WO1999020800A1 - Verfahren und vorrichtung zum einblasen von reduktionsmittel in einen schachtofen - Google Patents
Verfahren und vorrichtung zum einblasen von reduktionsmittel in einen schachtofen Download PDFInfo
- Publication number
- WO1999020800A1 WO1999020800A1 PCT/EP1998/006501 EP9806501W WO9920800A1 WO 1999020800 A1 WO1999020800 A1 WO 1999020800A1 EP 9806501 W EP9806501 W EP 9806501W WO 9920800 A1 WO9920800 A1 WO 9920800A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- heat exchanger
- flow
- reducing agent
- individual
- shaft furnace
- Prior art date
Links
- 239000003638 chemical reducing agent Substances 0.000 title claims abstract description 46
- 238000000034 method Methods 0.000 title claims abstract description 13
- 238000010438 heat treatment Methods 0.000 claims abstract description 47
- 238000012546 transfer Methods 0.000 claims description 24
- 238000007664 blowing Methods 0.000 claims description 21
- 229910052751 metal Inorganic materials 0.000 claims description 5
- 239000002184 metal Substances 0.000 claims description 5
- 239000007788 liquid Substances 0.000 claims description 4
- 238000009826 distribution Methods 0.000 claims description 2
- 230000001105 regulatory effect Effects 0.000 claims 1
- 239000007789 gas Substances 0.000 description 70
- 239000002817 coal dust Substances 0.000 description 25
- 238000006243 chemical reaction Methods 0.000 description 20
- 239000000203 mixture Substances 0.000 description 20
- 239000007787 solid Substances 0.000 description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 239000003245 coal Substances 0.000 description 5
- 238000013021 overheating Methods 0.000 description 5
- 239000002245 particle Substances 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 4
- 238000002347 injection Methods 0.000 description 4
- 239000007924 injection Substances 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 description 3
- 238000010276 construction Methods 0.000 description 3
- 230000007704 transition Effects 0.000 description 3
- 125000004432 carbon atom Chemical group C* 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000000197 pyrolysis Methods 0.000 description 2
- 230000005855 radiation Effects 0.000 description 2
- 229910000805 Pig iron Inorganic materials 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000012159 carrier gas Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000012790 confirmation Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000012432 intermediate storage Methods 0.000 description 1
- 229910001338 liquidmetal Inorganic materials 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 125000004430 oxygen atom Chemical group O* 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 239000008247 solid mixture Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B5/00—Making pig-iron in the blast furnace
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B5/00—Making pig-iron in the blast furnace
- C21B5/001—Injecting additional fuel or reducing agents
- C21B5/003—Injection of pulverulent coal
Definitions
- the present invention relates to a device for blowing reducing agent into a shaft furnace, in particular for blowing coal dust into a blast furnace in the production of pig iron.
- coal dust is extracted from raw coal in a processing plant.
- the raw coal is ground and dried and then stored in coal silos.
- the temporarily stored coal dust is loosened, pressurized and blown pneumatically into the shaft furnace by means of a carrier gas via delivery lines.
- the blowing is generally carried out by several blowing lances, which open into the blow molds of the shaft furnace, so that the entry occurs simultaneously at different points in the shaft furnace.
- the blown coal dust In order to achieve the greatest possible reduction in reducing agent costs by blowing in coal dust, the blown coal dust must be converted as completely as possible in the blow mold wind tunnel, so that only residual coke has to be gasified in the swirl zone.
- complete reaction herein means that "all the carbon atoms to material with oxygen, respectively, said carbon monoxide and / or carbon dioxide. If the conversion in this zone is not complete, which can be the case especially at high blowing rates, there is an accumulation of conversion residues in the shaft furnace, which leads to unstable furnace conditions.
- the main causes of the deficient coal dust conversion in the vortex zone are, on the one hand, the small dimensions of the actual reaction space and, on the other hand, the high speeds of the media and the flow properties of the hot wind in the blow mold.
- This object is achieved according to the invention by a method for blowing reducing agent into a shaft furnace according to claim 1 or by a device according to claim 6.
- the conveying stream is divided into several partial streams, which in turn are passed through a heating device, the reducing agent in the individual partial streams being heated up by heating in the heating device.
- the individual partial flows are preferably brought together again to form a common conveying flow for the purpose of homogenizing the temperature conditions, before the eventual distribution of the conveying flow among the individual blowing lances distributed around the shaft furnace takes place.
- coal dust By heating the coal dust within the heating device, heat can be supplied to the coal dust in a controlled manner, so that its temperature can be set to a value which is favorable for the use of the coal dust conversion in the shaft furnace.
- the coal dust preheated in this way consequently has to absorb significantly less heat from the hot wind after it has been blown into the shaft furnace in order to reach its ignition temperature, and its implementation in the shaft furnace sets significantly faster than with "cold" coal dust blown in, so that the short available reaction time for the implementation can be fully exploited.
- the lower heat transfer from the hot wind to the coal dust reduces the cooling of the reaction space, which can ensure that the temperature in the entire reaction space remains high enough to allow a reduction in the carbon dioxide formed in the coal dust conversion to carbon monoxide.
- this results in a further increase in coal dust conversion since the oxygen atoms present can bind significantly more carbon atoms to themselves.
- the increased carbon monoxide content has a very positive effect on the functioning of the shaft furnace, since it serves as a reducing agent for the actual metal extraction.
- the reducing agent is heated in several stages, that is to say the steps of dividing the flow into several partial flows, passing the individual partial flows through a heating device and heating the reducing agent in the individual partial flows within the heating device are repeated several times, the individual - NEN partial flows between two successive stages for homogenizing the temperature conditions can be merged into a common flow.
- the reducing agent in a partial flow In order to improve the heat transfer to the reducing agent in a partial flow, it is preferably set in a rotational movement about its direction of flow.
- the rotational movement and the associated turbulence in the partial flow causes the material in the partial flow to be rearranged so that the partial flow is thoroughly mixed.
- the speed of the individual particles in the partial flow and their exchange path length in the heat exchanger increase. As a result, the heat transfer to the reducing agent in the heat exchanger can be significantly improved. All partial flows are therefore preferably set into such a rotational movement.
- cold reducing agent can be metered into the common flow to regulate the blowing-in temperature of the reducing agent before it is blown into the shaft furnace.
- a device for blowing reducing agent into a shaft furnace comprises a conveying line for pneumatically conveying the reducing agent to the shaft furnace, a plurality of heat exchanger tubes which are integrated into the conveying line in a fluidic parallel connection, so that the pneumatic conveying flow is divided into several partial flows, and a heating device for transferring thermal energy to the individual partial flows.
- the reducing agent can be supplied with heat in a controlled manner during its transport between a storage container and the blowing lances on the shaft furnace.
- the heating takes place within the delivery line, ie it can take place immediately before the coal dust is blown into the shaft furnace.
- the coal dust is consequently released to the consumer immediately after heating, so that safety problems in the intermediate storage of a heated fuel are eliminated.
- the heat losses to the The environment is very small, not least because of the reduced radiation area.
- the required effective heat transfer surface is obtained in an arrangement with small dimensions, i.e. the area at which heat is transferred to the reducing agent or the respective partial flow.
- small dimensions i.e. the area at which heat is transferred to the reducing agent or the respective partial flow.
- a high heat transfer coefficient occurs in the solid-conveying gas mixture.
- the individual substreams can consequently absorb large amounts of heat in a very short time and over a short distance, so that the length of the heat exchanger tubes can be kept correspondingly small.
- the entire device is accordingly characterized by its compact design, which can be of great importance, for example, when converting existing systems.
- the heating device comprises a heating chamber to which a heat transfer medium can be applied, the heat exchanger tubes being arranged within the heating chamber or extending, at least partially, through the heating chamber.
- the heat transfer medium can comprise, for example, a hot gas from a furnace. There is then a direct heat transfer between hot gas and solid-conveying gas mixture. Due to the high temperature of the hot gas, the medium temperature gradient of the hot gas to the mixture of solid and conveying gas causing the heat exchange can be kept large. In addition, due to the (partially) high temperatures in the hot gas, a significant heat transfer by radiation is added to the convective heat transfer on the hot gas side, so that overall a very high heat flow density is achieved.
- the furnace is preferably operated with lean gas, eg blast furnace gas. This avoids unfavorably high combustion temperatures, which would make it necessary to pre-cool the hot gas before entering the heating chamber in normal operation.
- lean gas eg blast furnace gas.
- the when operating with high medium Temperature differences from hot gas to solid-conveying gas mixture The high exhaust gas temperature that arises behind the heating chamber does not constitute a significant economic loss if the residual heat of the exhaust gas is not used any further. If the heat exchanger tubes are not exposed to the conveying gas-solid mixture, for example when starting the Hot gas side, the hot gas can be brought to a lower temperature by adding cold air behind the furnace, thereby protecting the heat exchanger tubes from overheating.
- the exhaust gas can be cooled to a permissible discharge temperature by admixing cold air if the device is operated with a high medium temperature gradient, hot gas to solid-conveying gas mixture, and the exhaust gas is to be released into the environment immediately after leaving the heat exchange device without further use of the residual heat.
- the heat transfer medium can comprise a liquid or a condensing medium.
- a liquid heat transfer medium has a higher specific heat capacity C p than the gaseous one, so that here a larger amount of heat per volume can be carried and emitted.
- a condensing medium ie a medium that performs a phase transition when heat is emitted, is distinguished by a high heat emission at a constant temperature.
- a medium is therefore preferably selected, the condensation temperature of which corresponds to the desired blowing-in temperature of the reducing agent.
- the heat exchanger tubes are advantageously arranged essentially vertically and the partial flows flow through them from bottom to top. This prevents solid deposits with local pipe overheating, the pipe cross-section is applied evenly, and the heat transfer from the pipe wall to the solid-conveying gas mixture flow is optimized.
- a swirl body is arranged in one or more, but preferably in all, heat exchanger tubes, which rotates the partial stream flowing through the respective heat exchanger tube about its direction of flow. The mixing of the respective partial flow is improved by the rotation of the partial flow, so that the heat transfer to the partial flow is improved.
- the speed of the individual particles in the partial flow and their exchange path length in the heat exchanger increase.
- the swirl body can comprise, for example, one or more spirally twisted metal strips which extend in the axial direction inside the heat exchanger tube.
- the slope of the spiral twist of the respective metal strip can be chosen in accordance with the desired exchange path length of the reducing agent in the heat exchanger.
- the distributor and the collector are preferably identical in construction, so that the direction of installation of the heat exchanger bundles is irrelevant.
- the heat exchanger tubes are consequently combined into easy-to-assemble, standardized units, and clogged heat exchanger bundles can be easily replaced if necessary.
- the flow can be divided into several partial flows in several stages.
- the flow is divided, for example, into several heat exchanger bundles via pre-distributors.
- the device accordingly comprises a plurality of heat exchanger bundles, the heat exchanger bundles preferably being assembled together at a certain distance from one another to form a heat exchanger group and the heat exchanger group on the input side has a pre-distributor for evenly distributing an incoming flow to the individual heat exchanger bundles and on the output side it has an additional collector for merging the individual partial streams into a common output stream.
- the pre-distributor and the second collector are preferably of identical construction, for example they are of the type of the distributor for particle streams described in US Pat. No. 4,702,182.
- a plurality of heat exchanger bundles or heat exchanger groups are connected in series. This enables a compact arrangement to be achieved. Behind each heat exchanger bundle or each heat exchanger group, the solid-conveying gas mixture partial flows are brought together and any temperature increases that may occur in the individual tubes or tube bundles are compensated for. The failure of individual pipes or individual pipe bundles does not significantly affect the functionality and the exchange performance of the entire facility. In a system with heat exchanger groups, individual bundles, if shut-off valves are available, can be taken out of service for maintenance or shutdown.
- Guiding devices are advantageously arranged within the heating chamber in such a way that the heat transfer tubes are effectively flowed through by the heat transfer medium.
- the guide devices can be guide plates, for example, which direct the hot gas flow specifically to the individual heat exchanger bundles.
- a bypass line is preferably to be provided, which, seen in the flow direction of the delivery flow, opens into the delivery line behind the heat exchanger tubes.
- This allows the conveyor operation to continue practically without a transition.
- the changeover between the heat exchange device and the bypass line can be carried out gradually and smoothly by using solid mass flow control valves, with minimizing the risk of line blockages. If several solid-conveying gas mixtures are heated in parallel, with the entire hot gas supply coming from one furnace, different heating temperatures can be set in the individual solid-conveying gas mixtures with the aid of the solid mass flow control valves.
- 1 the schematic structure of a first embodiment of a device according to the invention for blowing reducing agent into a shaft furnace
- 2 the schematic structure of a second embodiment of a device according to the invention
- FIG. 5 shows a partially sectioned view of a detail from FIG. 4;
- FIG. 10 A first embodiment of a device according to the invention for blowing reducing agent into a shaft furnace is shown in FIG. It comprises a pressure vessel 10, into which the reducing agent is introduced before the blowing in, and a plurality of delivery lines 12, through which the reducing agent is pneumatically transported with a conveying gas to blowing lances (not shown) on the shaft furnace.
- a plurality of heat exchanger tubes 14 are integrated in each flow line 12 in a fluidic parallel circuit, by means of which the flow is divided into a number of partial flows.
- the heat exchanger tubes 14 are preferably combined to form heat exchanger bundles 16, in which the heat exchanger tubes 14 are mounted at a certain distance from one another, the heat exchanger bundles 16 on the input side having a distributor 18 for uniformly distributing an incoming flow to the individual Has heat exchanger tubes 14 and on the output side a collector 20 for merging the individual partial streams into an output stream.
- the heat exchanger bundles 16 are arranged in a heating chamber 22, in which a hot gas is generated by means of a furnace 24 which flows around the heat exchanger bundles 16.
- a hot gas is generated by means of a furnace 24 which flows around the heat exchanger bundles 16.
- the heat contained in the hot gas is given off to the individual partial flows in the heat exchanger tubes 14 and the reducing agent transported therein is heated.
- the heat transfer medium can also comprise a liquid or a condensing medium.
- the heat exchanger bundles 16 are advantageously each arranged essentially vertically and the partial flows flow through them from bottom to top. Deposits with local pipe overheating are avoided, the pipe cross-section is applied evenly, the heat transfer from the pipe wall to the reducing agent-conveying gas mixture is optimized.
- the hot gas is preferably generated in a combustion chamber 26 of the heating chamber 24 and passed in a cross flow between the heat exchanger tubes 14 (indicated by the arrow 28). After the hot gas has given off a large part of its heat to the various partial flows, the cooled hot gas is discharged via an exhaust pipe 30.
- the hot gas is advantageously generated by burning lean gas, for example blast furnace gas, with fresh air, which is fed to the furnace 24 via a gas supply 32 or fresh air supply 34. This avoids unfavorably high combustion temperatures, which would make it necessary to pre-cool the hot gas before entering the heating chamber 22 in normal operation.
- the hot exhaust gas temperature to the reducing agent / conveying gas mixture which arises behind the heating chamber 22 does not constitute a significant economic loss if the residual heat of the exhaust gas is not used further. If the heat exchanger tubes 14 have not yet been subjected to a reducing agent / conveying gas mixture, for example in the case of Approaching the hot gas side, the hot gas can be brought to a lower temperature behind the furnace by means of a cold air supply 36 and the heat exchanger tubes 14 can thereby be protected against overheating.
- the exhaust gas in the exhaust gas line 30 can be cooled to a permissible delivery temperature by admixing cold air via a cold air supply 38 if the device operates with a high medium temperature gradient hot gas to a reducing agent / conveying gas mixture and the exhaust gas after leaving the heat exchange device without further use of the residual heat to be released directly into the environment.
- a bypass line 40 is provided for each delivery line 12, which, seen in the flow direction of the delivery flow, opens into the delivery line 12 behind the heat exchanger bundles 16. In the event of a failure of the heat exchange device or a lack of heating, this allows the conveyor operation to be maintained.
- the changeover between heat exchanger bundles 16 and bypass line 40 can be carried out gradually and smoothly by using solid mass flow control valves 42, with minimization of the risk of line blockages.
- the regulation of the volume flow of the reducing agent-conveying gas mixture by the heat exchanger bundle 16 by means of the solid volume flow control valves can also be used advantageously for efficient temperature control of the flow. If, as shown, several reducing agent-feed gas mixtures are heated in parallel, with the entire hot gas supply coming from one furnace, different heating temperatures can be set in the individual solid-feed gas mixtures with the aid of the solid mass flow control valves.
- the division of the delivery flow into several partial flows can take place in several stages.
- the flow rate is divided, for example, via pre-distributors 48 into a plurality of heat exchanger bundles 16.
- the device accordingly comprises a plurality of heat exchanger bundles 16 which are integrated into the delivery line 12 in a fluidic parallel connection.
- the heat exchanger bundles 16 are preferably assembled at a certain distance from one another to form a heat exchanger group 50, the heat exchanger group 50 on the input side having a pre-distributor 48 for evenly distributing an incoming flow to the individual heat exchanger bundles 16 and on the output side an additional collector 52 for combining the individual partial streams into a common one Output current has.
- a plurality of heat exchanger groups are preferably connected in series.
- the reducing agent-conveying gas mixture partial flows are brought together behind each heat exchanger group and any temperature increases that occur in the individual tube bundles are compensated for.
- the failure of individual tube bundles does not significantly impair the functionality and the exchange performance of the entire facility.
- shut-off valves are provided, individual bundles can be taken out of service for maintenance or shutdown.
- FIG. 3 shows a section through a heat exchanger bundle 16. It comprises a plurality of heat exchanger tubes 14 which extend at a certain distance from one another.
- the heat exchanger tubes 14 are advantageously arranged in a circle around a longitudinal axis 54 of the heat exchanger bundle 16, a coaxial guide tube 56 being arranged at a short distance from the heat exchanger tubes 14 in the center between the heat exchanger tubes 14.
- This guide tube 56 discharges the hot gas stream arriving laterally and guides it past the individual heat exchanger tubes 14, so that the hot gas effectively flows onto the heat exchanger tubes 14.
- at least one mounting ring 58 can be attached to the guide tube 56, through which the heat exchanger tubes 14 are held in their respective positions.
- This mounting ring 58 advantageously extends outwards over half the length of the guide tube 56 and has bores through which the individual heat exchanger tubes 14 are guided.
- the heat exchanger tubes 14 are connected on the one hand to a distributor 18 and on the other hand to a collector 20.
- the distributor 18 divides the delivery flow arriving at an inlet flange 60 evenly into different partial flows, each of which is passed into one of the heat exchanger tubes 14. After passing through the heat exchanger tubes 14, the individual partial streams in the collector 20 are brought together again to form a common delivery stream and transferred to an output flange 62 in the subsequent delivery line.
- the different heat exchanger tubes 14 preferably have the same cross section and the same length, so that the individual partial flows and thus the flow velocities of the partial flows in the respective heat exchanger tubes 14 are largely the same. In this way, larger deviations in the temperature increases between the individual partial flows can be avoided.
- the distributor 18 and the collector 20 are preferably of identical construction, so that the heat exchanger bundle 16 is symmetrical with respect to a plane transverse to that
- the heat exchanger bundle 16 accordingly has none preferred installation direction, and consequently represents an easy-to-assemble, standardized unit which enables a quick exchange of clogged heat exchanger bundles 16.
- the heat exchanger bundles 16 are preferably installed in the heating chamber 22 by means of flanges 64 which are attached to the distributor 18 and collector 20 and which are screwed to the housing wall 68 of the heating chamber 22 with corresponding flanges 66.
- a compensator 70 is inserted on at least one side to compensate for the thermal expansion of the material.
- the different heat exchanger bundles 16 of the heat exchanger groups 50 are arranged essentially parallel to one another and side by side in several rows running in the flow direction of the hot gas.
- a heat exchanger group 50 comprises six rows, each with four heat exchanger bundles 16.
- the heat exchanger bundles 16 are mounted with their flanges 64 on the corresponding flanges 66 of the upper and lower heating chamber walls.
- connecting lines 72 between pre-distributor 48 or collector 52 and heat exchanger bundle 16 are shown in FIG.
- the connecting lines 72 are preferably designed as hoses in order to be able to compensate for thermal expansion.
- all the connecting lines are advantageously of the same length in order to implement the same partial flows with the same pressure drops in the individual lines.
- guide plates 74 are preferably attached, which direct the hot gas flow onto the individual heat exchanger bundles 16, so that an effective heat Transition is achieved.
- the guide plates 74 extend on both sides of a row of heat exchanger bundles 16 in such a way through the entire heat exchanger group 50 that an inflow channel 76 running in the flow direction of the hot gas is separated in the heating chamber 22 between two guide plates 74.
- the baffles 74 at the level of the heat exchanger bundles 16 preferably each have widenings 78 which extend outward from the heat exchanger bundle 16 and extend vertically upward, so that each heat exchanger bundle 16 is arranged in a substantially cylindrical receiving space which is in line with the receiving spaces of the adjacent heat exchanger bundles 16 of a row is connected by a straight line piece.
- the adjacent guide plates 74 of two adjacent rows are preferably brought together at an incline, so that the individual inflow channels are widened on the inlet and outlet sides and the inflowing hot gas is consequently channeled into the inflow channel.
- a hot gas flow that flows through the heat exchanger group is accordingly directed completely into the individual inflow channels, the hot gas speed in the individual inflow channels increases, and the flow against the heat exchanger bundles 16 arranged therein is optimized.
- the heat exchanger groups 50 configured in this way advantageously form standardized components, any number of which can be connected in series as required.
- the hot gas flowing through passes directly at the outlet of the first heat exchanger group into the inlet of the second heat exchanger group, etc.
- each heat exchanger tube 14 which extend along the longitudinal axis of the heat exchanger tube.
- the swirl body can as shown in Fig. 6, for example, a spirally twisted metal sheet, the slope of which is selected such that the exchange path length and the residence time of the reducing agent in the heat exchanger tube 14 are optimized for the desired heat absorption.
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
- Furnace Charging Or Discharging (AREA)
- Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
- Heat Treatment Of Articles (AREA)
- Manufacture Of Iron (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
- Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
Abstract
Description
Claims
Priority Applications (7)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE59801347T DE59801347D1 (de) | 1997-10-15 | 1998-10-14 | Verfahren und vorrichtung zum einblasen von reduktionsmittel in einen schachtofen |
AU19615/99A AU735069B2 (en) | 1997-10-15 | 1998-10-14 | Method and device for injection of reducing agents into a shaft furnace |
US09/529,057 US6478846B1 (en) | 1997-10-15 | 1998-10-14 | Method and device for injecting reducing agents in a shaft furnace |
JP2000517118A JP4139075B2 (ja) | 1997-10-15 | 1998-10-14 | 高炉に還元剤を注入する方法および装置 |
EP98964392A EP1023468B1 (de) | 1997-10-15 | 1998-10-14 | Verfahren und vorrichtung zum einblasen von reduktionsmittel in einen schachtofen |
BR9812932-5A BR9812932A (pt) | 1997-10-15 | 1998-10-14 | Processo e dispositivo para injeção de um meio de redução em um forno de cuba |
AT98964392T ATE204910T1 (de) | 1997-10-15 | 1998-10-14 | Verfahren und vorrichtung zum einblasen von reduktionsmittel in einen schachtofen |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
LU90150A LU90150B1 (de) | 1997-10-15 | 1997-10-15 | Verfahren un Vorrichtung zum Einblasen von Reduktionsmittel in einen Schachtofen |
LU90150 | 1997-10-15 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO1999020800A1 true WO1999020800A1 (de) | 1999-04-29 |
Family
ID=19731714
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP1998/006501 WO1999020800A1 (de) | 1997-10-15 | 1998-10-14 | Verfahren und vorrichtung zum einblasen von reduktionsmittel in einen schachtofen |
Country Status (13)
Country | Link |
---|---|
US (1) | US6478846B1 (de) |
EP (1) | EP1023468B1 (de) |
JP (1) | JP4139075B2 (de) |
KR (1) | KR100584848B1 (de) |
CN (1) | CN1083887C (de) |
AT (1) | ATE204910T1 (de) |
AU (1) | AU735069B2 (de) |
BR (1) | BR9812932A (de) |
DE (1) | DE59801347D1 (de) |
ES (1) | ES2161556T3 (de) |
LU (1) | LU90150B1 (de) |
TW (1) | TW348186B (de) |
WO (1) | WO1999020800A1 (de) |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
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DE102013006541A1 (de) | 2012-10-30 | 2014-04-30 | E.S.C.H. Engineering Service Center Und Handel Gmbh | Verfahren zur Herstellung von Roheisen im Hochofen |
LU92813B1 (en) * | 2015-09-02 | 2017-03-20 | Wurth Paul Sa | Enhanced pressurising of bulk material in lock hoppers |
CN111154933B (zh) * | 2020-01-03 | 2021-06-08 | 青岛恒拓环保科技有限公司 | 一种高炉喷煤系统喷吹罐之间的均压装置 |
Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE381917C (de) * | 1918-09-12 | 1923-12-14 | Ernst Diepschlag Dipl Ing | Verfahren zur Vorbereitung (z.B. Trocknen) der Brenn- und Schmelzstoffe fuer ihre unmittelbare Einfuehrung in die Schmelzzone von Schachtoefen |
DE410681C (de) * | 1921-06-09 | 1925-03-12 | Georges Etienne Pierre Forret | Vorrichtung zur Verteilung eines mit Stoffteilchen versetzten und aus einer Hauptleitung kommenden Gasstromes auf mehrere Nebenleitungen |
DE1608382A1 (de) * | 1962-12-21 | 1970-12-10 | Allied Chem | Verfahren und Vorrichtung zum Betreiben von Hochoefen |
US4325312A (en) * | 1979-07-17 | 1982-04-20 | Paul Wurth S.A. | Method and installation of injection of solid fuels into a shaft furnace |
US4373451A (en) * | 1981-04-06 | 1983-02-15 | Kennedy Van Saun Corporation | Apparatus and method for feeding pulverized solid fuel to a burner |
US4570552A (en) * | 1983-07-19 | 1986-02-18 | Paul Wurth S.A. | Process and apparatus for delivering carbon material to a furnace |
US4702182A (en) * | 1985-08-05 | 1987-10-27 | Paul Wurth S.A. | Process and apparatus for the injection by pneumatic means of metered amounts of pulverulent materials into a vessel which is under variable pressure |
Family Cites Families (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3197304A (en) * | 1961-10-12 | 1965-07-27 | United States Steel Corp | Method for introducing coal into a blast furnace |
LU71434A1 (de) * | 1974-12-06 | 1976-11-11 | ||
LU86701A1 (fr) * | 1986-12-04 | 1988-07-14 | Wurth Paul Sa | Procede d'injection par voie pneumatique,de quantites dosees de matieres pulverulentes,dans une enceinte se trouvant sous pression variable |
LU87453A1 (fr) * | 1989-02-14 | 1990-09-19 | Wurth Paul Sa | Procede d'injection pneumatique de quantites dosees de matieres pulverulentes dans une enceinte sous pression variable |
JPH04354810A (ja) * | 1991-05-30 | 1992-12-09 | Nisshin Steel Co Ltd | 高炉への微粉炭吹込み方法及び装置 |
ES2123018T3 (es) * | 1992-07-01 | 1999-01-01 | Wurth Paul Sa | Dispositivo para la inyeccion de carbon pulverizado en un crisol de alto horno. |
-
1997
- 1997-10-15 LU LU90150A patent/LU90150B1/de active
- 1997-12-20 TW TW086119408A patent/TW348186B/zh not_active IP Right Cessation
-
1998
- 1998-10-14 WO PCT/EP1998/006501 patent/WO1999020800A1/de active IP Right Grant
- 1998-10-14 CN CN98811451A patent/CN1083887C/zh not_active Expired - Fee Related
- 1998-10-14 BR BR9812932-5A patent/BR9812932A/pt not_active IP Right Cessation
- 1998-10-14 AU AU19615/99A patent/AU735069B2/en not_active Ceased
- 1998-10-14 JP JP2000517118A patent/JP4139075B2/ja not_active Expired - Fee Related
- 1998-10-14 AT AT98964392T patent/ATE204910T1/de active
- 1998-10-14 KR KR1020007003985A patent/KR100584848B1/ko not_active IP Right Cessation
- 1998-10-14 US US09/529,057 patent/US6478846B1/en not_active Expired - Lifetime
- 1998-10-14 ES ES98964392T patent/ES2161556T3/es not_active Expired - Lifetime
- 1998-10-14 DE DE59801347T patent/DE59801347D1/de not_active Expired - Lifetime
- 1998-10-14 EP EP98964392A patent/EP1023468B1/de not_active Expired - Lifetime
Patent Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE381917C (de) * | 1918-09-12 | 1923-12-14 | Ernst Diepschlag Dipl Ing | Verfahren zur Vorbereitung (z.B. Trocknen) der Brenn- und Schmelzstoffe fuer ihre unmittelbare Einfuehrung in die Schmelzzone von Schachtoefen |
DE410681C (de) * | 1921-06-09 | 1925-03-12 | Georges Etienne Pierre Forret | Vorrichtung zur Verteilung eines mit Stoffteilchen versetzten und aus einer Hauptleitung kommenden Gasstromes auf mehrere Nebenleitungen |
DE1608382A1 (de) * | 1962-12-21 | 1970-12-10 | Allied Chem | Verfahren und Vorrichtung zum Betreiben von Hochoefen |
US4325312A (en) * | 1979-07-17 | 1982-04-20 | Paul Wurth S.A. | Method and installation of injection of solid fuels into a shaft furnace |
US4373451A (en) * | 1981-04-06 | 1983-02-15 | Kennedy Van Saun Corporation | Apparatus and method for feeding pulverized solid fuel to a burner |
US4570552A (en) * | 1983-07-19 | 1986-02-18 | Paul Wurth S.A. | Process and apparatus for delivering carbon material to a furnace |
US4702182A (en) * | 1985-08-05 | 1987-10-27 | Paul Wurth S.A. | Process and apparatus for the injection by pneumatic means of metered amounts of pulverulent materials into a vessel which is under variable pressure |
Also Published As
Publication number | Publication date |
---|---|
LU90150B1 (de) | 1999-04-16 |
EP1023468A1 (de) | 2000-08-02 |
CN1279724A (zh) | 2001-01-10 |
BR9812932A (pt) | 2000-08-08 |
DE59801347D1 (de) | 2001-10-04 |
JP4139075B2 (ja) | 2008-08-27 |
TW348186B (en) | 1998-12-21 |
KR20010024493A (ko) | 2001-03-26 |
ES2161556T3 (es) | 2001-12-01 |
ATE204910T1 (de) | 2001-09-15 |
JP2003524700A (ja) | 2003-08-19 |
KR100584848B1 (ko) | 2006-05-29 |
CN1083887C (zh) | 2002-05-01 |
AU735069B2 (en) | 2001-06-28 |
AU1961599A (en) | 1999-05-10 |
EP1023468B1 (de) | 2001-08-29 |
US6478846B1 (en) | 2002-11-12 |
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