DE1433327A1 - Method of introducing solid material into a reaction zone such as a blast furnace - Google Patents

Description

DfM-Ckei ».

DR. ILSE RUCH of Munich PATENT Attorney RefcfcenlwAtlwlt VI « T «kfr« mnu * wti ΡΛ «" 1433327

Dr. Expl.

A 69 442
2/3/1

H / P

The M.W. Kellogg Company "New York. H.l .. USA

Method for introducing solid material into a reaction zone, for example a blast furnace

The invention relates to a method for introducing solid material into a heating zone and in particular for supplying finely divided solids, including sponge iron, ore concentrate, flux and carbonaceous material, into the rest or the melting chamber of a blast furnace. In particular, the invention relates to a method and a device for the production of dry powdery carbonaceous material and feeding this material to a hoof furnace at the level of the Y / ind nozzles.

As is well known, a blast furnace is made with refractory bricks The masonry manhole is kept permanently filled by pouring egg-containing material, flux, usually limestone, on top

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or dolomite, and carbonaceous solids, usually coke. The upper part of the furnace above the haste is the shaft into which the raw materials are introduced and in which they are prepared for melting by removing volatile material, heating the non-volatile material to elevated temperature, including melting temperature, and iron oxide by forming in the blast furnace, carbon monoxide flowing upwards is reduced. The lower part of the blast furnace includes the rest with the smelting room, in which the materials that have been prepared and sink through the shaft melt as slag and the slag-forming components separate from the iron-forming components. The coke introduced above serves as fuel for heating the Mass and is converted into a reducing agent, "by which metal oxides are reduced to metal. Ore and slag-forming constituents must be ^{heated to a temperature above about 538 °} C. so that the calcination of the ore and the extraction of the metal is possible, and this heating, takes place by burning coke with a hot blast, ie hot air, which is blown in through tuyeres in the upper part of the melting chamber. The exothermic reaction of carbon with oxygen produces carbon dioxide, which practically momentarily forms the carbon monoxide acting as a reducing agent with incandescent coke these implementations

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a total of about 3970 B.T.U. per pound of carbon consumed get free.

The present invention relates generally to the arrangement of a distribution zone or a distribution container or several such zones or containers for powdery solids carbonaceous material in a blast furnace as well as suitable control means to automatically ensure a constant supply of ensure finely distributed carbonaceous solids in these vessels and the blast furnace, regardless of the speed the supply of pesticides to the furnace at the prevailing pressures. the arrangement of at least one large, pressurized collection container for finely divided or powdered carbonaceous material downstream of one of the Grinding and drying section of the process that isolates this section against fluctuations in the blast furnace and, if necessary, carbonaceous pestilence to those described above Distribution hopper supplies, and a control system through which automatically the carbonaceous pests of a number of Inlet in the melting space are fed and distributed so that the feed rate of the solids through each inlet varies arbitrarily and independently of the other inlets or the flow rate through each Inlet kept the same, i.e. without differences between the individual inlets or the flow speed duroh

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one or more feed nozzles can be varied as required, while the total coal feed is kept constant.

The ratio of the fuel introduced into the furnace of a blast furnace to the savings in coke charge results from the condition. That a maximum adiabatic flame temperature, which is experimentally as has proven desirable to operate, maintain * As is well known for utilizing elevated Y / indtemperaturen above about 1300 or HOO ⁰ I ¹ vapor or a fuel, such as oil or Natijugas in the East of a blast furnace so that adiabatic temperatures in the range of about 3000 to about 400O ⁰ P, usually about 3300 ⁰ P to about 350O ⁰ P, are obtained. Purely a certain increase in. ' Wind temperature, the amount of a certain fuel to be introduced depends partly on its preheating, but for the most part on the heat required for the endothermic conversion of the fuel to hydrogen and carbon monoxide. It was found, however, that for the same reduction in coke feed rate, the direct introduction of a preheated fuel such as preheated coal particulates enabled either a lower wind temperature to be used or a significantly reduced amount of coal particulates to be used

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The present invention therefore relates to a method and a device for the direct introduction of either relatively cool or preheated finely divided powdered carbonaceous solid material in the rest of a blast furnace.

According to the present invention, solid carbonaceous material such as lignite (soft coal), bituminous coal or coke is prepared by crushing it to a particle size below 1/8 inch, e.g. below 16 mesh and the crushed carbonaceous material to a moisture content below about 3% by weight, and preferably not substantially above about 1 % by weight, dries. The dried and crushed carbonaceous material having a particle size suitable for a fluidized bed in the range of about 1.7 to about 1000 / u, with preferably at least about 12 $ having a particle size of less than about 75 / u, is treated with a suitable drying gas in transferred to one or more relatively large primary cyclone separators in order to separate and recover the powdery carbonaceous solid particles from the gaseous carrier or suspension medium. The gaseous material drawn off by the primary cyclone separator, which contains entrained carbonaceous fine or dust particles, can be further freed of solid particles in a suitable separator, so that a great deal of further dust is obtained from this gaseous material

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will. The separated dust can at a given time be combined with the powdery solids separated in the primary cyclone. The carbonaceous material separated in the primary cyclone is fed to a collecting container, from which it is transferred through a series of pressure-building containers and transfer lines through which the i ^l est3toi ^v fe from a zone of relatively low pressure of around atmospheric pressure to a zone of higher pressure can be directed. Suitably, the pressure-building zones are arranged to each other _f that the solids pass through their own weight of one to the next, as shown in the drawings. If necessary, however, a different arrangement can also be selected. ■

The pressurized receptacle is sized to have a holding capacity for pesticides in the area

from about 10 minutes to about an hour. That under Pressurized finely divided solid carbonaceous material can be adequately ventilated to keep it in a flowable state to hold, or it can be kept in the containers described here in a tight swirling state, that a dry fluidizing gas is passed upwards will. In the method of the invention, the pressurized container, which is described in more detail below,

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be kept at practically atmospheric temperature or at a considerably higher temperature. That is, if it is desired to supply the rest of the still furnace with relatively cool powdery colloidal material, this pressurized container is kept at practically atmospheric temperature or some other relatively low temperature. The carbonaceous solids can also be fed to the touch of the perforated furnace in a preheated state. The preheating of the solids to a desired temperature in the range from about 1100 to about 1600 ⁰ F can take place partially or completely in the pressurized collecting drum, for example by a separately introduced fuel or part of the pulverulent carbonaceous material in this container with a gas containing acid is burned, while the solids are kept in the state of a relatively dense fluidized bed, such as in fluidized bed coking.

The pressurized collection container described above is provided with means for drawing off solids therefrom, preferably a number of solids discharge lines or standpipes, which may or may not be ventilated and extend downward enough to be ventilated Control of the solids flow provided in it to be v / grounded. If relatively short exhaust lines

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are used, generally only back pressure or ventilation air is required for the valves. The valves control the flow of solids through these lines, and from their bottom into a transfer line that connects to a Distributor tank is connected to the blast furnace. This distribution container can be on the upper or the lower part of the blast furnace. According to this, the coal released from the pressurized collecting container will be Solid particles combined under elevated pressure with a suitable dry gaseous material to form a suspension which then via a transfer line into a distribution container which, at a desired pressure in the range of about 5 psig to about 100 psig, and preferably above the pressure in the furnace chamber will. If more than one, for example four, manifold tanks are used, then lead from the one under pressure standing collection container from the same number of transfer lines, so that each of the distribution container for itself is charged with pressurized powdery carbonaceous material through its own supply line. According to the invention however, several pressurized collection containers can also be used to supply four or more distribution containers be used. The manifold tanks used in the method of the invention will be sufficient ventilated to keep the carbonaceous material in it in

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swirling or flowing state, and everyone The upper part of the distribution tank is equipped with one or more cyclone absorbers in which the in these containers introduced gaseous material powdery Solid particles are separated and recovered.

Each manifold container is maintained under sufficient pressure to release the carbonaceous material therein with a admit one or more solids at the desired rate into the hurry of the blast furnace, regardless of the pressure in it. In addition, each is the distribution container with one or more, preferably several drainage lines, which can be short or long, and, for example, ventilated or non-ventilated, downwardly extending standpipes are provided. Any of these Discharge lines is then a separate supply source of powdery solid carbonaceous material for a single one Inlet to the furnace. I.e. any solids inlet or each inlet lance is controlled by its own flow of finely divided solids from a distribution tank flows down, supplies. In a blast furnace with 16 tuyeres are arranged, for example, four distributor tanks, and from each of these distributor tanks are in four lines withdrawn four separate portions of solids, so that the tuyeres of the Hoohofens each for itself

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are supplied with solids at a controlled rate. The one leading down from a distribution container Discharge line or the discharge lines can be suitable, in vertically spaced inlets for gaseous aeration material require in order to be located therein To keep solids in the desired swirling state. Preferably, according to the method of the invention however, relatively short vent lines are used, the length of which is just sufficient to provide the required flow control to enable. Therefore, the pressure of the dilute phase above the bed of solids in the vessels becomes preferred above the pressure of the solids flow under the valve or held at the point of contact with the gaseous material forming the suspension. ■

In the method of the invention, the finely moored carbonaceous material is introduced into the blast furnace through a lance or an inlet tube, which can be, for example, a carbon steel tube of suitable dimensions, through the Y / ind nozzle an alloy that is heat-resistant up to 1800 ^° F. or above, with this arrangement, a small amount of a cooling medium, such as air, is introduced between the protective sheath and the insertion tube to reduce a

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To prevent overheating of the latter, as when feeding Lignite turns out to be in the event of overheating of the -3 Linleitungsrohres coke would form in the ear. This 1 problem can, however hardly occur if powdery anthracite or powdery coke is supplied. However, in order to prevent the formation of locomotives in the Iiohr, means can be provided to pass an abrasive like -> and through which the The wall of the supply pipe is rubbed off and any J ^ oks formed thereon is removed. In addition, each feed tube n: it can be provided with a removable square tube so that it if necessary can be exchanged and arbitrarily individual feed tube can be replaced without the normal operation of the blast furnace must be interrupted. In this case, however, the supply area is not necessarily part of the V.ind nozzle, but can also be used in addition to the wind nozzle be introduced into the blast furnace.

In the procedure and the order of procedural stages according to the invention, the total amount of solid carbonaceous material introduced into the blast furnace at the height of the tuyeres v / ird by means of a loading scale in an initial position of the procedure. The drying, grinding and pressure build-up can, because the barely at the blast furnace is limited, in places that are quite far from the blast furnace, which is from the Üliandpunkt of the safety

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lieit means a special advantage. Against lingering however, since the solids in the whole process, there is inevitably a considerable amount of time between adjustments the loading scale and the time at which this Eire division takes effect on the tuyere of the blast furnace will. Therefore a practically instantaneous supply and control of the carbonaceous material actually introduced into the blast furnace r / u are the distribution containers on the blast furnace Equipped with level control devices that automatically dispense powdered solid icaterial at such speed Remove from the pressurized collection container that a desired!. "close to solid particles introduced into them and regardless of the actual feed speed required of solid particles is available in the blast furnace.

As mentioned, οas is in a blast furnace with for example 16 Vinci nozzles inject powdery carbonaceous oil through it single solid] eitungeii with or without a suspension-forming gaseous aüerial introduced, wooei the pulverized Coal is put under such a pressure that they are introduced from the blast furnace against the iücl.druck can. The plant is constructed in such a way, and equipped with appropriate means, that diaphragm shafts come out of the blast furnace be collected and a sufficient safety

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area, is provided that a desired supply of powdery solid particles is maintained. I.e. through . corresponding arrangement and interconnection of pressure controlled means in the method and apparatus of FIG Invention is the desired flow of particulate matter in the discharge lines, from which they are transferred through transfer lines are conveyed into the feed pipes for solid particles at the blast furnace. The solid particles can be introduced into the blast furnace in a relatively dilute or in a relatively dense phase. When the particulate matter is introduced in a dilute phase, the powdery carbonaceous material changes from a suitable gaseous one Material was taken up in this with the formation of a suspension and passed through the transfer line directly to the em Feed pipe passed. With this arrangement, the The density of the suspension can be varied between about 16 and about 192 kg / m by changing the volume of gaseous material and / or of solids that are introduced into the transfer line is appropriately sized, wherein the only condition is that the ratio of gaseous material to solids and the velocities are such that the suspension flows through the transfer line. That of the introduction of the carbonaceous residual particles in The system serving the dilute phase can, however, easily lead to a supply of the coal particles in a dense phase to the supply

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support pipes can be adjusted by the diluted phase in a small one placed above each feed tube Cyclone is passed and the dip tube of the cyclone is used to remove carbonaceous solid particles in dense phase downwards directly to the feed pipe.

In any of these arrangements, it is important to build up the pressure in the system so that the powdery coal particles, independently of pressure waves occurring in the blast furnace, at a desired speed through the supply pipes to be introduced.

Therefore, the solid particles in each flow from a distribution container down the line, as mentioned above

Flow valves, such as slide valves, or other suitable suitable / flow regulators. From the discharge line, the coal particles are discharged together with a suitable gaseous material in the form of a suspension into a transfer line which leads to the corresponding pesticide supply pipe. The gaseous material or compressible flowable medium that is used to form the suspension mi / c the finely divided carbonaceous material is under a desired pressure and in an i-ienge, which is controlled by pressure-responsive flow regulators that automatically changes the absolute pressure at the distribution container compensate, controlled, supplied, so that in these over-

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guide lines also with pressure changes in it and at the tuyeres or the supply pipes of the Iiochofen certain desired gas velocities in the range of about 1.5-30 m / 'süc and preferably about 9-12 m / sec are maintained, provided that this pressure is in the range of about 0.35 to about 7 atm. In the method and apparatus of the invention, the pressure drop through the solids flow control valves in each vent is maintained at a relatively low level, in the range of about 0.21 to about 0.42 kg / cm, in order to largely prevent erosion of the valves prevent and in order to ensure that the valves compensate for relatively small pressure differences between the individual transfer lines used in the process. In order that the pressure drop 12a of the valves can be kept within a certain desired range, a constant pressure difference between the inlet duct at the blast furnace and the vertical container is maintained by differential pressure in the system, which ensures that the pressure drop is maintained "sreglerventil for J ^(left and erosions are largely eliminated in each Strömun ^I esLötoffe in the desired range.

The gaseous niateriaü that is used to make the fine vertoi] fen koJiligen J''eotstojfe and in the

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To convey a suspension through the transfer lines is dimensioned by automatic control devices so that a desired amount of gas is kept in the transfer line at a practically constant speed, this speed being independent of the pressure prevailing in the wind tunnel or at the tuyeres of the blast furnace , is sufficiently low to prevent undesirable erosion.For this purpose, the gaseous fluidizing medium or compressible flowable material is initially placed under a pressure which is greater than the maximum pressure occurring in the process, and then the amount of this medium supplied to the process is Basic formula V = ^ - dimensioned accordingly, where "V" is the volume of the gaseous material, "W" is the flow rate of the gas in weight and "D ¹ ^ is the density of the gaseous material. When this designation is used for the method of the invention, the Flow velocity of the gas in weight " W "is changed in accordance with the absolute pressure in a direction which coincides with the changes in density due to changes in the absolute pressure, so that the ratio between the two is constant and therefore the volume of gas allotted to the system is constant. Thus, a weight flow meter which is used to automatically control the flow of the gaseous material is pressure compensated so that it

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directly corresponding to the measured absolute pressure and accordingly proportional to the density works in such a way that the ratio W / D and thus also the gas volume remains constant. By This control of the gas volume also becomes necessary for the flow rate of the gas in the transfer line controlled, since its given cross-sectional area remains constant «

The gaseous used for the process of the invention Material or compressible flowable medium can be preheated or not preheated air or a regarding the combustion of the carbonaceous solids be inert gaseous material · Except the use of gaseous products of combustion or a gaseous material with less than about $ 12 oxygen content should be considered

The method and device of the invention are not necessarily limited to use on a blast furnace, but can also with a cupola or any Process in which a furnace is passed through several solids inlets with finely divided solid material such as ore concentrate, Dewlap iron, cement, carbonaceous material or other finely divided materials are hardened will·

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The invention is described below with reference to the drawings illustrated embodiments are explained in more detail. These drawings represent schemats | i systems and Arrangements of process stages for grinding and drying from iiohkohle to a swirlable one. Mass of solid particles, Build up a desired pressure across the fluidizable particles and maintain a continuous one Feeding pulverized coal into a blast furnace iri & er Height of the tuyeres at a desired speed which is independent of that prevailing in the process Press istjol «* -. For the sake of simplicity, procedural stages are the majority of which are to be used are indicated in sections with dashed lines and only one of these process stages is shown and described in detail.

Figure 1 is a flow diagram showing a general arrangement and combination of the process steps shown in the figures Figures 2, 3 and 4 are illustrated in greater detail. For example, milling, drying and pressurizing should be done in front of the pressurized collecting container 1üO at a Double embodiment, i.e. in parallel Devices are made as shown in Figure 1, and also the majority of the following process steps are carried out such that, for one embodiment, four distribution containers (section D of Figure 4) with four standpipes

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or drain lines 164 from each header tank lead downwards so that each standpipe for itself solids particles to one of 16 tuyeres of a blast furnace (Section E of Figure 4) leads, are provided. That is, four down from the pressurized receptacle 100 leading standpipes transfer solids in transfer lines equal to line 150 ,. those with one of the four distribution containers in section D of Figure 4 in connection stand. In the embodiment of the invention shown in Figure 5, the entire structure of the method is practical the same. The main difference is in the use from two blocking tanks with parallel flow, which are fed by a single primary cyclone. The process steps of Figures 2 and 5 can be individually or as desired * - if used in the plural.

According to Figure 2 is coal in pieces by a rotatable Lui'tverschluß 4 (rotary air lock) introduced into a grinder 2 (bowl mill). Through the following described Milling and drying should be 28,600 pounds of dried coal per hour, of which at least 72, a grain size of below 200 mesh and the largest particles of which have a grain size below 16 mesh. In the process According to the invention, however, larger particles up to about 3.2 mm can in principle also be used, since these too

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can still be handled well in the following procedural steps. During the grinding of the coal in the mill 2 Air is introduced at a temperature of about 258 ⁰ G, the coal to a moisture content below 3 weight fö and preferably below about 1 wt -. Dry ⁰ Jo before in the in the following described primary cyclone is separated. Primary combustion air is introduced into the system through a filter 6, fed to a blower or compressor 10 via line 8 and then fed via line 12 to a zone 14 used to control the natural gas / air ratio. A combustible gas, such as uatr] ugas, is introduced into the system by conduit and supplied to this zone 14. In zone 14, the ratio of combustible gas to air is combined in one . , maintained range, and the mixture is fed via line 18 to the combustion zone 20, wherein the natural gas is burned with air, thereby forming an elevated temperature combustion product, which is combined with a second, through line 22 for the purpose of cooling or quenching the combustion products is combined at a lower temperature in the air stream introduced into it. The temperature of the air heated by the hot combustion gases and then introduced into the grinding zone for drying the ground coal is carefully controlled as a function of the type of coal used in the process

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a bituminous coal must be treated at a lower temperature than anthracite or coke and the temperature of the drying air after separation from the carbonaceous material must be below the temperatures that maintain the combustion. In the described specific embodiment of the method of the invention, bituminous coal is used, and the combustion gases are cooled to the extent by their assigned introduced air, that an air stream having a temperature below about 260 ⁰ C and preferably about 238 ⁰ O is obtained. This hot air is then fed via line 24 with the shut-off valve 26 to the grinding zone 2 in order to initiate the drying of the coal. The preheated air used to dry the ground coal forms a suspension with it, which is then fed through line 28 to a relatively large primary cyclone separator 30. The fan provided in the air inlet line 8 is sufficiently large to allow the atmospheric air with the associated natural gas to flow from the control zone 14 via line 18 into the combustion zone and from there into the grinder which is kept under negative pressure. This negative or subatmospheric pressure in the drying and grinding zone is intended to ensure that air flows into this zone rather than out of it. In the cyclone separator 30, which is at a pressure of about 43 cm of water under atmospheric pressure (a negative or minus pressure of

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about -17 inches water gauge) will be powdered Oil is very effectively separated from the air in the suspension, so that about 95% of the carbon is separated. The separated coal is withdrawn from the cyclone to be fed to a storage container described later. The air of the suspension separated in Ζνκίοη 30, which still contains a relatively small amount of entrained coal particles, is through line 32 from the Zykon withdrawn and fed to the suction side of the fan 34 under negative pressure. The fan 34 is dimensioned so that the desired negative pressure can be maintained and holds in the special embodiment., On the one suction side maintained a pressure of 48 cm of water under atmospheric pressure. This negative pressure is maintained in order to prevent air and carbon fines from flowing out of the system and thus serves as one of the safety measures, those involved in handling a mixture of powdered Coal and air are to be used. The air introduced into the blower with entrained carbon immersion ^ becomes with a slight overpressure of about 15 cm water is drawn off from this and through line 36 one of the separation of Coal fine particles serving zone 38 supplied. In this zone 3 ^, which is kept under slight overpressure, is the bulk of the confectionery divided into several small ones Cyclones are separated from the air supplied to this zone.

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From stirred in in the separation zone 38 is separated from air as much en :: r '^ inteil just withdrawn, that a suspension thereof; which is then formed by a line; .IcIa cyclone separator 42 is fed, in which the KOjIoI oi η particles are separated from the suspending gas and withdrawn from the bottom through line 44 urd the · : ■ -> -v ter be ο et 'en collecting container 72, yes in : Cyclone 42 separated. Gas from the suspension is withdrawn through line 6, fed through a Venturi junction regulator 4b, valve 50, shut-off valve 52 and line 54 of the line 32 under negative pressure, in order to be opened again. ^r i blouse 34 can be carried out.

Those in zone 36 of the. kohlefeinteilchen separated ■ air which still contains a small l.ienge to ivohlestaub, v.irc through line 56 drawn off through a conduit 6 and Zusatsgebläc -i <J in a What se rwä shear o2 passed. The auxiliary fan 58 serves the purpose of overcoming the pressure drop in the Viasserwäocher. Y / ater is introduced into the top of the scrubber 62 through line 64 to separate coal waste from the air introduced therein to form a slurry which is withdrawn through line 66 from the bottom of the vane 62. This slurry is thickened by gowns not shown and used according to Wunach. The one separated from the coal dust in V, äscher 62

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Air is fed through line 68 to a suitable chimney (exhaust).

The finely pulverized coal collected in the cyclone 30 becomes by their own weight via line 70 to a collecting container2, the one with atmospheric or something below spherical Pressure is maintained, supplied. As mentioned, the fine coal particles collected in cyclone 42 also pass through their own weight via line 44 into the collecting container 72. Ir collecting container 72 is therefore practically the entire pulverized coal produced and obtained in the previously described parts of the plant, with the exception of that in the Eaßwäscher 62 separated part collected. The collecting container 72, which is under approximately atmospheric pressure, is with a number of vertically spaced, not shown, temperature indicators and with upper, middle and lower solids level indicator .. for those introduced therein pulverized coal. The coal in the collecting container 72 is continuously with a gaseous Material, such as air, introduced through conduit 74 into the lower part of the conical bottom of this container, ventilated to keep the coal in it in a flowable Zxistand. The vent gas is supplied through line 71 derived from the upper part of the container and / in line 32 at sub-atmospheric pressure with that from the cyclone 30

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escaping gas combined. The coal in the collecting container flows by its own weight from the conical bottom of this container through a line 76 provided with valves 78 and 80 into the blocking container 82. In the system described here, the blocking container ö2 is used to increase the pressure on the pulverized coal from about atmospheric pressure to higher Pressure. Accordingly, the barrier container goes through a number of successive stages, namely filling, depressurization, emptying and depressurization. During the filling process, and when the coal in the blocking container 82 reaches a desired level, which is indicated by a level indicator in the upper part of this container, this level indicator automatically closes the valve 78 in the line 76 and thus interrupts the flow of solid coal particles into this container , after which the valve 80 is also closed and thus a gas-tight seal is created between the collecting container, which is under atmospheric pressure, and the blocking container. The following valves are of course closed during the J ^{1 UlIeIiS of the blocking container.} After the blocking container has been filled and the valves 78 and 80 have been closed, the pressure in the blocking container is increased to approximately above that in the subsequent distributor container by supplying compressed air through line 84. During filling, pressurizing and draining, the

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the oil in the blocking container 82 by supplying air through line 86 in the lower part of the conical bottom this container "ventilated to keep it in a flowable state. The in the Behäli 'ö2 to pressurize Lui "t used and venting is from its upper Part applied and then used either in the above-described extraction of i'einteilchen or entirely from the Drain procedures as described below. Well the pressure in the blocking vessel 82 to a desired value which is sufficient to move the coal into a subsequent, to transfer pressurized distribution container is increased, the valves 90 and 92 are automatically opened, and the coal passes from the conical bottom through conduit 88 into a pressurized one shown in FIG Collection container 100. The opening and closing of the valves 90 and 92 takes place automatically in the correct Order when the coal is transferred from the pressurized lock tank to the pressurized collection tank 1üO flows or after the barrier container has emptied is. If in the conical bottom part of the barrier container, As shown, a level indicator indicates that the entire Coal is applied to a signal from this level indicator automatically the valves 90 and 92. in the correct sequence closed, so that the connection between the blocking container 82 and the pressurized collecting container

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holder 100 is interrupted. The still under elevated pressure Üperrbeliälter Ö2 after closing the valves 90 and 92 by. Exhaust the gas or air therein through line 102 with valve 104 and restriction orifice 106 through a suitable chimney, not shown, to the atmosphere under a lower pressure of about 0.07 to about 0.35 atmospheres. After such a lower pressure is reached, a pressure-actuated failure closes the valve 104 and opens the valve 110 in line 108 with the constriction 112. The line 108 is in an open connection, with which, as mentioned above, held under subatinosphere Line 32. In addition, there is a communication line between line 1Q_, 2 and line 108; 114 Einein .bsnerrventil 116 and a \ ^r ereiigung 11b provided. The valve 116 is normally open so that while the sealing container is filled with coal, underdevelopment, emptying and printing of this container, a limited amount of gas can be continuously withdrawn. The main function of this line is to discharge the Leliiftun gas introduced into the bottom of this container. The line 108 with the valve 110 and the constriction 112 is open in order for the gas to flow through after the pressure in the sealing container has been reduced considerably in the postpressure stage. With this special form of implementation, the pressure is

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It is lowered to about 0.07 atmospheres by venting the gas through line 102 with valve 104 to suitable valves, not shown. Then the valve 110 is automatically opened and the valve 104 is closed, so that the remaining gas in the sealing container is fed through line 108 to the line 32 which is under atmospheric pressure. Durcn Sehließen of the valve 104 and opening valve 110 is to re Jihi facilitate zn with coal from eggs collecting container 72 of the! Pressure in the lock container on at least Atmospnärendruck, preferably at subatmospheric pressure, reduced, 11 s of the container, and the cycle described above will be repeated. In this embodiment of the method, the time required for one of filling, vacuum setting, emptying and depressurization and all the valve actuations required for these stages is generally of the order of magnitude of about 7 minutes. This time is scarce, but varies considerably depending on the number and size of the blocking containers used. As in the embodiment shown in Figure 5, two blocking containers can be arranged parallel to one another and used alternatively, as described further below. In one embodiment, all the stages described above, from grinding in the grinder to the pressurized collecting container 10 doj pelt, can also be carried out, with the pulverized cabbage (3 finally in a ^ uiiiuinsameii, under pressure

stoJ -jndeii iiulf;? iigb .. ... lter 1 UO fTüiagt vl-'d. _t

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As shown in Figure 3, the level of pulverized coal in the pressurized receiver 100 is increased measured a number of level indicators, and the cave got there through lines 88 and 120 into this container. That is, in a special implementation of the procedure the above-described process steps can be performed prior to grinding, Dry and pressurize so that the coal can be conveyed through the lines 88 and 120 into the collecting container 100, double and in parallel arrangement be performed. The receptacle 100 is maintained under a pressure of about 1.4 to about 7 atmospheres by duroh line 122 ventilation air is introduced, which then is drained from the upper end of this collecting container 100 through line 126 with the control valve 128. The pressure on the air in line 126 is reduced to a suitable value as it passes through valve 128, whereafter it Air through line 130 to valve 132 and shut-off valve 134, as shown in FIG. 2, is fed to the line 36. The branch line 136 shown in FIG. 22 with the valve and the shut-off valve 140 is used to divert some of the air from line 130 to parallel process steps similar to those in the drawing shown and described above to forward »

The pulverized coal, which is under increased pressure in the collecting tank 100, is from the lower part thereof

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by a number of separate discharge lines or standpipes similar to that in Figure 3 for the embodiment shown there Standpipe 142 shown withdrawn.

The standpipe 142 has in its lower part ^ the valves 144 and 146 to control the flow of powdered solid particles down through this standpipe. the pulverized coal passes from the bottom of the standpipe under increased pressure into a transfer line 150, the air by. Line 148 is fed to form a suspension of coal in air passing through the transfer line 150 to a separating and distributing container 152 (FIG. 4) which is under lower pressure. The suspension of Coal and air enters the bottom of container 152 and flows up through it at a sufficiently reduced rate Speed for the suspended coal to separate from the air and an aerated bed of pulverized Coal can form in it. The air can pass through one or more cyclone separators 154 in the upper part of the Container 152, v / o entrained pulverized koiile separated from the air and from where they are passed through ' a suitable dip tube is fed back into the bed will. The air is drawn from the top of the container 152. Line 156 with valve 1 58 together with in the same Way received air from the further manifold tanks

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through line 160 to control valve 162 (Figure 3) and from there passed into the line 130 in order to separate fine coal particles from it in the separator 38.

The separated and recovered in the distribution container 1jü2 pulverized Konle is made by several pipes or standpipes deducted from this, .uei a special embodiment four sol before discharge lines 164 are provided and in following; described.

From de: «Distribution container 152 is the pulverized coal withdrawn through the line 164 provided with a Venturi nozzle 166 and a control valve 168 in its lower part. In the standpipe 164, the pulverized coal is at a Execution of the process by admitting several air, Either distributed over its vertical height, ventilated, un the density of the carbonaceous material is below about 720 kg / m and preferably below about 370 lcg / m for a coal in which 70> j have a grain size of -200 mesh to hold. From the ground In line 164, the pulverized coal enters a transfer line 170 into which air is blown through line 172 so that in this transfer line 170 an ..iuspens: i on from Koh] ο in air with a concentration of less than about 4b i: g Xonie per m air is formed. i; i.r; ijn i.iuajH? iiö-i on will with a relatively low

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Velocity of about 9 »6 in / sec through line 170 to the normally open shut-off valve 174 and from there to the lance 176, which is emptied into the tuyere 178. The tuyere 178, shown schematically passing through the furnace wall 184- and through which the furnace air is passed, is fitted with a valve 180 and is supplied with air through the wind tunnel 182. A portion of those used in the method of the invention Air, in particular the compressed air, is taken from the air compressors (not shown) of the oven and introduced into the process through line 186 (Ji'igur 3) and fed through valve 188 to the cooling device 190, in which it is cooled ^{to a temperature of about 38 ° C} In order to keep the suction temperature of the auxiliary compressor constant, the bypass line 192 with the valve 194- is provided so that the air can be partially or completely led around the cooler. The compressed air flows at the desired temperature through line 196 to a water separation drum 198. From the bottom of this drum 198 water is withdrawn through line 200 with valve 202, while air t is withdrawn through line 204 and passed through the filter 206 and line 208 'to an additional compressor 210. There the air is further compressed to a pressure of about 4.9-7 aiii and then through line 212

Cj / - \ L / w I "

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with the valve 214 to the cooler 216, wherein the compressed air is ^{cooled to a temperature of about 38 0} G / ird. This cooled air is then fed to the water separator drum 220 through line 218. The air may be bypassed partially or completely past the cooler 216 through the bypass line 222 with the valve 224. Water separated from the compressed air is withdrawn from the drum 220 at the bottom through line 226 with valve 228. The dry compressed air is then withdrawn from the top of drum 222 through line 230 for use as described below. The return line 232 with the valve 234 is used to return the compressed air to the line 208, which is connected to the suction side of the compressor 210, in the event that such a return is desired for the reasons described below. The air compressed in line 230 to a desired pressure, which can be up to 7 atmospheres. is then fed through a flow regulator 236 and line 238 to an air distribution line 240 through which it is distributed for uses described below. A portion of the air in line 238 is withdrawn through line 242 to be used as instrument blowback air. Air is also withdrawn from line 238 through line 244 in order to put certain valves in the process under pressure and in order to

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provide additional ventilation air. Mn toilet Compressed air in the distribution line 24U is supplied by conduit through flow regulator 248, valve 250, and shut-off valve 252 into line 122, which is in communication with the lower part of the pressurized collecting container 100, introduced to be used as described above. Another portion of the air in line 240 is by line 254, flow regulator 256 (Ji'igur 2) and valve 258, and then through line 262, valve 264, shut-off valve 266 and restriction (restriction orifice) 268 into line 74, the with the container 72 in communication, introduced to, as described above in connection with I'igur 2, used to become. A portion of the air in line 262 can be withdrawn through line 260 for use in a parallel system (not shown). I am part of the air in line 254 also flows through flow regulator 270 and valve 272 into line 276 and from there through valve 278, shut-off valve 280 and constriction 282 into line 86 to be used as described above, Din part the air in line 276 (Figure 2) can be withdrawn through line 274 to be in a parallel system, not shown to be used accordingly. Another part of the air in line 240 (ü'igur 3) is through line 284, Strcimungsregistrier- and control unit 286 and valve 2o8 one

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Air collecting drum 290 supplied. From this drum the compressed air flows through line 292, valve 294 (i'igur 2) and valve 296 are zn into the conduit 84 which communicates with the reservoir in Ö2 compound to be used, as described above. From line 292, air can also be fed through line 295 to an iraralle! Control unit 30υ and valve 302 introduced into line 304. The air in conduit 304 is directed through restriction 306 into isolation valve 30d before entering conduit 148 for use as described above. The branch lines 310, 512 and 314 connected to line 304 are also provided with constrictions and shut-off valves (not shown) like those designated with 306 or 306 and serve to supply air to the lower or outlet end of the standpipes leading down from the container 100 316, 318 and 320, through which pulverized coal is fed into one of the distribution containers, similar to that described above in connection with the transfer line 150 and the distribution container 152.

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Another portion of the pressurized air in line 240 is passed through Line 322 withdrawn and through, the flow registration and control unit 324, valve 326 and shut-off valve §38 (fig 4) is fed to an air distribution line 330. This air manifold 330 is provided with sixteen unrelated but shown branch lines equal to line 332 to provide one of the plurality of standpipes, for example one of sixteen standpipes, in that described in connection with standpipe 164 >, iron, to supply air, i.e., as in Figure 4 as shown, air is drawn from the manifold 330 through a of the branch lines, identified as branch line 332 is fed to an air manifold 340 through valve 334, air flow meter and valve 338. From this line 340 a number of branch lines lead into the standpipe 164 for instrument and valve return air (not shown) and / or aeration air to be introduced therein. The branch lines connecting the manifold 340 and the standpipe are with constrictions, such as 342, 344, 346, 348, 350 and 352, which serve to split the flow if desired. A bypass line 3-54 with valve 356 is used to To introduce air from line 332 directly into the lower part of the standpipe 164. '

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From the manifold 240 (FIG. 3), air continues to be withdrawn through line 360 and through the flow regulator 362 and valve 364 into line 366 and from there through the shut-off valve 368 is fed to the air distribution line 370. A line 372 with the valve 374 is connected to the Line 366 in connection and serves as an alternative to the introduction of further air into the process. The air distribution line 370 has sixteen branch lines, such as line 376, with valve 378 and throat 380 by passing the air in line 172 for use as described above.

One of the essential features of the method of the invention relates to the control system that controls the flow of the pulverized Coal is guaranteed by the system to the tuyeres, regardless of the pressure that is applied to them Wind nozzles can occur over a relatively large range from about 0.35 to about 7 atmospheres. To this The purpose is by means of a differential pressure control 382 (Pigur 4) between the wind tunnel 182 of the blast furnace and Maintain a constant pressure gradient in each of the distribution containers 152 via the air distribution line connected to it, thereby ensuring that the pressure drop across the slide valve in each standpipe is in the range of remains about 0.21 to about 0.42 kg / om regardless of

909882/0477

Changes in air pressure at the V / ind nozzles. Differential pressure control device 382 maintains the desired pressure drop by controlling the back pressure on valve 162 (Figure 3) in line 160 through which air flows from pressurized manifolds ..152 to separator 38, and thereby the pressure holds in the vessel 152 at the desired value _t, the · by line 340 flowing, the ventilation of the standpipes serving air and the air flowing through line 172, the transfer of the coal in dilute phase from the bottom of the standpipe I64 through line 170 for introduction lance 176 serving Air, and the air used to transfer the coal through transfer line 150, is controlled by pressure co-injection flow devices which automatically compensate for changes in pressure measured at the manifold as described above, thereby maintaining substantially constant gas velocities even with pressure changes in the system. That is, the pressure maintained in line 160 by the differential pressure control device 382 is measured by the pressure registration device 384 (ligur 4) and sends a corresponding signal to the dosing devices 386, 388 (i'igur 3) and 390 (I'igur 4). The dosing device 386 actuates the flow registration and control device 392, which in turn operates the

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Valve 326 is actuated to provide the desired amount of ventilation air the standpipe 164 flows, regardless of the im Blast furnace pressure, as described above. The Thu, control device in connection with the flow regulators are pressure compensated flow regulators that are set to match that in the header tank or maintain a desired flow of air in the air flows withdrawn from this container. Accordingly, the metering device 388 (Figure 3) controls the flow registration and control device 394, which in turn controls valve 302 so that in line 304, which is in communication with line 148, the desired air flow is maintained, through the coal from the standpipe 142 through line 150 to the manifold 152 is fed, regardless of the pressure prevailing therein, as described above. The dosing device 390 (FIG. 4) also receives a signal from the pressure register device 384 (i'igur 4) and operates a flow registration and control device 396, which the Controls valve 364 to provide a desired flow of air regardless of the pressure at the bottom of standpipe 164 to line 172 is retained.

The pressurized collecting container 100 (Figure 3) is equipped with suitable pressure control devices, '

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by the pressure in this container above the pressure in the distribution container 152 to hold, whereby it is ensured that, regardless of the prevailing in the distribution container 152 Pressure, coal from the collecting container into the distribution container. That is, by a differential pressure actuator 398 (FIG. 3), which controls the valve 128 in line 126, becomes a desired predetermined X in the receptacle 100

ν maintain pressure, which is controlled by the fact that \ between the bottom of the collecting container 100 and line 160, as described above, a certain pressure difference maintains. This also serves to reduce the pressure drop in the Slide valve I46 in standpipe 142 relatively low, i.e. to be kept at about 0.21 kg / cm. A differential pressure registration and control device 400 (FIG. 2) controls valve 294 through which compressed air is supplied to container 82 is, and is actuated by the pressure prevailing in the distribution container 100 so that the compressed air in line 292 (FIG. 2) can put the blocking container 82 under a pressure which is equal to or higher than that in the collecting container 100.

The air supplied to the process through line 186 (Figure 3) is discharged from the outlet side of the (not shown) Blast furnace air compressors that supply the air for the wind tunnel (Figure 4), delivered so that the pressure of the air

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current in line 186 varies directly with and according to the pressure in wind tunnel 182. However, since those for that Process required air in the manifold 240 (Figure 3) must be under a higher pressure, i.e. under a pressure of about 50 pounds above that required in the wind tunnel, the auxiliary compressor 210 (Figure 3) is provided, to cause this pressure increase, and by the iiim associated Differential pressure registration and control device 402 which operates valve 234 in return line 332, the desired pressure increase is applied to that of the distribution line 240 through lines 230 and 238 Maintain air. In addition to the pressure control system described above, each header tank has a solids level control device assigned equal to that described in connection with the manifold container 152 as shown, by did the flow of coal into these containers is controlled. This solids level control device is actuated the valve 146 in the standpipe 142 leading down from the distributor container 100 so that the pulverized coal is maintained in the hopper 152 at a certain level. The collecting container 100

by also has coal level indicators, / which the grinder of the process is turned off or started as required to achieve the desired flow of pulverized Coal to the sump 100 to maintain.

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In the above-described process, a number of conveniently placed automatic temperature regulators are also used for safety reasons, since the temperature of the air used in the process with the pulverized coal must be carefully controlled. Accordingly, the temperature of the compressed air in line 230 is maintained by a temperature controller shown, which operates the valves 214 and 224 at about 38 ⁰ G. The temperature of the air supplied to the grinder through line 24 (Figure 2) is automatically controlled by a temperature controller shown which actuates the control device 14 for the flow ratio of air and natural gas by controlling the amount of natural gas that is combined with air and the furnace 20 is supplied, kept at not significantly above 238 ^° C. The drawn off from the cyclone separator 30 (Figure 2) through conduit 32, air containing Kohlefeinteilchen wifd maintained at not substantially above about 77 ⁰ C by the above-described, the controller controlling Stromungsverhaltnis fourteenth

As a further safety measure, temperature registration points are arranged there in the method described above, where it appears desirable, an uncontrolled and undesirable temperature increase in the process as quickly as possible to discover. These temperature indicators are connected to an alarm system that detects undesired temperature

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elevation and indicates their location. In this case, a carbon dioxide system is provided so that, if necessary, carbon dioxide can be introduced into the section of the process in which the undesired temperature increase is de-deoected. As a result, the entire system or only part of it can be protected by carbon dioxide.

The initiation of the procedure described here is proportionate simple, since it consists mainly in the fact that first the intended air flows and pressures can be set in all sections of the system. Thereafter, the air heater or furnace 20 (Figure 2) is set, by supplying it with natural gas and thus heating the air supplied to the grinder. The temperature of the procedure even if no coal is being transported does not rise above the due to the automatic temperature control provided permissible limits. Then the coal feeder l for the grinder switched on and the loading speed increased to the desired fourth. Then the remaining parts of the procedure arise automatically Even in such a way that the grinders are ground in from the grinder through the pressure build-up stages to the distribution containers 152 and from there, as described above, to the introduction for the pulverized coal.

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However, the interruption of the proceedings requires others Considerations as it is important for both security and procedural reasons that the Remove all pulverized coal from the system. To interrupt the process, the coal feeder for the grinder is switched off. The influx of natural gas to the oven used to heat the air supplied to the grinder is automatically lowered, when the amount of coal coming from the grinder decreases until it is completely removed. A decrease in the ratio on the combustion controls of the furnace enables this Setting a desired low temperature without carrying coal. Eachdem of the at the bottom of the under Atmospheric pressure standing collecting container 72 angeordente

Level indicator shows that the entire pulverized Coal is removed from this container, the flow of natural gas to your furnace is cut off while the furnace is in operation air continues to be supplied. During normal operation, a signal from the upper level indicator in the blocking container 82, the valves 78 and 80 in line 76 between the containers 72 and 82 are automatically closed. Sin automatic closing of these valves when interrupted However, the process is not always possible because there may be an insufficient amount of pulverized Konle remains in the system. Therefore are manual too

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actuating bypass relays arranged with holding windings, which enable the normal cycle of the containment vessel 82, i.e. load-pressurize-empty-depressurise, manually, i.e. without activating the signals of the automatic level indicator. Through this manual Actuation takes all of the pulverized coal from a container 72 and 82 removed. When the whole pulverized Coal is removed from the above portion of the system, the differential pressure regulators in the standpipes 142 of the lower ground The pressure in the collecting container 100 is manually set to 0, so that all of the pulverized coal can be removed from the container 100. After that, the entire Coal from and from the distribution hoppers 152 Sfcandipes 164 leading downwards are removed. Important; is that air flows through the system for a long enough time until with certainty that all pulverized coal has been removed from the system, and that valve 174 is in front of each Introductory lance is closed before the air disturbance is completely stopped by the procedure.

FIG. 5 shows schematically an embodiment of the method of If'igur 2 with a parallel flow. Reservoir 82. That is, the sequence of process steps for increasing the pressure on the pulverized coal from atmospheric pressure up to an increased iruck, like a ie iuii; he reference aiii '

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jj'igur 2, is applied in the same V.'cise to the parallel arrangement of distribution containers 82 'and 82 ", as shown in i'igur 5. The arrangement of" Figure 5 is such that these containers o2' and 82 "alternately feed coal from the collecting container 72 'with" and alternatively deliver the pressurized cone to the collecting container 100', as described in connection with FIG. Therefore, the same reference numerals in l'igur 5 are used as in figure 2 the _S necessary by one or two strokes are completed. The description of the process stages of FIG. 2 is also applicable to the embodiment shown in FIG. 5 when using one of the blocking containers arranged in parallel, so that a detailed description of FIG. 5 is superfluous.

The parallel arrangement of Figure 5 can be without essential

at

Modifications T take the place of the arrangement of Figure 2, and this arrangement can be used individually or in parallel, as described in connection with FIG.

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Claims (1)

Claims 1 _# Method for feeding solid material into a reaction zone, characterized in that the solid material is comminuted to a fluidizable particle size (2), the solid material prepared in this way is fed to at least one distribution zone (152) maintained under increased pressure and from this distribution zone in a plurality of separate and independent streams (I64) separate introduction zones (178), which empty into a reaction zone (184), and the independently controlled flow of fluidizable solid material in the individual streams is maintained at a predetermined speed. 2 «Method according to claim 1, characterized in that a gaseous material is used to convey the fluidizable solid material. 3 «Method according to claim 2, characterized in that an oxygen-containing gaseous material is used. 4. The method according to claim 2 or 3, characterized in that a constant pressure gradient is maintained between the distribution zone (152) and the reaction zone (184) to control the flow between these zones _o 909882/0477 5. The method according to claim 4, characterized in that the absolute pressure measured at the distribution zone (152) is used is used to reduce the volume of the gas, shaped material to regulate. 6. The method according to claim 5, characterized in that the speed of the individual streams of solid material, to the reaction zone is kept at a certain value that the weight of the gaseous material with is combined with the solid material, as a puncture of the absolute pressure is regulated so that the ratio W / D remains practically constant. 7. Method according to one of the preceding claims, characterized in that the solid material which can be swirled off is passed through a number of pressure build-up zones (72,82,100) to the distribution zone (152). 8 _# Method according to claim 7, characterized in that the fluidizable material is fed with preheated gaseous material to a raised separation zone (38) in which the solid material is separated from the gaseous material and from which the separated fluidizable material is passed through its own weight through the pressure build-up zones (72,82,100) 909882/0477 - 49 is directed. · 9 · Method according to claim 8, characterized in that the fluidizable solid material under subatmospheric Pressure produced and the separation zone (38) under subatmospheric Pressure is maintained, _# 10 The method of any of the preceding claims, characterized in that is held a dilute phase solid material above a dense phase of solid material in the distribution zone (152). 11. The method according to any one of the preceding claims, characterized in that each of the distribution zone (152) see below the linear flow of solid particles is passed through a solids flow control valve (168) and at a rate which is controlled in that this valve in dependence on the flow of coal particles through a zone The measurement of the solids flow (166) is controlled 12. The method sur controlling the linear velocity of a sur transfer of finely divided solid material in the form • lner Suspeenion gaseous through a transfer zone koMpreeeiblen used medium, characterized in that is used of the Abaolutdruok SUSPESION (152) Λ * <·· «09882/0477 the ratio of the weight flow / density of the compressible Medium in the suspension and thereby the speed of the gaseous flowing through the transfer zone (170) To keep the medium practically constant, 13, method according to claim 12, characterized. that an elongated transfer zone is used and that solid material is fed as a suspension in the gaseous material of a reaction zone. 14 ·· Method according to one of the preceding claims, characterized in that the solid material is bituminous
Coal, anthracite, coke, limestone, ore concentrate and / or sponge iron is used. 15. Method according to one of Claims 1 to 11 and 13, characterized in that the material which can be swirled
pulverized coal is used, which is fed to a blast furnace at the height of the tuyeres » 90-9882 / 0477