• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    This invention relates to the direct production of liquid iron from dispersed iron ore. The purpose of the invention. Shade is to increase productivity. In a two-stage process for producing liquid iron, a melter gasifier is used to burn coal gasification and regeneration and to dissolve DO Sla Sl: el. S / D 7
    公开号:SU1313354A3
    申请号:SU833661051
    申请日:1983-11-14
    公开日:1987-05-23
    发明作者:Вулетич Богдан
    申请人:Корф Инжинеринг Гмбх (Фирма)；Фоест Альпине Аг (Фирма)；
    IPC主号:
    专利说明:

    melting of pre-reduced dispersed iron ore. In this case, the pre-reduced ore is divided into two fractions — finely dispersed to 20 Mm and coarse-dispersed, and then the coarse-dispersed is separated for subsequent processing, and the finely dispersed is sent to the melter gasifier. This separation optimizes the amount of reducing gases produced, the cost of fuel, the cost of the desulfurization process, the amount of gas recirculated and its heating, and use as a carrier when dispersed materials are fed into the melter gasifier. An installation for carrying out the method includes a shaft furnace 2 for anticipation associated with pipeline 1
    The invention relates to metallurgy, in particular to a method for producing molten iron from dispersed iron ore.
     the invention is an increase in productivity.
    Not all the amount of sponge iron particles obtained in the direct reduction unit, but only a part of it, is fed into the fuel gasification melting reactor. The coarse dispersed fraction that is installed on the way from the shaft kiln reduction unit to the smelting reactor by gasification can be heated in a hot state to the next melting vessel, for example, in an electric arc furnace, it can also be hot briquetted, passivated or cooled in order to it could be used as a starting material for a smelting furnace.
    Since only a fine fraction is melted in the smelting reactor, it may be difficult if un-refined coal with a high sulfur content is fed into the smelting reactor. The fine-dispersed fraction is due to the larger surface of thin clocks through the ore separator according to size with a melting gasifier 1, which gasifies coal in a fluidized bed, restores dispersed ore and melts feed materials with the formation of liquid iron. The separator 7 is heat resistant in the form of a tray, a sieve or a grid, installed with the ability to oscillate. Downspout 12 of the pre-reconstituted ore has protrusions or a baffle wall. The installation also has a refrigerator, and the carbon dioxide purification unit is connected to the refrigerator and gas supply and gas outlet openings of the melting gasifier 1. 2c. and 19 3.p. f-ly, 4 ill.
    Sponge iron, by weight, binds a large relative proportion of sulfur.
    FIG. 1 schematically depicted
    installation that implements the proposed method; in fig. 2 - drain pipe with liquid cooling, longitudinal-. Nye slit} in FIG. 3 - coarse fraction separator; 1 and grains; in fig. 4 installation, implementing the proposed method, another option.
    The installation (Fig. 1) for the direct production of liquid iron from lump iron ore contains a gasification melting reactor 1 with gasification (gasifier) coal.
    Dispersed iron ore 3 is fed into the shaft furnace 2 direct reduction from the top, which is in the form of
    The free flowing mass is dipped down into a shaft furnace and with the help of hot reducing gas with a temperature of about 750-900 ° G blown through the middle holes 4
    the gas inlet is reduced to sponge iron. Used reducing gas (flue gas) out of the shaft furnace 2 through the upper outlet of the gas release - pipe 5.
    Hot sponge iron obtained by reducing dispersed iron ore with a temperature of about
    750-850 ° C is discharged from the bottom of the shaft furnace for direct reduction 2 and through pipe 6 enters the separator 7 of the coarse fraction. The latter alternatively may have a thermally loaded sieve with a mesh size of, for example, 12 mm, through which it does not pass, and sponge iron particles of more than 12 mm in size are retained. There is a separation into fine fraction and coarse fraction. Sponge iron particles of the fine fraction come out of the separator 7 of the coarse-dispersed fraction through the first outlet 8 and through the pipe 9 into the discharge device 10, which has, for example, a scraper or auger. The sponge iron particles of the coarse-grained fraction exit the separator 7 coarse fraction through the second outlet 11 and enter through the pipe 12 into the cooling unit 13, in which they are cooled to room temperature so that they can be transported further without great risk of secondary oxidation. to the place where they need to be recycled. The plant has an outlet of 14 cooled particles of spongy iron from the cooling unit 13. Charging of coal to the reactor is carried out through pipe 15.
    The discharging device 10 has in its lower part an outlet 16 for sponge iron particles, which is connected to the interior of the melter gasifier 1 through at least one vent pipe 17. The sponge iron particles are dispensed through the outlet 16. Thus, the melted gasifier 1 (reactor 1) with gas is supplied continuously or periodically required feed materials in an amount necessary for the melting process through the drain pipe 17. The amount of coal required to form and maintain the coal fluidized bed is fed into the melter gasifier 1 through the pipe 15 directly. The melting gasifier 1 can be divided into three zones, namely the lower zone 18, in which there is cast iron and slag, the middle zone 19 for the carbonized bed and the expansion
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    Renal upper zone 20, which serves as a stilling chamber. Sponge iron particles are supplied not at the upper boundary of the stilling chamber, but inside the stilling chamber near the upper boundary of the coal fluidized bed of zone 19. This is achieved in this case due to the fact that the downpipe 17 is deeply immersed in the stilling chamber of zone 20. Thus, significantly the amount of fine particulate fraction carried along with the gas is reduced. The most optimal depth of the downflow pipe 17 is simply determined experimentally. It is advisable when the vent pipe ends at a short distance above the upper boundary of the coal fluidized bed.
    The use of one or several vent pipes 17 allows, by changing the direction of these pipes at the lower end or by installing baffle sheets, to significantly reduce the vertical component of the velocity of the falling down material and thereby increase the residence time of sponge iron particles in the coal fluidized bed. Due to the high thermal loads of the drain pipe, which is immersed in the inner space of the melting reactor with gassing, it is advisable to cool the pipe.
    FIG. Figure 1 shows schematically trays 21 and 22 for discharging pig iron. Slags as well as a nozzle 23 for injecting oxygen-containing gas.
    (
    The resulting reducing gas is discharged through the outlet 24 at a temperature of about 1200 ° C. From there it is directed further along the line 25 of the reducing gas to the inlet 4 of the gas of the direct reduction unit 2. Since the reducing gas directed to the direct reduction unit 2 should not have a temperature exceeding 900 ° C, a cooling gas supplied through line 27 is added to the hot flow of the rising reducing gas through line 25 in place 26 to control the temperature. This cooled 1st gas is a flue gas returned back after it was cleaned and cooled in the flue gas scrubber 28 and after the CO absorber 29 in front of which the compressor 30 is installed to create the required pressure, the CO content was reduced. gas in this form could be mixed with hot reducing gas, but it was passed through a cooling unit 13 and, in direct heat exchange, interacting with spongy iron particles of a coarse-grained D1i, causes cooling These particles of spongy iron. In this heat exchange, the prepared top gas is heated to approximately 500 ° C. Then, along line 27 at site 26, it is added to the stream of hot reducing gas of line 25 in order to lower its temperature to a value below 900 ° C. In case more sponge iron should be produced in the installation than pig iron, some of the prepared The flue gas in a separate recuperator 31, connected in parallel to the cooling unit 13, is preheated in order to be able to set the desired gas temperature. As
    the heating gas must be used; 30 sheets 38 deviate almost to the uncharted top gas for the scrubber 28, which depends on the need
    warm. Due to this, it is also possible to avoid the enrichment of the circulating gas with inert components such as NJ. In order to be able to obtain sponge iron with a low sulfur content, the gas must be subjected to desulfurization in a hot gas desulfurization unit 32.
    To avoid the occurrence of sintering, it is necessary that the amount of hot gas flowing upward through the pipes 17.9 and 6 be kept low. This can be achieved by creating a high flow resistance in the area of the discharge device 10 - the discharge pipe 9 and the separator 7, when the discharge is controlled so that the pipe 9 is constantly at least partially filled with material. Thus, the resistance of the parallel path to the reducing gas line 25 is maintained at such a high level that along this parallel path
    no harmful gas streams can form.
    Due to the high thermal stress inside the melter gasifier 1, the vent pipe (FIG. 2) is equipped with liquid cooling. For this purpose, by means of three metal pipes 33-35, mounted concentrically relative to each other, a fluid channel is formed through which a cooling fluid, such as water, flows. The cooling system is covered on all sides with a refractory layer 36.
    In the lower part of the downpipe, protrusions 37 are installed in the form of a cascade, on which material can be deposited, which thereby serves as a protection against wear. Instead of these protrusions, or in addition to these protrusions, a baffle plate 38 may be provided at the lower outlet of the pipe, preferably in the shape of a truncated cone, similar to a Chinese head. The sponge iron particles falling down, by means of protrusions 37, are deflected in the pipe in the form of a meander and are braked and with the help of
    35
    40
    horizontal direction, as a result of which their vertical velocity components are markedly reduced. Melting gasifier 1 has a cover 39.
    Schematically shown in FIG. 3, the separator 7 is configured as an inclined drain chute 40 with at least one branch pipe 41 branching down from it.
    The flow from the top into the separator 7 bulk material stratifies during movement along the separator, thin
     the particles settle down, and the larger ones collect on the upper side. With an appropriate control of the removal of sponge iron particles of the fine fraction from the first pin-hole (| g STI 8 get the flow profile
    (fig.Z), i.e. the coarse parts of the sponge iron 1 are directed further along the downpipe 40, to the second outlet pipe 12 and are diverted from there. If the removal of sponge iron fine particles is controlled (Fig. 1) by means of an unloading device 10, which is connected to the separator 7 through a pipe, then the resistance to the flow of hot
    gas can be maintained at a relatively high level.
    In the schematic representation of the second form of installation (Fig. Details, corresponding to the details of the installation in Fig. 1, have the same conventions. The direct restoration unit, designed as a shaft furnace 2, has a restoration unit on top of the loading device 3 for dispersed iron ore and a gas outlet 5 for the used reducing gas (flue gas) and at the bottom of the discharge device 42, a gas inlet 4 for the hot reducing gas. The cover of the upper zone 20 serving as The calming zone has a chamber 43 which is connected to the stilling chamber. An orifice 44 is provided in the head of the reactor-gasifier to release a reducing gas (not 1 valuable gas) formed in the melter gasifier a gas inlet 45 for cleaned and prepared flue gas from the mine the direct reduction furnace and the inlet 46 for the inlet of the desulfurization agent. In addition, a pipe 15 for the supply of coal and a submersible pipe 17 for the delivery of a fine dispersed tube are passed through the lid of the filling gasifier 1 Noah fraction.
    In the lower part of the melter gasifier 1, trays 21 and 22 are provided for discharging liquid iron and liquid slags, then above the slag mirror at least one nozzle 23 or one burner 47 for injecting gases and fine-grained solids.
    Under the shaft furnace 2 direct reduction, there is a cooling unit 48 for hot sponge iron particles unloaded through the unloading device 42. The inlet 49 of the cooling unit 48 for the hot sponge iron particles is connected to the discharging device 42 via the outlet line 6. The line of the discharge pipe 6 has a level measuring device 50, by means of which the unloading device 42 is controlled.
    The cooling unit 48 in the upper part near the inlet 49 has an outlet 51 for cooling gas and in the lower part next to the outlet 14 for cooling sponge iron particles has an inlet 51 for cooling gas. Cooling takes place as in the embodiment according to FIG. 1 in countercurrent and in direct exchange with particles of sponge iron dipping in the cooling unit. Since not only sponge iron particles of the coarse-grained fraction (Fig. 1) are supplied to the cooling unit 48, it is advisable to provide a stilling chamber in the upper part of the cooling unit so that the removal of the fine fraction would be as small as possible. This can be, for example, achieved by the fact that the vent pipe 6 at a certain length enters the cooling unit so that above the bulk cone inside the cooling unit there is a calm-k
    The camera is good. I
    Below the cooling unit and connected to the inlet 14 by a drain pipe 50 is a sorting device 52, designed as a screening station, which separates the sponge iron particles. The outlet 8 for the fine fraction is connected to the device to the fine fraction mounted above the melting reactor 1 with gas, the outlet 16 of which is connected to the discharge pipe 17. It is also possible to connect to the pipe 15 through which the coal is fed into the melting reactor 1 with gasation. If the sorting device 52 is not installed above the melting reactor 1 and the pipe 9 cannot be designed as a drain pipe, appropriate supply of 1e means for the fine fraction should be provided in this pipe. If the separation in the sorting device 52 is carried out so that the fine fraction contains only particles with a grain size of not more than 3 mm, then it may be appropriate to at least part of this fraction be blown into the melting reactor 1 through nozzles 23 or 47. Then suitable pipelines to the nozzles are provided.
    9
    With the outlet 11 of the sorting device 52 for the coarse-grained fraction, which is withdrawn from this process, a pipe 12 is connected, through which the coarse fraction can be led to a special Kli melting unit to a device for compacting, passivating, or also another cooling unit 13, to which prepared top gas is supplied as a coolant.
    As in the exemplary embodiment of FIG. 1 The flue gas scrubber 28 is connected to the flue gas outlet 5 of the shaft furnace for direct reduction and the flue gas 53 of the flue gas scavenger 28, connected via CO and 55 pipelines to the CO absorber 29, the outlet of which 24 is gas through lines 56 and 57 - connected to the inlet 51 for the cooling unit 48. In addition, as in the first embodiment, there is a pipe 27 from the outlet 51 of the gas of the cooling unit 48 to the reducing gas line 25, to mix with the gas flow the reducing gas flowing along this line to the gas inlet 4 of the shaft furnace 2 is directly reduced, prepared and heated in the cooling unit 48 of the top gas. This not only makes it possible to regulate
    The temperature of the reducing gas supplied to the shaft furnace 2 is directly reduced, but the consumption of coal and oxygen in the melting reactor 1 can also be reduced with gasation almost
    half. As a result, the amount of sulfur introduced with the coal and the sulfur content in the reducing gas are also reduced by about half.
    The cooling unit 48 (Fig. 4) is provided with a cooling gas circulation circuit 58 comprising a pipeline 57, a cooling gas purifier 59 and a compressor 60. For cooling in a cooling unit, a larger amount of cooling gas is required than is available prepared and supplied through pipeline 56 top gas.
    1335410
    Pipeline 27, which is connected to the gas outlet 51 of the cooling unit and to the circulation loop 58 of gas cooling 5, leads to pipe 61 to inlet 45 in the gasifier head of the chamber 43, in which connecting line 62 ends to pipe 63 of the tower CO - Absorbent sorbent 29. A prepared blast furnace gas of various temperatures can be supplied via pipeline 61 to the head of the gasifier of chamber 43, so that the optimum temperature can be set here for the desulfurization of hot gas.
    The outlet 44 in the head of the gasifier of the reducing gas chamber 43 obtained in the melting reactor 1 is connected via a pipe 63 to the cyclone 64. The gas outlet 65 is connected to the reducing gas line 25, which is connected to the shaft furnace unit 2.
     Instead of one cyclone, several cyclones can also be used, connected together in a cyclone battery. The outlet 66 for the separated solids is connected via a pipe 30 to the pipe 67 with a pipe 68, which is connected through a compressor 30 to the pipe 54 of the flue gas 28. Pipeline 68 supplies part of the effluent from the purifier.
    35 of the flue gas 28 to the burner 47 as an oxygen-containing gas, while this gas simultaneously serves as the carrier gas of the separated solids of the cyclone 64. Go to valve 40 and the nozzles 23, in addition, oxygen can be supplied through the pipeline 69. The branch line 70 from the pipe 54 connecting to the gas outlet 53 of the cleaned top gas 28 leads to the steam generator 71. Part of the unprepared flue gas can thus be used as gas fuel to form steam, which is used in the COj tower, the -absorber 29.
    In the method carried out with the installation (FIG. 4), in addition to avoiding the release of an excess amount of reducing gas formed in the melting reactor 1 with gassing, the flow rate at which it is maintained is taken into account
    and
    the low level of sulfur content in the pig iron smelted in the melting reactor and recovered from the process is a coarse fraction of sponge iron particles, when coal with a high sulfur content is used as energy carrier. To this end, measures are envisaged to reduce the proportion of energy, three months.
    A means for maintaining combustion and part of the flue gas or, rather, the mixture of flue gas with dust is combusted. The amount of top gas supplied through line 68 must be chosen so that, in connection with other measures for temperature control, the temperature of the gasifier head will be
    melt fine / O between 850 and 1250 C, preferably
    . By the possible use of flue gas as an oxygen carrier for gasification, it is natural that
    fraction in the melting reactor 1 so that the top gas from the shaft furnace is partially unprepared.
    partially after purification from CO and after direct heat exchange in a cooling unit, introduce into the process for sponge iron particles discharged from the direct reduction unit. An integral part of the energy needed to melt the coal produced by burning is reduced due to the fact that, when separating particles of sponge iron in the sorting device 52, the proportion of tonnes is. the particulate fraction is reduced with respect to the coarse grain, i.e. The granularity range of the fine fraction fed to the melting reactor 1 is reduced to a particle size of up to 5 mm, preferably up to 3 mm. These particles, due to the longer residence time in the fluidized bed of the melting reactor with gassing, melt with a significantly lower energy expenditure, i.e. with less coal and with less sulfur. Then it is also possible to use part of the flue gas supplied from the purifier 28, unprepared flue gas, which contains carbon dioxide and water vapor, to use coal for gasification. A portion of the flue gas (Fig. 4) is fed via line 66 to one or more burners 47 of the melting reactor 1, which exit to the fluidized bed. Using a coke gas as a carrier, the material also extracted from the cyclone 54, namely particles of coal and desulfurizing agent extracted from the reducing gas, is returned back to the smelting reactor 1. In order to prevent the ventilation openings from slagging and save them free, to the burner, through line 69, oxygen or air is supplied, the oxygen consumption per ton of product is also reduced, and this increases the efficiency of the process.
    A further saving of coal and a decrease in the sulfur content in the reducing gas and in the spongy iron is achieved by the fact that in the tower CO-absorber the prepared top gas is mixed with the reducing gas. This happens, (Fig. 4)
    25 in such a way that part of the top gas prepared in the tower CO absorber 29 through pipelines 54 and 57 is passed through a cooling unit 48, this part is heated in direct contact with hot sponge iron particles and then again part of it is supplied to the line 25 reducing gas and further part of the pipeline 61
    35 is supplied to the head of the gasifier 43 Another part of the prepared top gas produced by the absorber tower is supplied directly via line 62 and part of pipe 40 to pipe 43 of the gasifier. With the help of a certain amount of prepared flue gas mixed with the reducing gas, the consumption of coal and oxygen, the amount of sulfur introduced with the coal, and the sulfur content in the reducing gas are reduced by about half.
    Temperature control is also carried out using the prepared top gas supplied via pipe 50 to wire 61 of the gasifier 43, and the temperature in line 61 can be set from 55 by the ratio of the amount fed through pipe 27 and pipe 62. The temperature setting in the gasifier head has a significant meaning especially tog1335412
    A means for maintaining combustion and part of the flue gas or, rather, the mixture of flue gas with dust is combusted. The amount of top gas supplied through line 68 must be chosen so that, in connection with other measures for temperature control, the temperature of the gasifier head will be
    . By the possible use of flue gas as an oxygen carrier for gasification, it is natural that
    Oxygen consumption per ton of product is also consumed, and this increases the efficiency of the process.
    A further saving of coal and a decrease in the sulfur content in the reducing gas and in the spongy iron is achieved by the fact that in the tower CO-absorber the prepared top gas is mixed with the reducing gas. This happens, (Fig. 4)
    5 in such a way that part of the top gas prepared in the tower CO absorber 29 through pipelines 54 and 57 is passed through a cooling unit 48, this part is heated in direct contact with hot sponge iron particles and then again part of it is supplied to the line 25 reducing gas and further part of the pipeline 61
    5 is supplied to the gasifier head 43. Another part of the prepared top gas produced by the absorber tower is supplied directly via line 62 and part of the pipe 61 to the head 43 of the gasifier. With the help of a certain amount of the prepared top gas mixed with the reducing gas, the consumption of coal and oxygen, the amount of sulfur introduced together with the coal, and the sulfur content in the reducing gas are reduced by about half.
    Temperature control is also carried out using the prepared top gas supplied via pipe 61 to the head of the gasifier 43, and the temperature in line 61 can be set from 5 to the ratio of the amount fed through pipe 27 and pipe 62. The temperature setting in the gasifier head has a significant meaning especially tog131
    yes, when the desulfurization agent is supplied to it or to the off-gas line 63 in order to further reduce the sulfur content. The optimum temperature for the desulfurization of hot gas is about 900 ° C. With the proposed method, a desulfurizing agent is introduced into the head of the gasifier 43 through the opening 46, for example calcium hydroxide in finely dispersed form, and the optimum temperature for the desulfurization of the hot gas is set using a prepared pulp gas injected through the inlet, 45 gas. The desactivation of the reducing gas takes place mainly in the head of the gasifier and in line 63 of the exhaust gas. The used and unused desulfurization agent is separated in a cyclone 64. and via line 67 is returned back to the smelting reactor 1 with gassing.
    权利要求:
    Claims (14)
    [1]
    Invention Formula
    one . A method of reducing dispersed iron ore into sponge iron followed by remelting into cast iron, including the reduction of ore in a shaft furnace with a countercurrent heated 1 m reducing gas coming from the smelter and charging the sponge iron into the melter gasifier, burning coal in a fluidized bed, melting sponge iron, production of hot reducing gas, cooling of -gas to the temperature of reduction, cleaning, dust collecting, recirculation, supply to the shaft, furnace and lower part of gasification pa, and w differing with the fact that, in order to increase performance, the sponge iron particles exiting of the shaft furnace is divided by a fine 20 mm -and a coarse fraction and a fine fraction is fed to the melter gasifier.
    2. A method according to claim 1, characterized in that the amount of melted sponge iron particles of the fine fraction is set such that the amount of reducing gas formed during their melting corresponds to the amount needed to reduce all ore fractions, and this amount
    [2]
    4-14
    accounts for at least 20% of all sponge iron particles.
    3. The method according to claim 1, characterized in that the division into
    [3]
    the fractions are produced in such a way that the average sulfur content in the fine. the fraction corresponds to five to ten times the average sulfur content of the coarse-grained fraction.
    4. A method according to claim 1, characterized in that a desulfurizing agent is introduced into the gas produced in the melter gasifier,
    [4]
    5. Method according to paragraphs. 1-4, of which is due to the fact that the means
    [5]
    for desulfurization, it is fed to the head and / or to the gas outlet pipe of the melting gasifier.
    6. Method according to paragraphs. 1-5, that is, in that a portion of the top gas of the shaft furnace is mixed into the reducing gas obtained in the smelting gasifier after it has been washed, cooled and carbon dioxide has been removed.
    [6]
    7. Method of pop 6, characterized in that at least part of the washed and purified top gas is heated by sponge iron particles leaving the shaft furnace, and then introduced into the reducing gas.
    [7]
    8. The method according to claim 7, characterized in that the separation
    [8]
    Particles into fine and coarse fractions are produced after direct heat exchange with purified flue gas.
    9. Method according to paragraphs. 1-8, about ti and - h and y and with the fact that, as a wearer of oxygen or gasification means, a part of the top gas is introduced into the melting gasifier after washing and cooling.
    [9]
    10. Method by. 1-9, of which it is due to the fact that the dust collected in the cyclone is blown into the melting gasifier with the help of flue gas.
    [10]
    11. The method according to paragraphs. 1-10, about a t of l and h. And y and i with the fact that the dust collected in the cyclone is blown into the melting gasifier with top gas with air or oxygen mixed with it, at least one burner and partially burned or gasify.
    [11]
    12. Installation for reduction of dispersed iron ore into sponge iron, followed by remelting into cast iron, containing a shaft furnace with loading and unloading material, supplying and discharging reducing gas, located below its melting gasifier, piped through an intermediate tank with a shaft furnace, gasifier nodes for supplying sponge iron, coal and additives, gas production units, pig iron and slag, gas and fine gas injection nozzles, substances, piping system and recycling units and cleaning and cooling the waste gases, valves, cyclone and compressors, characterized in that it is equipped with a particle size separator and a coarse fraction processing unit, while the fraction separator is located between the discharge furnace of the shaft furnace and the melter gasifier and is filled with pipelines, connecting it with a melting gasifier and with a coarse-grain processing unit made in the form of a melting vessel, units for hot compaction, passivation or cooling.
    [12]
    13. The installation according to claim 12, about tl and - so that the particle size separator is made in the form of an inclined tray with waste
    [13]
    at least one nozzle for metered separation of fine particles.
    14. Installation according to claim 12, characterized in that the separator of supplies with a sieve or grate of heat-resistant material up to 800 C.
    [14]
    t5. Installation under item 14, the difference is that the sieve or lattice is connected to a vibrator.
    O
    five
    16. Installation on PP. 12-15, which is associated with the fact that the outlet of the metered-dose branch pipe of the fine fraction is connected by at least one discharge pipe to a melter gasifier.
    17. Installation by paragraphs. 12-14, which means that the discharge pipe for the material is provided inside with protrusions in the form of a successive cascade of steps and / or a baffle plate.
    18. Installation according to claim 17, which is described in that the baffle wall is made in the form of a truncated cone.
    19. Installation on PP. 12-15j is related to the fact that it is equipped with a refrigeration unit, located downstream of the shaft kiln unloading unit, with a pre-separator of fractions with input and output units of sponge iron and cooling gas from the recirculation circuit.
    20. Installation on PP. 12-16. It is due to the fact that the cooling gas inlet of the refrigeration unit is connected to the CO purification unit,
    and the outlet is connected to the gas supply or gas outlet opening in the melter gasifier.
    21. Installation on PP. 12-17, which means that the outlet for solid particles of the cyclone is connected to the pipeline of the recirculating circuit cleaning unit and to the lower gas supply nozzle
    0 melting gasifier.
    Priority on items 15.11.82 - on PP. 1, 2, 6, 7, 10,
    11, 12, 13, 14, 15; 5 08/15/83 - on PP. 3, 4, 5, 8, 9, 16, 17, 18.
    0
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    U2i
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    同族专利:
    公开号 | 公开日
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    DE3328373A1|1984-05-17|
    CA1215842A|1986-12-30|
    PL244563A1|1984-07-30|
    EP0111176A1|1984-06-20|
    BR8306264A|1984-06-19|
    AT19658T|1986-05-15|
    PL142647B1|1987-11-30|
    US4543123A|1985-09-24|
    US4542889A|1985-09-24|
    AU569481B2|1988-02-04|
    ES527233A0|1984-08-01|
    DD210310A5|1984-06-06|
    AU2089683A|1984-05-24|
    ES8406554A1|1984-08-01|
    DE3363431D1|1986-06-12|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US1353716A|1916-10-05|1920-09-21|Charles S Bradley|Production of iron and steel|
    US2747988A|1951-04-23|1956-05-29|Kenneth R Marsden|Method for the recovery of pure iron oxide and iron from oxidic iron ores|
    BE642457A|1963-12-23|
    US3199974A|1964-05-25|1965-08-10|Hydrocarbon Research Inc|Fluidized iron ore reduction process for production of iron powder|
    DE2401540B2|1974-01-14|1975-11-13|Fried. Krupp Gmbh, 4300 Essen|Method for melting sponge iron|
    DE2401909C3|1974-01-16|1985-06-27|Fried. Krupp Gmbh, 4300 Essen|Process for the production of steel|
    US4094665A|1977-05-13|1978-06-13|Stora Kopparbergs Bergslags Ab|Method for simultaneous combined production of electrical energy and crude iron|
    DE2905339A1|1979-02-13|1980-08-21|Metallgesellschaft Ag|METHOD FOR PRODUCING STEEL|
    US4316739A|1979-07-16|1982-02-23|Midrex Corporation|Method for producing molten iron|
    US4248626A|1979-07-16|1981-02-03|Midrex Corporation|Method for producing molten iron from iron oxide with coal and oxygen|
    US4304597A|1980-03-20|1981-12-08|The Direct Reduction Corporation|System for control of sinter formation in iron oxide reducing kilns|
    CA1125505A|1980-05-09|1982-06-15|William E. Creswick|Fabricated tuyere|
    US4436551A|1981-10-26|1984-03-13|Sumitomo Heavy Industries, Ltd.|Process for making steel from direct-reduced iron|
    US4412858A|1982-07-12|1983-11-01|Hylsa, S.A.|Method of converting iron ore into molten iron|DE3438487C2|1984-10-17|1987-10-15|Korf Engineering Gmbh, 4000 Duesseldorf, De|
    AT381116B|1984-11-15|1986-08-25|Voest Alpine Ag|METHOD FOR THE PRODUCTION OF LIQUID PIPE IRON OR STEEL PRE-PRODUCTS AND DEVICE FOR IMPLEMENTING THE METHOD|
    SU1479006A3|1984-11-26|1989-05-07|Фоест-Альпине |Method of producing molten iron or steel products and reducing gas in melting gasifier|
    DE3503493C2|1985-01-31|1987-10-22|Korf Engineering Gmbh, 4000 Duesseldorf, De|
    DE3504346C2|1985-02-06|1986-11-27|Korf Engineering GmbH, 4000 Düsseldorf|Method and device for the production of sponge iron particles and liquid pig iron|
    US4685964A|1985-10-03|1987-08-11|Midrex International B.V. Rotterdam|Method and apparatus for producing molten iron using coal|
    DE3603894C2|1986-02-05|1993-03-18|Deutsche Voest-Alpine Industrieanlagenbau Gmbh, 4000 Duesseldorf, De|
    DE3785851D1|1987-02-16|1993-06-17|Moskovskij Institut Stali I Splavov, Moskau/Moskva, Ru|
    AU596758B2|1987-11-13|1990-05-10|Jp Steel Plantech Co.|Metal-making apparatus involving the smelting reduction of metallic oxides|
    US4981628A|1988-10-11|1991-01-01|Sudamet, Ltd.|Repairing refractory linings of vessels used to smelt or refine copper or nickel|
    AT390622B|1988-10-25|1990-06-11|Voest Alpine Ind Anlagen|METHOD AND INSTALLATION FOR THE PRODUCTION OF LIQUID PIG IRON|
    AT394201B|1989-02-16|1992-02-25|Voest Alpine Ind Anlagen|METHOD FOR GENERATING COMBUSTIBLE GASES IN A MELT-UP CARBURETTOR|
    DE4037977C2|1990-11-29|1992-09-24|Deutsche Voest-Alpine Industrieanlagenbau Gmbh, 4000 Duesseldorf, De|
    US5320676A|1992-10-06|1994-06-14|Bechtel Group, Inc.|Low slag iron making process with injecting coolant|
    US6197088B1|1992-10-06|2001-03-06|Bechtel Group, Inc.|Producing liquid iron having a low sulfur content|
    US5397376A|1992-10-06|1995-03-14|Bechtel Group, Inc.|Method of providing fuel for an iron making process|
    US5354356A|1992-10-06|1994-10-11|Bechtel Group Inc.|Method of providing fuel for an iron making process|
    AT402506B|1993-01-26|1997-06-25|Holderbank Financ Glarus|METHOD FOR THE PRODUCTION OF RAW IRON AND CEMENT CLINKER|
    US5958107A|1993-12-15|1999-09-28|Bechtel Croup, Inc.|Shift conversion for the preparation of reducing gas|
    AT406483B|1995-07-19|2000-05-25|Voest Alpine Ind Anlagen|METHOD FOR THE PRODUCTION OF LIQUID PIPE IRON OR STEEL PRE-PRODUCTS AND SYSTEM FOR IMPLEMENTING THE METHOD|
    AT406480B8|1995-07-19|2000-07-25|Voest Alpine Ind Anlagen|METHOD FOR THE PRODUCTION OF LIQUID PIPE IRON OR STEEL PRE-PRODUCTS AND SYSTEM FOR IMPLEMENTING THE METHOD|
    AT406482B|1995-07-19|2000-05-25|Voest Alpine Ind Anlagen|METHOD FOR THE PRODUCTION OF LIQUID PIPE IRON OR STEEL PRE-PRODUCTS AND SYSTEM FOR IMPLEMENTING THE METHOD|
    AT403381B|1996-06-10|1998-01-26|Voest Alpine Ind Anlagen|METHOD AND SYSTEM FOR CHARGING METAL CARRIERS IN A MELTING GASIFICATION ZONE|
    AT403696B|1996-06-20|1998-04-27|Voest Alpine Ind Anlagen|MELTING CARBURETTOR AND SYSTEM FOR THE PRODUCTION OF A METAL MELT|
    AT403930B|1996-07-11|1998-06-25|Voest Alpine Ind Anlagen|METHOD FOR CHARGING METAL CARRIERS IN A MELTING-GASIFICATION ZONE AND SYSTEM FOR IMPLEMENTING THE METHOD|
    AT404022B|1996-11-08|1998-07-27|Voest Alpine Ind Anlagen|METHOD AND INSTALLATION FOR THE PRODUCTION OF LIQUID PIPE IRON OR STEEL PRE-PRODUCTS FROM IRON-CONTAINING MATERIAL|
    AT404362B|1996-12-17|1998-11-25|Voest Alpine Ind Anlagen|METHOD AND MELTING CARBURETOR FOR PRODUCING LIQUID METAL|
    AT510586B1|2011-05-12|2012-05-15|Siemens Vai Metals Tech Gmbh|METHOD AND DEVICE FOR DISPERSING DUST PARTICLES FROM A DUST LINE|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE3242232|1982-11-15|
    DE19833328373|DE3328373A1|1982-11-15|1983-08-05|METHOD AND SYSTEM FOR THE DIRECT PRODUCTION OF SPONGE IRON PARTICLES AND LIQUID PIPE IRON FROM PIECE IRON ORE|
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