4.34 3.43
CH4 1.50 6.20 3.02 1.64
N2 3.87 3.86 3.90 12.59
In the experiment example, in the case of producing 1 ton of molten iron,
the coal consumption was 650 kg/ton of molten iron. In contrast, in the
comparative example, in the case of producing 1 ton of molten iron, the coal
consumption was 750-850 kg/ton of molten iron. Accordingly, the experimental
example has coal consumption that is reduced by about 15 % to 31 % as
compared with the comparative example. This is because the quality of the
supply gas deteriorates due to nitrogen integration according to reformation and
circulation of the discharge gas to limit an amount of the discharge gas that is
reformed and circulated to increase an amount of the reducing gas supplied to
the fluidized-bed reduction reactor according to the comparative example.
Further, a corresponding coal consumption reduction is limited. Meanwhile, an
amount of nitrogen included in the supply gas is more significantly reduced in
the experimental example than in the comparative example, and an amount of
hydrogen included in the supply gas is increased according to the use of the
hydrocarbon gas. As the quality of the supply gas is improved, reduction
38
operation efficiency of the fluidized-bed reduction reactor is more significantly
increased in the experimental example than in the comparative example.
While this invention has been described in connection with what is
presently considered to be practical exemplary embodiments, it is to be
understood that the invention is not limited to the disclosed embodiments, but,
on the contrary, is intended to cover various modifications and equivalent
arrangements included within the spirit and scope of the appended claims.
[Reference numerals]
10. fluidized-bed reduction reactor
12. packed-bed reduction reactor
20. compacted iron manufacturing device
22. compacted iron supplying pipe
23. distributing chute
24. compacted iron returning pipe
30. melter-gasifier
40, 49, 401, 403. reformer
41, 42. pressure gauge
43, 44. differential pressure gauge
45, 46. level meter
47, 48. discharge gas pipe
50. heat exchanger
60. first heater
62. first heater
70. supply gas pipe
39
80. dry dust collector
82. water cooling device
84. compressor
90. discharge gas pipe
92. discharge gas branch pipe
93. mixed gas pipe
94. reformed gas pipe
100, 200. molten iron manufacturing apparatus
231, 233, 241, 243, 471, 491, 931, 933, 941, 943, 4913, 4914, 4910,
4911, 4951, 4917, 4918, 4920, 4922, 4951. valve
405, 407. nitrogen supplying pipe
491, 493. reduced iron charging hopper
495, 497. reduced iron discharging hopper
4031. mixed gas inlet
4033. mixed gas supplier
4035. opening
4914, 4921. pressurization line
40
WE CLAIMS:
【Claim 1】
A molten iron manufacturing method comprising:
supplying a discharge gas from a reduction reactor that converts iron
ore to reduced iron;
supplying a mixed gas that is obtained by mixing some branched
discharge gas and a hydrocarbon gas;
supplying a reformed gas by reforming the mixed gas; and
injecting a reducing gas, discharged from a melter-gasifier connected
with the reduction reactor to receive the reduced iron, and the reformed gas into
the reduction reactor,
wherein the supplying of the reformed gas includes
supplying some of the reduced iron as a reforming reaction catalyst, and
reforming the mixed gas by using the reforming reaction catalyst.
【Claim 2】
The molten iron manufacturing method of claim 1, wherein said some
reduced iron is directly supplied from the reduction reactor in the supplying of
said some reduced iron as the reforming reaction catalyst.
【Claim 3】
The molten iron manufacturing method of claim 1, further comprising
agglomerating the reduced iron by compressing it,
41
wherein said some reduced iron is agglomerated and supplied in the
supplying of said some reduced iron as the reforming reaction catalyst.
【Claim 4】
The molten iron manufacturing method of claim 2, further comprising
recovering said some reduced iron used as the reforming reaction
catalyst and supplying it to the melter-gasifier.
【Claim 5】
The molten iron manufacturing method of claim 2, wherein the reformed
gas is generated in at least one reformer to which said some reduced iron in the
supplying of the reformed gas is charged, and nitrogen is supplied to the
reformer.
【Claim 6】
The molten iron manufacturing method of claim 5, wherein the mixed
gas is annularly rotated in the reformer and is injected in a circumferential
direction.
【Claim 7】
The molten iron manufacturing method of claim 1, wherein the reformed
gas is generated in a plurality of reformers to which said some reduced iron is
charged to be used as the reforming reaction catalyst in the supplying of the
42
reformed gas, and the reformers includes a first reformer and a second reformer.
【Claim 8】
The molten iron manufacturing method of claim 7, wherein said some
reduced iron is charged into the second reformer after charging of said some
reduced iron into the first reformer is completed.
【Claim 9】
The molten iron manufacturing method of claim 7, wherein, when a
differential pressure of the first reformer is equal to or higher than a
predetermined value, an inflow of the mixed gas into the first reformer is
blocked, and a reformed gas is generated in the second reformer by supplying
the mixed gas to the second reformer.
【Claim 10】
The molten iron manufacturing method of claim 7, wherein, when a
differential pressure of the first reformer is equal to or higher than a
predetermined value, the reformed gas is externally outputted.
【Claim 11】
The molten iron manufacturing method of claim 7, wherein, after the
reformed gas of the first reformer is discharged, the first reformer is purged, the
reforming reaction catalyst included in the first reformer is discharged, and said
43
some reduced iron is supplied to the first reformer.
【Claim 12】
The molten iron manufacturing method of claim 1, wherein, in the
supplying of the reformed gas, said some reduced iron is continuously charged
to and discharged from the reformer that generates the reformed gas.
【Claim 13】
The molten iron manufacturing method of claim 1, wherein the supplying
of the reformed gas includes:
providing a plurality of reduced iron charging hoppers connected to the
reformer in front thereof and a plurality of reduced iron discharging hoppers
connected to the reformer in back thereof;
adjusting a differential pressure between the reduced iron charging
hoppers;
charging said some reduced iron to the reformer through the reduced
iron charging hoppers;
adjusting a differential pressure between the reduced iron discharging
hoppers; and
discharging said some reduced iron from the reformer through the
reduced iron discharging hoppers.
【Claim 14】
44
The molten iron manufacturing method of claim 1, further comprising:
performing primary heating on the mixed gas by allowing it to indirectly
contact the discharge gas; and
performing secondary heating on the mixed gas by using oxygen.
【Claim 15】
The molten iron manufacturing method of claim 14, wherein the
discharge gas is cooled and cleaned in the supplying of the discharge gas.
【Claim 16】
The molten iron manufacturing method of claim 14, wherein the mixed
gas is heated to 1000 °C or less in the performing of the primary heating on the
mixed gas.
【Claim 17】
The molten iron manufacturing method of claim 16, wherein the mixed
gas is heated in a range of 1100 °C to 1200 °C in the performing of the
secondary heating on the mixed gas.
【Claim 18】
The molten iron manufacturing method of claim 1, wherein the reduction
reactor includes a packed-bed reduction reactor or a plurality of fluidized-bed
reduction reactors in the supplying of the discharge gas.
45
【Claim 19】
The molten iron manufacturing method of claim 18, wherein when the
reduction reactor includes the fluidized-bed reduction reactors, a mixture
obtained by mixing the reducing gas and the reformed gas is supplied to each
of the fluidized-bed reduction reactors.
【Claim 20】
A molten iron manufacturing apparatus comprising:
a reduction reactor configured to reduce iron ore into reduced iron;
a melter-gasifier connected with the reduction reactor to manufacture
molten iron by receiving the reduced iron and to supply a reducing gas to the
reduction reactor;
a discharge gas pipe connected with the reduction reactor to pass a
discharge gas discharged from the reduction reactor therethrough;
a discharge gas branch pipe connected with the discharge gas pipe to
pass another discharge gas that is branched from the discharge gas, and to
receive a hydrocarbon gas and supply a mixed gas obtained by mixing the
hydrocarbon gas with the discharge gas;
at least one reformer connected with the reduction reactor to receive
some of the reduced iron, and connected with the discharge gas branch pipe to
supply a reformed gas by reforming the mixed gas by said some reduced iron;
a supply gas pipe configured to supply the reducing gas to the meltergasifier
by connecting the reduction reactor with the melter-gasifier; and
46
a reformed gas pipe configured to connect the reformer with the supply
gas pipe, and to supply a mixture obtained by mixing the reformed gas with the
reducing gas to the melter-gasifier.
【Claim 21】
The molten iron manufacturing apparatus of claim 20, further comprising
a heat exchanger connected with the discharge gas pipe and the
discharge gas branch pipe, to heat the mixed gas by the discharge gas.
【Claim 22】
The molten iron manufacturing apparatus of claim 20, further comprising
a compacted iron manufacturing device connected with the reduction reactor
and the melter-gasifier, to supply compacted iron obtained by agglomerating the
reduced iron to the melter-gasifier, and connected with the reformer to supply
said some reduced iron as the compacted iron.
【Claim 23】
The molten iron manufacturing apparatus of claim 22, further
comprising:
a compacted iron supplying pipe configured to connect the compacted
iron manufacturing device with the reformer, and to supply the compacted iron
to the reformer; and
a compacted iron returning pipe configured to connect the compacted
47
iron manufacturing device with the reformer, and to return other compacted iron
that has completely been used to the compacted iron manufacturing device.
【Claim 24】
The molten iron manufacturing apparatus of claim 20, further
comprising:
a first heater connected with the heat exchanger and the discharge gas
pipe to heat the mixed gas by receiving and combusting the discharge gas; and
a second heater connected with the first heater to re-heat the mixed gas
by receiving oxygen.
【Claim 25】
The molten iron manufacturing apparatus of claim 20, wherein said at
least one reformer includes a plurality of reformers including a reforming
reaction catalyst, and the reformers include a first reformer and a second
reformer, and
the molten iron manufacturing apparatus further comprises:
a mixed gas supplying pipe configured to connect the heat exchanger
with the first reformer and the second reformer;
a purge gas supplying pipe connected to the first reformer and the
second reformer; and
a discharge gas pipe connected to the first reformer and the second
reformer.
48
【Claim 26】
The molten iron manufacturing apparatus of claim 25, further
comprising:
a pressure gauge mounted in each of the first reformer and the second
reformer to measure each internal pressure of the first reformer and the second
reformer;
a differential pressure gauge mounted in each of the first reformer and
the second reformer to measure a difference between pressures of upper
portions of the first reformer and the second reformer and an internal pressure
of the mixed gas supplying pipe by connecting the upper portions thereof with
the mixed gas supplying pipe; and
a level meter mounted in each of the first reformer and the second
reformer to measure a height of the reforming reaction catalyst.
【Claim 27】
The molten iron manufacturing apparatus of claim 20, further
comprising:
a plurality of reduced iron charging hoppers disposed in front of the
reformer and connected in series with the reformer; and
a plurality of reduced iron discharging hoppers disposed in back of the
reformer and connected in series with the reformer.
【Claim 28】
49
The molten iron manufacturing apparatus of claim 27, further comprising
an inert gas injecting pipe mounted in at least one of the reduced iron
charging hoppers and the reduced iron discharging hoppers to pressurize an
inside of the hopper by injecting an inert gas into the hopper.
【Claim 29】
The molten iron manufacturing apparatus of claim 20, wherein the
reformer includes an annular mixed gas supplier to surround a center of the
reformer, a plurality of openings are separately formed at a predetermined
interval in the mixed gas supplier, and the mixed gas is injected into the
reformer through the openings.
【Claim 30】
The molten iron manufacturing apparatus of claim 20, wherein the
reduction reactor includes a packed-bed reduction reactor or a plurality of
fluidized-bed reduction reactors.
【Claim 31】
The molten iron manufacturing apparatus of claim 30, wherein, when the
reduction reactor includes the fluidized-bed reduction reactors, the supply gas
pipe is configured to connect each of the fluidized-bed reduction reactors with
the melter-gasifier.