US3800630A

US3800630A - Procedure and installation for continuous steel making

Info

Publication number: US3800630A
Authority: US
Inventors: I Tripsa; I Potoceanu; C Popescu; C Cazan; I Nisipeanu; C Velicov; N Furnicescu; E Berceanu; D Cosma; O Tanasescu; N Deica; I Martin; D Dulama; N Kraft; G Driscu
Original assignee: CONSILUIL NAT PENTRU STIINTA S
Current assignee: CONSILUIL NAT PENTRU STIINTA S; CONSILUIL NAT PENTRU STIINTA SI TECHNOLOGIE RU
Priority date: 1970-10-08
Filing date: 1971-10-01
Publication date: 1974-04-02
Anticipated expiration: 1991-04-02
Also published as: GB1350499A; FR2112273A1; DE2144962C3; FR2112273B1; AT318676B; BE773038A; AU3407071A; DE2144962A1; AU464758B2; BR7106734D0; DE2144962B2; RO55785A2

Abstract

A process for the continuous production of steel wherein a stream of iron, admixed with alloying ingredients, slag-forming elements and the like is atomized with compressed air at a pressure of 7 to 8 atmospheres to remove phosphorous, silicon and manganese. The melt is continuously drawn from the collecting basin in this chamber beneath the slag layer and is then atomized by directing a blast of oxygen at the stream of iron to decarburize the melt which is thereupon collected, separated from slag and finely vacuum-processed and alloyed, all in a continuous stream.

Description

United States Tripsa et al.

atent 1 1 [4 1 Apr. 2, 1974 PROCEDURE AND INSTALLATION FOR CONTINUOUS STEEL MAKING [75] Inventors: losif Tripsa, Bucharest; lon

Potoceanu, Galati; llie Nisipeanu, Galati; Corneliu Velicov, Galati; Constantin Popescu, Galati; Cornel Cazan, Galati; Nathan Kraft, Galati; Gheorghe Driscu, Galati; llie Martin, Galati; Dan Dulama, Galati;.

Ovidiu Tanasescu, Bucharest; Nicolae Deica, Bucharest; Edmond Berceanu, Bucharest; Dante Cosma,

Bucharest; Nicolae Furniceseu, Bucharest, all of Romania [73] Assignee: Consiluil National Pentru Stiinta si v Technologie, Bucharest, Romania 22 Filed: on. 1, 1971 [21] Appl. No.: 185,503

. 30 Foreign Application Priority gum Oct.'8, 1970 Romania 64632 [52] U.S. Cl 75/49, 75/53, 75/59,

1 75/60, 164/53 [51] Int. Cl. C21c 7/02, C21C 7/10 [58] Field of Search....-...,. 75/46, 49, 51, 60; 164/53 [56] v References Cited UNITED STATES PATENTS 2,969,282 1/1961 Churcher 75/60 2,665,982 1/1954 Crego 75/60 3,519,059 7/1970 Voskob0inik0v.... 164/53 3,672,870 6/1972 Rhydderch 75/60 5/1972 Whetton 75/60 Primary Examiner-L. Dewayne Rutledge Assistant Exam iner-Peter D. Rosenberg Attorney, Agent, or Firm-Karl F. Ross; Herbert Dubno [57] ABSTRACT 'A process for the continuous production of steel wherein a stream of iron, admixed with alloying ing redients, slag-forming elements and the like is atomized with compressed air at a pressure of 7 to 8 atmospheres to remove phosphorous, silicon andmanganese. The melt is continuously drawn from the collecting basin in this chamber beneath the slag layer and is then atomizedby directing a blast of oxygen at the stream of iron to decarburize the melt which is thereupon collected, separated from slag and finely vacuum-processed and alloyed, all in a continuous stream.

3 Claims, 1 Drawing Figure PROCEDURE AND INSTALLATION FOR CONTINUOUS STEEL MAKING is their incompatibility with the continuous cast-iron,

process production processes and the continuation steel-casting and steel-rolling processes. This makes it difficult to create a truly continuous technological flow in the processing of ores into cast iron, steel and subsequently rolled metal.

In a procedure for continuous steel-making, liquid cast iron is introduced vertically and continuously into the apparatus through a funnel and is atomized by means of oxygen under pressure which sweeps away powdery fusing agents as, for example, lime and fluorine, the latter being necessary in the refining process. The drops of cast iron react quickly with the oxygen and the fusing agents and are turned into steel, which is collected at the lower part of the apparatus, is deoxidized and is cast by means of a continuous casting machine.

In yet another procedure used in continuous steelmaking, cast iron is continuously introduced into a container and is intensely blown upon with the oxygen and fusing agents introduced through a nozzle similar to those used in oxygen converters. Owing to the carbon oxide given off,'the metal bath mixes with the slagand is turned into emulsion, which overflows into a second container, where the steel thus made separates from slag, is deoxidized and is discharged into a continuous casting machine. Although these two continuous proceduresoffer many technological advantages owing to the high'speed of the reaction between the metal melt and the gaseous stage and the liquid slag, they yet have a number of disadvantages since all physical and chemical processes are carried out in a single unit although some of those processes, for example, silicon oxidation, prevent a suitable unfolding of the others, namely removal of sulphur and phosphorus. Consequently, only cast iron with .a low sulphur and phosphorus content can be processed by means of the aforementioned procedures. An attempt has been made to do away with this drawback by using two reaction containers when phosphorous cast iron is processed. Nevertheless the final sulphur and phosphorus content in the steels made by these two procedures is high.

On the other hand the quality of the steel made under these conditions is notsa'tisfactory for no efficient means is available for minimizing the gas content and the amount of nonmetallic inclusions in the melt.

As regards the installation used, its main drawback is that, owing to the simultaneous action of aggressive slag and of veryv high temperatures, the refractory lining of the apparatus is short lived.

From the economic standpoint, the disadvantage of the two procedures lies in the high loss in of iron swept away with the discharged gases, for oxidation occurs at high temperatures, the cast iron having a high carbon content while on the other hand such losses are due to the fact that iron drops are mechanically swept away by the slag, which is directly discharged from the atomizing aggregate without any previous decanting.

The procedure used in accordance with this invention does away with the aforementioned disadvantages for with a view to intensifying the physical and chemical processes of the various steelmaking stages, which are carried out in distinct aggregates, sulphur removal by means of usual reagents is carried out in the first stage directly in the trough in which cast iron is discharged from the furnace or in a mixer. In the second stage phosphorus, silicon and manganese are removed and more advanced sulphur removal takes place as well as partial decarburization by subsequent atomizing of mixedcast iron and fusing agents by means of compressed air at-2-8 atm. at moderate temperatures of l,320-l ,450 centigrade in a suitable aggregate. In the 7 third stage the metal is decarburized down to a 0.2-0.8

' percent carbon content by means of an oxygen blast at l,520-l,670 C and by cooling-and diluting the melt with pre-heated iron-containing admixtures, after which the melt is decanted. In the fourth stage, if rim- I ming steels are to be obtained, alloying and final deoxidization are effected in a separate bath with suitable fusing agents and ferro-alloys, while for killed steels there is an intermediate phase for processing decarburized iron under vacuum with a view to gas removal and deoxidization by means of its own carbon content, the ascending flow of the metal melt inthe vacuum-aggregate being ensured by the carbon oxide contained in the non-killed melt. I

In order to optimize the continuous steel-making flow, the combustion gases with a high carbon oxide content given off in the decarburization stage, are burnt with preheated air above the decanting, alloying and final deoxidation baths, after which their heat content is recovered in conventional regenerators and final alloying and deoxidation are effected, the melt being protected by a layer of synthetic slag introduced in powdery form and discharged from the respective bath in counter-current with thesteel made, and recirculated, also in counter-current, during the decarburization stage, whence, together with the slag resulting during the latter stage, it is recirculated in the cast iron atomizing unit where, recirculating in counter-current with the metal melt, it assimilates the silicon oxides given off in the respective stage so that a basicity ranging from 1.8 to 2.2 is reached. After the metal drops swept away have been decanted and the iron oxides swept away in metal form have been reduced by the carbon in the metal bath or by addition of supplementary reducing agents, the resulting slag is channelled towards the granulation stages.

' The installation for carrying out the method of the present invention is made up of a mixer into which molten cast iron flows continuously from the furnace in a strain. The unit is shaped like the frustum of a cone and provided with a funnel with a calibrated orifice for feeding molten metal, with means for feeding fusing agents and compressed air and with a sole-plate continued at one end by a melt-discharging channel and at the other end, by a slag-discharging trough.

The installation also includes a cylindrical decarburization container provided with facilities for blowing oxygen and additional ferrous material. The capacity of these facilities is at least fifteen times greater than the per minute output of metal melt. A lateral orifice connects the blowing facilities with a decanting vessel, which may be directly connected with the final deoxidation and alloying vessel by means of a siphon trap or may be initially connected to the ascending pipe of a vacuum processing aggregate which has an oblong, possibly an oval, vacuum chamber and is connected by means of a descending pipe to the final alloying and deoxidation vessel. The latter vessel is provided with orifices for the introduction and discharge of synthetic slag in counter-current; the slag is-recirculated in the decanting vessel and is further recirculated, together with the slag resulting from decarburization in the cast iron atomizing aggregate through suitable orifices.

The sole FIGURE of the drawing is longitudinal section of the installation according to the invention.

The cast iron discharged from one or several furnaces, which are not shown in the FIGURE, flows in the form of a molten-iron stream 1 along a trough 2 where a layer of furnace slag 3 is separated by means of a conventional device 4 in a mixer 5. The mixer 5 is provided with devices for the introduction of powdery reagents, preferably by means of a gas (nitrogen or methane); and for the separation 'of desulphurization slag, which is subsequently discharged. Thus, in the first stage of the technological process the slag in the mixer 5 or along the trough 2 is treated with common active desulphurization agents, for example lime, sodium carbonate, calcium carbide, aluminum., which are introduced with the assistance of a proportioning device 6, sulphur activity during this stage being at its highest owing to the high carbon, silicon and phosphorus content. After desulphurization, the liquid cast iron is separated from a first slag layer 7 by means ofa conventional device (eg stripper 8), and flows continuously into a funnel 9 with a calibrated orifice through which the molten-metal stream is passed with a view to atomization. i The calibrated orifice of the funnel 9 may have any section desiredincluding a circular one, though to minimize thelpressure of the air necessary for suitable cast iron atomizing, a rectangular or elongated section is tobe preferred, so that atomization of the cast iron jet in the form of small drops should be achieved with air at a pressure of 2-8 atm. Compressed air is intro duced through two pipes (10a and 10b), which are parallel to' the flat cast iron jet; the pipes are water-cooled and slope radially at an acute angle of 10 to 80 as against the vertical. The inside diameter of the horizontal pipes (10a and 10b is 10-50 times greater than the width of the slits through which compressed air is blown in.

Conventional devices 11a and 11b feeding common powdery fusing agents required for dephosphorizing cast iron as, for example, lime, ore, etc., end above the horizontal compressed-air pipes (10 a and 10 b).

The atomized cast iron flows in the form of fine drops 12 into an atomizing unit 13.

It is in the atomizing unit 13 that the second stage of the metal melt processing takes place, during which the silicon, manganese and phosphorus are eliminated, the cast iron being atomized with the help of air and fusing agents and moderate temperatures (1,300l,400C) being thus obtained. At these temperatures these elements are practically completely eliminated while the carbon in the cast iron is partially oxidized, the carbon content being maintained over 2.5 3 percent. The lower temperatures result in smaller losses of iron swept away with the discharged gases as well as in enhanced durability of the lining of the cast iron atomizing unit.

The atomizing unit 13 has a metal body in the shape of the frustum of a pyramid lined with refractory materials able to withstand the temperatures developed as a result of the intensive reactions in the oxidation of the silicon, manganese and phosphorus in the cast iron, and of part of the carbon in the cast iron, as well as full combustion of the carbon oxides produced. The unit is provided with a basin 15, in which the metal melt and the slag collect; at one end the sole-plate continues as the channel 19 for continuous discharge of the melt after continuous separation of another slag layer 14. It is through channel 19 that the metal melt is introduced into the decarburization container 20.

At its other end the sole-plate 14 of the atomizing unit 13 terminates in an elongated trough 16 where the metal drops in the slag are decanted and the iron oxides in the slag are reduced. The discharged slag 14 is introduced into a water-jet granulation device which is not shown.

At the lowest part of the basin 15 there is an orifice designed for cast iron discharge 18, which is usually closed but which opens to discharge the entire quantity of metal melt and slag when for various reasons continuous operation of the installation is interrupted for a long period. The gases produced during this stage in the processing of the metal melt are discharged through a pipe 17.

The decarburization chamber 20, which is preferably cylindrical is in a vertical position and has a capacity at least fifteen times greater than the per minute output of the metal bath. The channel 19 along which the metal melt flows into the chamber 20 may have any section and can be located at various levels, though it is preferable that the melt should be introduced tangentially at the bottom of the chamber 20 to ensure good mixing of the metal bath in the container and consequently rapid dilution of the carbon content in the fresh portions of the metal bath.

The decarburization chamber 20 is provided with one or more conventional nozzles 22 designed for blowing pure technical oxygen, as well as with orifices 23 and conventional devices (which are not shown in the drawing) feeding powdery fusing agents (lime, fluorides, ore, cinder, etc.) and additional iron for cooling the bath, in the form of scrap iron, metallized pellets or iron sponge.

The decarburization-chamber 20 sustains the third stage in the processing of the metal melt; the latter reacts intensely with oxygen and fusing agents, a steel and slag emulsion being thus obtained, which is discharged through a lateral opening 25 of the chamber 20 into a decanting vessel 23.

In order to reduce the loss of iron, which is swept away with the discharged gases, the metal bath in the decarburization chamber 20 always contains,'as has been shown above, a volume at least 15 times greater than the per minute output of metal melt so that the carbon content is diluted after introduction of every portion of the melt into the chamber 20. The carbon content in the decarburization container 16 being kept constant, at a value ranging from 0.2 to 0.8 percent C depending on the quality of the steel to. be made, losses of iron with the burnt gases are diminished to a minimum.

As the decarburization reaction is exothermic and heat is given off in the process, the metal bath is overheated and, in order to keep the temperature at a constant level l,520 1,670C, depending on the brand of the steel to be made cooling materials must be introduced. To this end the necessary quantities of iron oxide (cinder) and metal iron in the form of pieces of calibrated dimensions, scrap iron, metallized pellets and iron sponge, are continuously introduced into the chamber through the orifice 23. This results inoptimum use of the reaction heat, a rise in steel making efficiency and dilution of the carbon content of the metal melt in the decarburization chamber 20.

Resistance of the refractory lining of the decarburization container and of the decanting vessel is ensured by the complete elimination of the acid silicon and phosphorus oxides from the slag, elimination of the oxides being due to the total oxidation of silicon and phosphorus in the cast iron atomizing unit 13.

' The decarburization chamber 20 has a discharge orifice (which is not shown in the drawing.) which is generally closed but maybe opened in order to discharge the melt upon a prolonged interruption in the running of the installation. v

The decarburization vessel 29 has a vault 24 which it shares with the decarburization chamber 20; the latter is provided with an orifice 26 through which the preheated air required for the burning of gases yielded I in the decarburization stage is blown. The gases contain carbon oxide. The recuperator in which the air is pre-heated is not shown in the FIGURE. The burnt gases are directed towards the stage of final decarburization and alloying of steel by means of a channel 42 located at the upper part of the' decanting vessel 29.

The decanting vessel 23 is also provided with a channel' 26b, which serves to discharge the slag layer 70 resulting from decarburization and has an orifice 28,

To this end the vacuum chamber, as has already been shown, has an elongated, oval, section about seven times greater than its width so that the time during which the vacuum acts on the same portion of steel is 3-4 timeslonger than the time it takes the steel to pass through the vacuum installation commonly used, or is equivalent to the sum total of the time during which the vacuum acts on the steel, if there is repeated passage after recirculation through installations of this type.

On the other hand no argon penetrates into pipe 31 for admission of the metal melt, as the latter consists of rimming steel able to generate a sufficient amount which is generally blockedfand whichserves to discharge steel when the installation is brought to standstill. THe vessel has a siphon trap 29, through which rimming steel is discharged towards the casting installation, and an orifice 30 to which a pipe' 31a is connected, the latter coming from an aggregate 32 processing the metal melt under vacuum when killed steel is to be obtained. 7 q

The vacuum processing aggregate 32 has a vacuum chamber of anelongated, possibly oval, shape, two pipes 31a and 31b for feeding and discharging steel, a pipe 31c connected to the vacuum pump for gas discharge, and locks 33 for addition of ferro-alloys and fusing agent's under vacuum conditions, if necessary.

Two or more vacuum processing aggregates 32 may be mounted in parallel so that, in case one unit is disabled, another-aggregate may be used and the continuous steel-making installation is not be kept at a standstill for a long time. In the making of killed steel, the fourth technological stage, takes place in the chamber of the vacuum processing aggregate32; it-consists of deoxidation by the carbon in the metal melt, and in the removal of gas from the melt. A low content of gases and non-metal inclusions is thus ensured in the steel made.

35 in the vessel serves to introduce the necessary ferroalloys (ferro-manganese, ferro-silicon, etc.) in granulated or melted condition and in the quantities needed to obtain the chemical composition prescribed for the various brands of steel to be made, including alloy steel. When these additives have been assimilated, the steel is discharged, preferably into continuous casting machines, thoughcommon ladles may also be used.

Subsequently the steel is introduced into ingot or casting molds so that ingots or castings are obtained. In case of need a second casting machine or several such casting machines may be used without the continuous making of steel being interrupted.

The vessel for final deoxidization and alloying of killed steel 34 is shaped like an elongated trough and is provided, as has already been shown, with an orifice 35a feeding powdery or liquid ferro-alloys, with another orifice 35b feeding a powdery mixture that forms deoxidizing slag, with a siphon trap for steel discharge without anyslag being swept along towards the continuous or common casting machines 40, with yet another orifice 41, which is permanently stopped and serves to discharge the contents when the installation is brought to a standstill for along time, and with a channel 43 through which the burnt gases are discharged towards the chimney stack. The burnt gases are directed from the decarburization stage through channel 42.

When the powdery mixture of lime and fluorine is introduced through orifice 38, a layer 44 of synthetic slag for desulphurization and deoxidization isformed. The slag is discharged through orifice 45, circulates in counter-current with the steel produced, and is directed through a channel'that is not shown in the FIG- URE towards the decanting vessel, which is provided to this end with an orifice serving to feed synthetic slag. The latter, together with the slag layer 27 resulting from the decarburization stage, is channelled towards the cast iron atomizing aggregate 13, which is provided with an orifice 46 serving to 'recirculate the slag. The necessary conditions are thus created for full use of the refining capacity of slag. From the cast iron atomizing aggregate 13, the-slag 14 goes along a trough 16 where the metal drops swept away mechanically are decanted, and is subsequently discharged. It is in the same trough that the iron oxides in the slag can be reduced by means of the carbon in the metal bath or, if

necessary, by means of the carbon in the reducing materials (coke, methane, etc.) introduced for this purpose.

A minimum iron content in the discharged area is thus ensured as well as best efficiency in the making of steel. The slag discharged possesses a comparatively reduced basicity (1.8-2.2) owing to assimilation of the silicon oxides produced in the atomizing installation andcan consequently be used as building material, the

economic efficiency of the entire process being thus enhanced.

The installation may be provided with various orifices for visual monitoring, gauges to check the running of all aggregates, facilities for centralization of the controls of the installation at one or morecontrol points as well as with facilities enabling the use of electronic computers with a static or dynamic operation regime to control the steel-making process in the respective installation.

It has been found that by effecting desulphurization in the first stage by means of common clesulphurizing agents and under the conditions shown above, in mixer 5, the sulphur content decreases fromits initial values of 0.039 to 0.136 wt percent to values ranging from 0.013 to 0.042 wt percent.

During the second stage, which takes place in the cast iron atomizing aggregate 13, the silicon content decreases to the final value of 0.48 to 1.03 wt percent; the manganese content decreases from its initial value of 0.83 to 1.22 wt percent to values below 0.05 wt percent; the phosphorus content decreases from its initial value of 0.051 to 0.107 wt percent to 0.008 to 0.036 wt percent; the sulphur content further decreases from 0.013 to 0.042 wt percent tothe final value of 0.002 to 0.021 wt percent, and the carbon content decreases from its initial value of 3.79 to 4.21 wt percent to 2.84 to 3.09 wt percent. Consequently on issuing from the atomizing aggregate 13 the metal melt practically consists only of iron and carbon.

As a result of the dilution of the melt in the metal bath mass of the decarburization container 15, which is 15 times larger, the carbon content decreases to 0.2 wt percent for example, and this value is kept constant in the container. The carbon content of the metal melt further decreases owing to intense reaction with emulsion slag, so that the carbon content in the decanting bath is kept constant: 0.10 wt percent, in the example given above.

The final composition of steel, according to requirements, is obtained by adding the required quantities of ferro-alloys to the final deoxidization and alloying bath 36, to achieve a pre-established rise in the content of carbon, silicon, manganese and other alloying elements.

The present invention offers the following advantages: I

An optimum quality is ensured for all compositions of killed and rimming steel owing to a low content of sulphur, phosphorus, gases and non-metal inclusions, and to a chemical composition which is in accordance with the standards established for the most complex steel types.

High efficiency is obtained in the making of steel by reducing to the very lowest losses of iron swept away together with the slag and the discharge gases and by allowing the processing into steel of a considerable quantity of iron waste, mechanized pellets, iron sponge, cinder and other materials containing metallic iron in the form of oxides materials which may be introduced and be preheated by using the heat of the discharged gases Good use is made of the reaction heat resulting directly or indirectly (by CO gas combustion) from the decarburization process. The heat is used to heat the metal melt and maintain it at the required temperature of 1,5201,670C until the steel is discharged from the installation; to smelt iron waste, metallized pellets and iron sponge, and to reduce the iron oxides in the cinder and other materials introduced into the decarburization container. To this end complete combustion of the gases resulting from the decarburization process is ensured in the steel-making installation, and part of the physical heat of the discharged gases is recovered and is used to preheat the combustion air.

Oxygen consumption per ton of steel is reduced to a minimum for the processes of silicon, manganese and phosphorus oxidation and about 25 percent of the oxidation of the carbon in the cast iron are achieved by means of the oxygen used in the atomizing of cast iron. Furthermore for the oxidation of the carbon in the decarburization container use is made of part of the oxygen brought by the iron oxides in the cinder and in the other materials that are added.

Consumption of fusing agents is reduced to a minimum owing to full use of the refining capacity of the slag that is formed, and to its movement, which is in counter-current with the metal melt. At the same time the final composition of the slag discharged from the aggregate makes possible its granulation and its use as building material.

We claim:

1. A method of making a steel comprising the steps of:

a. continuously desulfurizing a molten-iron melt by treating a continuous stream thereof with a desulfurizing agent; f

b. continuously atomizing the molten iron stream treated in step (a) and depositing, the atomized droplets of molten iron'through a slag layer into a first molten-metal bath;

c. continuously decanting a second stream of molten metal from an upper portion of said first moltenmetal bath;

(:1. decarburizing said second stream of molten metal by continuously emulsifying same at a location spatially removed from said first bath with at least one oxygen jet to produce an emulsion of the molten metal of said second stream:

e. collecting said emulsion in a second molten-metal bath beneath a slag layer and separating gas from said emulsion in said second bath;

f. continuously decanting a third stream of molten metal from an upper portion of said second bath below the slag layer thereof and casting the molten metal of said third stream; and

g. feeding slag from said layer above said second bath to the slag layer of said first bath.

2. The method defined in claim 1, further comprising continuously treating said third stream at a subatmospheric pressure to degas the molten metal of said third stream and permit deoxidation thereof with carbon intrinsic to the molten metal of said third stream.

3. The method defined in claim 1, further comprising

Claims

2. The method defined in claim 1, further comprising continuously treating said third stream at a subatmospheric pressure to degas the molten metal of said third stream and permit deoxidation thereof with carbon intrinsic to the molten metal of said third stream.
3. The method defined in claim 1, further comprising the steps of collecting molten metal of said third stream in a third molten-metal bath; forming a synthetic slag layer on said third bath; deoxidizing and alloying the molten metal in said third bath; and circulating at least portions of the slag layer above said third bath to at least one of the slag layers of steps (b) and (e), the molten metal of said third bath being decanted for casting in step (p).