BE460421A - - Google Patents

Description

       

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  Process for the treatment of mineral and organic products and installation for the implementation of this process.



  The present invention relates to a process for reducing mineral or organic products with a view to their purification or transformation, characterized in that the product to be treated is stirred on superimposed trays and that this product is dropped from tray to tray. as it is stirred, while the reducing gas is circulated between the plates, which favors reduction owing to the large contact surface between the reducing gas and the material to be treated, this process thus making it possible to process large quantities of products in a space-saving enclosure.



   According to one embodiment, the product to be reduced is first calcined in order to remove the volatile impurities by stirring the product to be treated on the superimposed trays and in

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 dropping this product from tray to tray as it is stirred, while the hot gases are circulated between the trays, then said product is dropped onto the
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 prcMj.er reduction plateau and 3 'we provoke ous'.i! t 1 <1 =, Îtlumticon coufornent in the previous paragraph, t.



  A variant is characterized because one r:.:. ;; nÈn't "i 1'3 reducing gas by the action of a catalyst or ii1al carbon :.desce.1.t.



  According to a first modc of ¯ a 1 = q '¯on, - -' the leaks from the reducing gas regeneration chamber on the products to be treated in order to calcine them before the operation
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 reduction, which improves the thermal re.T.dei # ut.



   A variant of the above process is characterized because part of the reducing gas to be regenerated is sent to the product to be reduced, while the other part is regenerated before being sent to the product to be reduced.



   The invention also extends to a process for manufacturing hydrogen characterized by sending a stream of vapor
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 of water on magnetite, which, combined with 1 toxge, 1.i water, liberates hydrogen and that one. re8enerate this i.gnétite by reducing it according to the procedures in accordance with one or other of the preceding paragraphs.



   The invention also relates to a process for the halogenation of inorganic or organic products with a view to their purification or their transformation, characterized by the fact that the product to be treated is stirred on superimposed trays and that this is dropped.
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 product from tray to tray as and assures its l: r:;. ss; 1.G}, while we circulate 1: .3 lâlo ::, 5n: rt between the rla V: ā : has what favors 11blogé.11ttoll "therefore <1 * 1¯a cr '! ::! .. 3 3 :::: C':

   C2 de conts-ct 03> iter the gr-z Il:;. LoGénl1t and la: s: 4it.re to Irsitor this proceeded p riiett = have .i.xsi to deal with Gl - ;;. Gr} E: s .iuārlt: its de,:, roc1uits dans -ar-e enclosure d "3û <\ Om1): 1e.t: 1., ::,: t reduced *!. 'invention concerns eacore wi p # mPlài , the ^. '. slv7.'i7, ratio of products n: 1;

  iàsra = 1x or organic ell view of their purification or luar transformation characterized because the product to be treated is stirred on superimposed trays and

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 fall this product from tray to tray as it brews, slums where the chlorinating gas is circulated between the trays, which promotes chlorubation due to the large contact surface between the chlorinating gas and the material in treating this process thus making it possible to treat large quantities of products in a small footprint,

   
The invention extends to a method of calcining mineral or organic products with a view to their purification or their transformation in which the product to be treated is stirred on superimposed trays and this product is dropped from tray to tray as and when. s measurement of its stirring, while the hot calcination gases are circulated between the trays, a calcination process characterized by the fact that the hot calcination gases can be produced at different stages of the trays and at temperatures well determined for each of these stages, which makes it possible to adjust the temperature of the product to be treated under the best conditions, according to the combinations to be produced at the different stages.



   The invention also extends to a distillation process. of mineral or organic products with a view to their purification or their transformation characterized because the product to be treated is stirred on superimposed trays heated internally by a circulation of heating fluid and this product is dropped from the tray as and when as it is stirred, the distillation products rising through the trays to be then condensed.



   The invention also extends to a method for drying solids, characterized because the material to be dehydrated is stirred on superimposed trays, internally heated by a circulation of heating fluid and this material is dropped. from tray to tray as it is stirred, the dehydration vapor rising through the trays to be evacuated.



   Case processes are applicable, not only to a single product, also killed to. a mixture of products, the action of purification n being able to be carried out on one, several or on the whole

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 products constituting the llldb.l1ge.



   According to an embodiment of any of the preceding methods, the reaction gas flows from the bottom to the top in the opposite direction to the product to be treated, which produces a circulation.
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 methodical and enables the differences in temperature between the reaction gas and the product to be treated to be best adjusted.



  The invention extends in a general manner to these methods of reduction of halogenlittion, chlorination, calcination, distillation or drying of products -elnùratiz or. Gold # & niu0S.



  Liais it also relates to various sodas of realization which smells like all the preceding processes *
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 According to a first embodiment of the methods for reducing halogenation of chlorurztioa, calcination, distal- lation and drying, the preceding operations are carried out at a pressure lower than the pressure .t:; -. Osph6rlque.



   The thickness of the layer of treated product varies depending on the reactions to be carried out.



   The product is heated on part of the trays
The gases intended for the treatment of the product are brought into contact with the product on part of the trays.
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  Each tray or series of trays is heated separately so as to obtain temperature zones defined on each tray, which makes it possible to perform various successive or simultaneous reactions each corresponding to one or more temperature zones.
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 t3rlperatars.



   A cooling fluid is circulated in certain trays, so as to absorb heat on the trays where the reductions are exothermic, which makes it possible to limit the heat.
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 reaction temperature and to ensure Gs :: o.ler.1ent storage. du: r # t.-'-. riPl used.



  Catalysts are incorporated into the product to be treated or flui.e: zeü;., To promote l3s r.:...ctiO.1S ani3re and aiiroître laurs speeds.



  We run a lans of different products to process from top to bottom in more. '.: 1st anpprells tales and series' 1 ")

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 one below the other and in which the various gaseous streams required are circulated, the mixture of products to be treated circulating by gravity. o controls the reduction speed by varying the stirring speed of the treated products on these trays, adjusting the speed to a very low value allowing reactions to be carried out on powdery materials, while reducing. sant the entrainment of dust.



   The products to be treated are brought to the pulverulent state to facilitate the reactions which thus become faster and more complete. The invention generally extends to all of these processes, whatever the apparatus. and the facilities for their realization. However, the invention also extends to various installations allowing a particularly simple and efficient implementation of the above processes.



   To this end, the invention relates to an installation for the reduction of products in accordance with the foregoing methods and characterized by a calcination furnace first purifying the product to be reduced and a reduction furnace arranged under the calcination furnace, so that the product to be treated circulates by gravity from one oven to the other.



   The invention also relates to an installation for the reduction of the product in accordance with the preceding paragraph and characterized because the gases leaving the reduction furnace are sent to a converter which regenerates the reducing gas by the action of a catalyst or of incandescent carbon.



   The invention / extends also to a distillation or drying apparatus characterized by rotary plates interposed between the fixed plates, the rotary plates sweeping the product to be distilled to bring it down from plate to plate, these plates being traversed by a heating fluid to bring the product to the distillation or drying temperature.



   The invention also relates to a process for the treatment of ores containing iron oxide.



   In their natural state, ores (oxides, sulphides

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 carbonates, etc.) contain, independently of the desired metal element, a variable number of metal compounds constituting the impurities; these are in the majority of cases difficult to remove and, therefore, the element metal cannot ultimately be obtained except in a state of purity approaching more or less absolute purity.



   Thus, for example, the iron oxides obtained by the processes customarily used can have an impurity content of 20% and sometimes more.



   The known purification or enrichment processes rely in the majority of cases on the application of physical means as is done in flotation processes. or separation. using a magnetic field.



   It is recognized in the latter case that the purification of the ore is very variable, and in any case incomplete unless the ore already presents a high purity, as in the case for example of natural magnetite,
This is essentially due to the nature of the impurities, their physical state, as well as their possible combination with the element metal.



   It is possible to remove the impurities, partially or totally, by chemical means, using appropriate reagents * But this technique is very expensive in practice and is only used for refining the crude product as long as this operation is paying.



   The object of the present invention is to avoid the foregoing drawbacks,! It relates to a process for the treatment of ores containing iron oxide, characterized in that the ore is heated until complete melting, so that the impurities constituting the guangue are slagged, float the molten dioxide mass and are thus easily separated from this oxide.



   According to one embodiment of the invention, a flux, lime, soda silica, for example * is added to the treated ore.
This flux is chosen according to the nature and composition of the impurities from a qualitative point of view and according to the importance

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 quantitative impurities,
In carrying out the process according to the invention, the ore is brought to complete melting with or without the addition of reagents, and the slag is obtained in the upper part of the molten bath and the molten oxide. , stripped of most of its impurities, at the lower part.



   The operation is carried out in different media, depending on the nature of the iron oxide which it is proposed to obtain * a) the operation is carried out in a medium ydant to obtain iron seequioxide, For example, can blow air or oxygen into the bath so that the proteoxide is brought to the state of sesquioxide fe2 o3 or magnetite fe3 o4.

   b) on the contrary, the operation is carried out in a slightly reducing medium in order to obtain iron protoxide Feo or magnetite oxide Pe3 04 so as to remove as much as possible in this case of the iron sesquioxide. '
The treatment of the oxide of molten iron at the outlet of the melting furnace depends on the nature of the iron oxide which is to be obtained as explained below:
The molten iron oxide is subjected:

   a) abrupt cooling to normal temperature away from air to obtain Fe3O4, b) less, rapid cooling, for example, in the ambient environment to obtain Fe2O3 c) rapid and abrupt cooling from a temperature of 700 minimum, retort for Fe3O4. when we want to obtain FeO.



   In the case of ores containing volatile metal oxides, for example zinc oxide, the ore is first heated so as to remove the volatile oxide which is then recovered by condensation, then the residual ore is treated with the previous processes.



   The invention also relates to a process for obtaining metal iron and its oxides from ore, whatever its nature, characterized because the ore oxide is first reduced to the metal state or of sub-oxide, then the

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 reduced product, thus separating the metal or x from impurities and effectively removing these impurities in the form of slag.
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  This process which, in fzit, is characterized by the. C3mtainaison of the two operations known per se (ro1clue, ti O! l, then fusion) thus makes it possible to obtain the iron # at.t = 1 or the suboxide.au ..11fr.: xlmüm possible of purity , 1s. all of the gangue being effectively eliminated. 'The intention concerns, not only, the process ,, 61141rel described above and characterized pure 1 & co: b; ¯nr i son, 5.? Nér ;;; the two a p6r & t Ion known per se (rGdt , tetiol1, fusion),:

  There are also other procedures which are carried out by this. combination of the previous process with eoMplénientaireSt operations
First of all, the invention relates to a process in accordance with the preceding ones and characterized because, after having separated the iron metal or the suboxide, it is oxidized, so as to obtain an oxide with a desired oxygen content.
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  We can also, according to the idea, reduce the
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 oxides of, iron -mataI or the sub-oxide until 10 iron peroxide (sesquioxide Fe2 0) is obtained, ie the oxide with maximum oxygen content.



   It is also possible, in accordance with the invention, to reduce the iron oxides obtained in accordance with the preceding paragraphs and in particular the iron sesquioxide Fe2 O3, so as to obtain an oxide in a less oxidized stage, in particular the magnetic oxide Fe O4.



   Ultimately, the process defined above has the following three general characteristics: a) treatment of iron ores by the combination of the two operations (reduction, smelting). b) oxidation of the iron metal or of the oxides obtained according to the preceding paragraph. c) reduction of these oxides, so as to ultimately obtain the oxide at exactly desired content.



   In the following description we have grouped, for the clarity of 'this' exposed all the embodiments around

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 these various successive operations:
1 - Reduction operation -
It is advantageously possible, according to the invention, to carry out the reduction of the iron ore by applying to this reduction reducing gases with high carbon monoxide CO contents (preferably greater than 60); these high content reducing gases have high activity and thus allow reduction to be carried out at relatively low temperatures. Therefore, the expenditure of calories in the operation is reduced to a minimum.



   The proportion indicated above can obviously be modified by way of example. In particular, reducing gases of up to 80 - 90% carbon monoxide CO and even more can be used.



   In order to obtain these reducing gases with a high carbon monoxide content, they can be advantageously produced by passing oxygen, instead of air, over the carbon.



   It is possible, without departing from the spirit of the invention, to use reducing gases of very different compositions and in particular one. can use reducing gases which contain either carbon monoxide CO, hydrogen H, or a mixture of carbon monoxide and hydrogen.



   In the latter case, the reducing gases are obtained, for example, by passing water vapor over glowing charcoal, resulting in the formation of a water gas rich in carbon monoxide and in hydrogen.
The hydrogen introduced into the reducing gases also has the effect of greatly reducing the carbonization of the iron and thus makes it possible to obtain a molten metal with low carburization *
The implementation of the above characteristic of the method according to the invention thus leads to provision in this. installation of a steam generator *
The water vapor 'thus obtained is applied partly to the manufacture of the reducing gases, as explained above, and partly to any other operation, for example drying the oxidized ore.



   This water vapor thus constitutes a very convenient means of heating to ensure in a very simple way the setting.

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 industrial work of the whole of the invention.



   According to another characteristic of the invention, the reducing gases are passed over the iron ore in order to reduce it, then these gases are regenerated and they are passed again over the iron ore, these gases thus circulating in a closed cycle, which ensures a completely methodical reduction of the ore and perfectly homogeneous results; this arrangement thus has the important advantage of reducing the. consumption of reducing gases and in particular the consumption of the coal necessary for the formation of these reducing gases.



   According to one embodiment of the. previous characteristic, the reducing gases rich in carbon monoxide are partially or partially regenerated. all by their passage through a carbon column, whatever its purity. In particular, this charcoal can contain sulfur without inconvenience.



   It is obviously necessary to bring the coal column under conditions such that it can efficiently regenerate the reducing gases rich in carbon monoxide.



   In particular, in accordance with the present invention, it is possible to bring the coal column to a suitable temperature for regeneration, by external heating, by internal heating or by combustion of this coal column itself.



   According to one embodiment of this characteristic, the gases originating from the heating of the coal column (combustion gases from burners, combustion gases from the coal column itself, etc.) are combined with the reducing gases, the all of these gases being reduced by the coal column, this assembly then being effectively applied to the reduction of the iron ore treated.



   The heating or the combustion of the coal column can advantageously be adjusted so as to control the composition of the reducing gas and hence its efficiency.



   As a result, we have a very simple way to control everything. instant the action of the gas reducing agent on the treated ore and consequently control the reduction according to the degree to which this reduction is desired (obtaining iron metal or obtaining its oxide).

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   There is an advantage, in accordance with the present invention, in effecting this heating and combustion of the. column of carbon in the presence of a catalyst, in particular iron oxides, which also makes it possible to control the composition of the reducing gas.



   This catalyst constitutes an effective means of control over the composition of the reducing gases and consequently over them. acting on the ore processed for the 'purpose explained above'.



   According to the invention, the hot reducing gases leaving the reduction furnace are advantageously applied for the heating required for the various operations of the process, such as sintering, fusion, refining, etc., which allows very extensive recovery of the calories. As a result, the thermal efficiency of the operation is further improved.



   According to an embodiment 'of the latter arrangement, the hot reducing gases leaving the reduction furnace and still containing significant contents of combustible gas such as carbon oxide or hydrogen or a mixture of the gases. two are burnt in the melting furnace. Under these conditions, total use is thus obtained of the residues of the combustible gases still contained in the reducing gases. For example if the reducing gases, after the reduction operation, still contain a certain content of carbon monoxide (CO) this combustible gas burnt in the melting furnace is thus used efficiently; the process according to the invention is thus carried out under optimum performance conditions.



   The invention obviously extends to the general combination of the two means defined above (reduction of the ore, smelting of the reduced product), whatever the particular procedures by which the ore-treated with a on the one hand and the reducing gas on the other.



   However, according to the present invention, the reduction operations (reduction of iron ore, reduction of iron sesquioxide) are advantageously carried out by stirring on the plates of a rotary kiln, the reducing gases circulating in the opposite direction to the product. treated, We thus obtain a

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 completely methodical reduction of ore and oxides treated and completely homogeneous results.



   It is practically advantageous to calcine the ore before reducing it, so as to immediately remove the volatile impurities and thereby facilitate the reduction operations.This calcination can, for example, be carried out, as well as the reduction, by mixing of the treated ore on the plate, of the rotary kiln, the hot gases circulating in the opposite direction of the product to be calcined, with or without the presence of reactants, bases NaOH- CaO - acids SO4H2, HCI- 'Halogens., lime hypochlorite etc * ...



   2 - Melting operation - in, can perform the melting simply by heating the reduced ore, in an acid or basic hearth melting furnace * However, there is advantage, according to the invention, to melt the reduced product in the presence of fluxes, facilitating the melting of the gangue and the formation of 'slag, in particular CaO, SiO2. soda MgO, acids *
After the operation of reducing the oxide of the ore, the reduced metal product is advantageously sintered, so as to agglomerate the ore before melting and thus to avoid the. dust formation and the corresponding losses. This frying, which is optional, can be carried out without increasing the fuel consumption.



   Preferably, the reduced metal product is sintered in the presence of fluxes, such as bases (CaO soda, etc.) which facilitate sintering.



     As indicated above, the melting operation makes it possible to separate impurities in the form of slag, either the metal itself or the suboxide of this metal, these two products (metal or suboxide) being able to be then, effectively processed as explained below.



   3 - Oxidation of products after reduction and fusion.



   These products are present either in the state of metal or in the state of sub-p @ yde. One can operate in one or the other way described below. First of all, according to the invention, the metal iron or the sub-xoyde can be oxidized to obtain the magnetic iron oxide De 304.

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   After obtaining this magnetic iron oxide, spraying is carried out in the liquid state, using a compressed inert gas such as nitrogen, then this oxide is poured into a liquid such as water which sta - bilise the magnetic oxide and evide its oxidation by air.



   Then, the stabilized magnetic oxide is dried, pulverized to dryness, and then delivered to the market.



   Likewise, the sesquioxide can be obtained by carrying out the oxidation of the metal or of the suboxide edited at 1200 - 1300 C.



   It is also possible, from these last 2 oxides (magnetic oxide Fe3 O4 and sesqui-oxide Fe2O3 and working by reduction, to obtain less oxygenated oxides; in particular, it is possible to reduce the magnetic iron oxide Fe3O4. to obtain the suboxideFeO, which can be stabilized by rapid cooling in water.



   These oxidation operations can be carried out in many ways, by any known means, in particular one can according to the invention, oxidize the metal iron or the suboxide by blowing in an oxidizing gas by spraying the molten product with cooling. in air, by peroxidation of the pulverized or ground solid metal in the presence of oxygen; or other similar means.



   When the reduction has been carried out until iron metal is obtained, it is advantageous, in accordance with the invention to refine the iron metal obtained by reduction of the ore hydroxide, so as to remove certain impurities (carbon, manganese , etc.) and get. a pure metal, this refining being carried out for example by blowing in air or oxygen, or by adding reagents, such as iron oxides (scale), silicon, aluminum, etc ... the refined metal is finally collected , for example by casting in ingot molds, by spraying, by injection of inert gases under pressure, by direct precipitation in water or any other means known per se.



   It is also possible, in accordance with the general process of the invention, to oxidize the metal after refining, which makes it possible to obtain very pure oxides.

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   4 - Miscellaneous operations -
As indicated above, any reduction of the iron oxides obtained by oxidation of iron can be carried out. In particular, the magnetic iron oxide Pas 04 can be reduced, as indicated above, so as to bring it back to the state of iron protoxide Skin
All these reduction operations, as indicated moreover above, can be carried out by stirring on the plate of a rotary kiln, the reducing gases circulating in the opposite direction to the treated product.



     The invention also relates to some secondary operations and characteristics which are described below:
According to the invention, the burnt gases originating from the various operations (sintering, melting, refining, etc.) are collected and they are partially or totally regenerated by reduction of these. gases' burnt, so as to obtain reducing gases and these regenerated reducing gases are applied to the reduction of iron oxide.



   As a result, both the burnt gases are recovered and they are used efficiently in the implementation of the process.



   It is also possible, in accordance with the present invention, to obtain, from liquid air on the one hand, oxygen for the production of the reducing gas, on the other hand, nitrogen for the formation of a neutral atmosphere, for example by to collect and protect the molten metal or oxide from any oxidation.



   According to another characteristic of the invention, the burnt gases coming from the various operations (sintering, melting, refining, etc.) are collected and applied to reheating operations in one or the other of the operations. phases of the process (calcination, vaporization of water, etc.). The present invention extends: a) to the general processes as they have been described in. the preamble of the present request b) all the characteristics defined above and relating to the auxiliary ventilation for the implementation of the essential operations;

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 c) to all the operating modes i.e. dsQf.l3us.



   The invention extends not only to the above methods and to their various combinations, but also to the characteristics described below and to their various possible combinations.



   The methods, installations and apparatuses in accordance with the invention are shown by way of example in the accompanying drawings in which: FIG. 1 represents an apparatus for carrying out the methods in accordance with the invention for the reduction , Oxidation, chlorination, distillation, drying, etc '...'.



   - Figure 2 shows an embodiment of the cooling of the trays - Figure 3 shows an installation for the reduction of mineral or organic products - Figure 4 shows a variant of the installation of Figure '3 with a converter for the regeneration of reducing gases.



     -'-The. Figure 5 shows schematically the converter -seur used in the installation of Figure 4. ¯ - Figures 6 and 7 show two embodiments. ti on of a reduction installation according to the invention.



   - Figure 8 shows a distillation apparatus, - Figure 9 shows a distillation or drying apparatus with vacuum pump.



   - Figures 10 and 11 are two schematic vertical sections of the whole of an installation for the implementation of a process according to the invention for the treatment of ores containing iron oxide.



   - Figure 12 is a diagram of a complete installation for obtaining iron metal and its oxides from ore.



   - Figures 13 and 14 are two diagrams of converters serving for the regeneration of reducing gases.



   - Figure 15 is a diagram of another embodiment of an installation according to the invention.



   - The calcination, reduction, oxidation processes,

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 chlorination, are advantageously carried out in the oven .represented in the. figure 1.



   This oven is made up of a certain number of horizontal circular trays 1, 2 ... 7, superimposed, forming stepped floors, completely independent of each other.



   The odd trays 1, 3, 5, 7 are fixed, while the even trays are movable around a fictitious axis coinciding with the vertical axis of the furnace * Columns also support the movable trays mounted on rollers 13 rolling - on a rail 14 fixed to said columns-
The upper fixed plate 1 which closes the oven. is covered with a suitable heat insulating coating, preventing wastage and is provided with a suitable dispensing apparatus for the product to be treated.

   An opening 15, mixed in the center, serves to evacuate the reaction gases. = 'The lower plate also fixed 7 closes the cap of a cylindrical masonry block containing the hearth, the flues 30, the ducts 31 for the reaction gas inlet and the tank 32 where the treated product falls.



   The movable plates 2, 4, 6 receive their rotational movement by means of a vertical shaft 17 carrying toothed gears 18 which mesh with the crowns-12, said shaft being controlled from above or from below, by means of of a suitable transmission-, Each plate carries, sealed in its vault, a series of teeth 20 of a suitable refractory product, which are shaped and oriented to move in the desired direction the product spread on the bottom immediately below, either from the center to the periphery, or from the periphery to the center.



   Thus, in the example shown here, the cover plate 1 carries teeth arranged and oriented to move the product supplied by a distributor to the center of the sole 2. from where it will fall on the sole-3 on which it. will circulate from the center periphery and that, by the sole fact of the rotation of the sole 2.



   'This product' arriving at the periphery falls through openings 21 provided for this purpose, on the fixed .sole 3. The

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 teeth provided under the vault 3 bring it back from the periphery of the. sole 4 to a central drop orifice 34 from where it falls on sole 5 and so on alternately from sole to sole and drop down through orifices 24, 25, 26 and 27a
The reaction gases follow a reverse path through the same orifices 27, 26, 25, 24, until the evacuation through the orifice 15,
The lower part of the furnace has burners, 34 directly above the orifice for introducing the reaction gases.



   To cool the soles, circulation is provided. of cold air or gas in the channels 35 provided in the bricks of the vault and in the teeth 20 thereof, as shown in Figure 2.



   The circulation of the cooling fluid can be caused in the movable soles, for example each time the orifices of the channels pass in front of a suitable suction or discharge orifice; the air or the circulation gas thus reheated in the. crossing of said channels that can be used in product processing plants.



   Heating can be direct or indirect depending on the. material to be treated and can be carried out on one or more trays or on all of the fixed trays, all fuels being able to be used for this purpose.



   The regularization of the temperature in the mass depends above all on the thickness of the product placed on the trays and is all the more perfect as the thickness of the product is lower. The scraper teeth 20 make it possible to equalize the thicknesses of the products.



   Pulverulent materials can also be carried out as treatment, either dry distillations of sawdust or small pieces, or fu.si6ns, or cause entrainment by water vapor, by inert fluids or by suitable solvents.



   The reaction agent can, to a certain extent, be circulated in a closed cycle, in order to reduce its consumption.



   Likewise, simultaneous or successive reactions, - or alternating, for example oxidation and reduction reactions, can be carried out in the same apparatus, even at different

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 temperatures; for this purpose, -e ** -UO2; this & iictes oxidizing and reducing agents are provided in different zones of the oven.



   For the. calcination, heating is provided by burners 34 located at the lower part of the furnace, or possibly at the level of each fixed hearth, the fumes passing through the furnace in the opposite direction to the material.



   3, The output of the last bottom hearth, the material can be brought into contact with the flames, for one. more energetic treatment.



   The clacination can also be carried out on the raw material to which is added, either a flux or a body or a mixture of defined bodies, with a view to carrying out side reactions. Thus, for example, it is possible to add chlorinated compounds to an ore, in order to render mineral impurities soluble and easily removed by washing.



   Products containing zinc can also be purified in the same way. The zinc is volatized in the form of an oxide which can be recovered directly at the outlet of the apparatus.



   For the reduction, the previously calcined material is preferably used in order to remove volatile impurities.



  This material is brought into the reduction furnace 40 according to that shown in FIG. 1.



   The reduction furnace 40 is placed under the calcination furnace 41 (FIG. 3) which makes it possible to eliminate the handling equipment from one furnace to another, the material circulating by gravity.



   The reduction furnace 40 is brought to the desired temperature.



  The reducing baz is circulated as indicated above by introducing it through the orifice 31.



   This reducing gas is generally hydrogen. Hydrogen can be obtained by dissociation of water vapor in the furnace itself. For this purpose, water vapor is injected into the bottom of the oven, through the opening 31.



   However, remarkable results can be obtained by carrying out the reduction with carbon monoxide which is then regenerated in a converter 42 ..



   To this end, the carbon monoxide CO is passed over the oxide to be reduced., In the reducing furnace 40, for example iron oxide Fe2 O3, The reaction is carried out as

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 next: 3 fe2o3 + CO = 2 Fe3O4 + CO2
The carbon dioxide obtained is then sent through a pipe 45 into the converter 42 (FIG. 4) where it is transformed into carbon monoxide on contact with the carbon, the reaction being incandescent as follows:
CO2 + C = 2 CO
The carbon monoxide thus obtained is sent in part through the pipe 44 into the reducing furnace 40 where it performs the previous reduction and the cycle begins again.

   The converter. 4 ?. where the production of carbon monoxide from carbon dioxide takes place is advantageously constituted as follows (FIG. 5) It comprises at its upper part a sealed airlock 51 for the continuous supply of gas. coal and at the lower part a grid 52 and a scrub door 53. The converter 42 is heated externally by the burners 541 542 543 544 supplied with gas or any other fuel.



   These burners 54 are located on different stages, which makes it possible to produce zones of different temperatures. the gas to be treated is brought to a. the lower part 55 of the converter 42 and travels from bottom to top through the coal where the catalyst is maintained at the desired temperature by the burners 54.



   The thus treated leaves at the top of the converter and is led downwards by a pipe 56 to be then directed into an exchanger 57 where it gives up all or part of its calories to the gas to be treated before being fed. at the bottom of the converter 42.



   In effect, the gazdevant-being treated arrives at the upper part of the exchanger 57 via a pipe 58 and circulates through a series of parallel tubes 59 in .la. room of. cooling 70 of the treated gas.



   For the reductions, a mixture of hydrogen and carbon monoxide in the form of a water gas, for example, can also be employed as a reducing gas.



   This gas of composition x CO + y H2 can be fegenerated in the same way as CO gas by passing through the converter.

 <Desc / Clms Page number 20>

 sor 42.



   Depending on the composition of the reducing gases and the. reaction temperature, one can obtain in the example of the oxide of
 EMI20.1
 iron Fef 0 the whole range of spells-oxides, salt oxide, diva.- slow oxide or even pure iron which can be melted down.



  , According to another embodiment (FIG. 6) the fumes from the burners of the converter 42 are used to carry out the calci-
 EMI20.2
 previous nation of ¯1 'o.:; Danemarkyde in the household. for this purpose, the scaffolding gases: 1t from the converter 42 are directed by the pipe 46 at the inlet of the calcination furnace 41. The circulation of the reducing gas is ensured by a ven'bil: J.-alU '47.

   We. thus recovers càïlor '- ,, which leads to excellent thermal efficiency and to a very simple operation of'! tizistaJ¯7 a tian. In fact, the degree of reduction of the oxide is a function of the temperature and of the concentration of reducing gas in the gaseous phase which is itself a function of the temperature of the converter 42, the operation of the installation comes down to maintaining temperatures
 EMI20.3
 of each ràaculorre
Thus, in the particular case of the manufacture of magnetite, from iron sesquioxide with carbon monoxide,

   the reduction can be made around 600 650 with a
 EMI20.4
 gaseous composition of carbon 4-doyde 00 and 60% of carbon dioxide CO 2 '- The converter temperature is of the same order, the reducing gas carrying out a closed circuit.



   According to another embodiment, a mixture is sent. carbon dioxide and carbon monoxide in the reduction furnace (40) figure; through tubing 48. To recover part of the
 EMI20.5
 gas mixture after the reaction in the. reduction furnace 40, the. converter 42 in bypass on the circuit of the reduction furnace 40. The carbon monoxide obtained in the converter 42 is then introduced through the pipe 49 in the desired quantity and
 EMI20.6
 determined in the reduction furnace 40 with the mixture of carbon monoxide and carbon dioxide introduced into the cycle.



   An oxide freed from its volatile impurities by calcination can be obtained in this installation which, on reduction, gives a very pure magnetite. The purity of this magnetite.,

 <Desc / Clms Page number 21>

 is further improved if the charcoal used is charcoal.



   Pure magnetite regenerated according to the foregoing methods can be used for the preparation of hydrogen. To this end, a stream of water vapor is sent over the magnetite brought to red which oxidizes releasing hydrogen, the oxidized product then being regenerated by reduction, the two operations being able to be carried out in the same apparatus. As indicated above, the reducing agent can be either carbon monoxide, or water gas, or a mixture of the two gases. Either of these reducing gases are prepared from carbon dioxide or 1a. water vapor in the converter 42.



   The hydrogen produced is very pure because the reducing gas itself can be very pure. Magnetite retains its properties for a very long time. The thermal roundness of the. The transformation is very high, the heating of the hydrogen generator being able to be provided by the fumes coming from the converter 42, as well as by the excess carbon monoxide from the 'conversion of carbon dioxide, or by the excess gas to water from the water vapor introduced into converter 42; depending on the reducing gas used.



   FIG. 8 represents an apparatus for carrying out the distillation process according to the invention.



   This device behaves, like the oven of the. FIG. 1 of the fixed plates 1, 3, 5, 7 and of the rotary plates 2, 4, 5 rotating opposite the fixed plates. These plates are hollow and are traversed by the heating fluid of the. water vapor for example.



  The distillation products go to the upper part of the apparatus where they are evacuated with a view to their condensation. This apparatus is advantageously used for the dry distillation of small pieces of wood or sawdust, as well as for the treatment of seeds and wood waste.



   This apparatus can also be used as a dryer to dry, for example, in a neutral atmosphere. or reducing wet magnetite or any other products:
The water vapor is eliminated at the top of the appliance. To decrease the drying temperature, a vacuum pump 64 performs a vacuum in the enclosure. relative (figure 9).

 <Desc / Clms Page number 22>

 



   Installations are thus produced which make it possible to carry out all kinds of reactions with an improved thermal balance thanks to the devices for recovering the heating gases and the reaction gases.



   Figures 10 and 11 show another invention for carrying out a process according to the invention for the treatment of ores suitable for iron oxide?
A melting furnace A is heated by burners B supplied by a gas supply conduit C1 and arc C2. These burners are set so as to maintain a temperature in the oven of 1700 to 1800 o C.



   The loading of the treated ore is effected at D, immediately above the level of the. melted mass in the oven; therefore, the formation of ore dust by the flue gases is reduced to the minimum possible. This loading is carried out either continuously or discontinuously.
This loading can be carried out in multiple ways: first of all, outside the furnace, a mixture between the iron ore and the flux can be carried out and the mixture thus prepared in D introduced into the chamber of the furnace above the free level of molten oxide.



   One can also bring directly and separately in D in the furnace on the one hand the ore and on the other hand the flux.



   The tank of the for A has two superimposed orifices E1 E2 one (E1) ensures the evacuation to the outside of the slag formed on the upper surface of the bath, while the other (E2) ensures the evacuation of 'molten metal oxide.



   The slag thus separated is treated by known methods, for example by granulation in a body of water.



   The molten oxides are collected through the orifice E2 and are then subjected to cooling under the conditions indicated above; in particular these oxides are subjected to sudden cooling so as to obtain Fe3 04 (magnetic oxide). The molten oxide can be brought to a highly divided state by the action of an inert gas under pressure.



  The fumes from the. fuel combustion

 <Desc / Clms Page number 23>

 of the burners B passing at their exit from the furnace field A in inversion generators G1 G2 where they. abandon their sensible heat which is used for preheating the fuel gas and the combustion air to obtain the required operating temperatures according to known methods.



   In the case where the process is applied to pyrite ash resulting from the combustion of sulfur, the installation in accordance with the invention and shown in the attached drawing, is independent of the pyrite roasting furnace or immediately arranged. - ment following the toasting oven. It is also possible to obtain by the combination of the devices described above, the whole range of iron oxides.



   Numerous modifications can be made to the method and to the installation described above by way of example, in particular the sensible heat of the fumes at the outlet of the Gl @ 2 regenerators can be used. dehydration, preheating the ore to be melted, drying the finished product, etc.



   The process according to the invention can be applied to iron ores of very different naters, in particular it can be applied to the treatment of pyrite ash which is used as such, without any prior grinding.



   For the manufacture of magnetite, from sesquioxide, it is not necessary to maintain the reducing medium by injecting water vapor or hydrogen, or Co or carbon in the presence of air, because, above the melting temperature of magnetite (1500/1600 C) iron sesquioxide dissociates into magnetite and oxygen.



   Under these conditions, it suffices to keep the temperature of the oven at 1600 0 minimum. However, as solid solutions (Fe304 - Fe2O3) can form, it is advisable to inject, if necessary, into the laboratory of the furnace containing molten oxygen, an inert gas or a reducing gas, in very small quantities. to reduce the small amount of Fe2O3 kept in solid solution
Iron protoxide FeO can be obtained from Fe2O3 or Fe3O4 from the smelting of the ore according to the present invention, by subjecting the latter to reduction by CO or

 <Desc / Clms Page number 24>

 hydrogen for example.



   Conversely, by subjecting the protoxide FeOa to oxidation
 EMI24.1
 we can get the. magnetite Fe04 or sesquioxy-de a S FeO ..



  Ores containing an infusible oxide, such as alkaline earth carbonates, or hydrates for example, cannot be processed.



   To facilitate the separation of the gaague and the oxides with these ores, it is possible to decompose the carbonate and the hydrates sprayed beforehand in a flame before bringing them to an oxidative fusion according to the process; in accordance with the invention,
 EMI24.2
 If finally with regard to the embodiments of the present invention, all the systems of the furnace can be used.
 EMI24.3
 sés, provided that they are arranged in such a way as to allow complete melting of the ore. it is thus, for example, that the turbulence furnaces, I: s rotary furnaces, 1'0.o: 1: 'g with crucibles,: tc. on- can be used after àtdapti) Lo ± ù-.



  If there is electrical energy, the treatment
 EMI24.4
 This can be done in any electric oven, either continuously or discontinuously.



   FIGS. 13 to 15 represent a general installation for obtaining metal iron and its oxides from ores, according to the processes in accordance with the invention.



   The overall installation shown in FIG. 13 comprises groups of devices which follow one another in the order corresponding to the operations of the process, such as
 EMI24.5
 that they were previously described * The following description follows the following order: 1 - Circulation of the treated ore, 2 - Circulation of various gases.
 EMI24.6
 



  The crude mineral <1 brought to 1 and ljrllé in 2 undergoes in 5 a dehydration and calcination operation, this calcination having the effect of depriving the ore mw: 5d * n, tercw> t of all its volatile impurities * This dehydration operation and calcination:,. preferably in a rotary plate kiln, the ore being stirred
 EMI24.7
 sur'ce p-lataaae while the heating gases flow in direction

 <Desc / Clms Page number 25>

 Reverse of this minera. 1.



   The ore thus dehydrated and calcined is brought to 4 in. a reduction furnace, for example, a rotary plate furnace, the ore to be reduced on the one hand, the reducing gases on the other hand, circulating in the opposite direction to each other *
The ore thus reduced, for example, to the state of metallic iron or iron suboxide, is sintered at 5, so as to agglomerate the ore and to avoid any formation of dust and the corresponding losses.



   The ore thus agglomerated is then brought into a melting furnace 6, in which it is advantageously possible to add fluxes such as bases, to facilitate the melting of the gangue and its separation. This melting furnace thus makes it possible to separate: a) at the upper level the slag or slag coming from the gangue discharged at 10 and used for example to form agglomerate bricks or all other applications * b) reduced metal products, these products being constituted, for example, by metal or by an oxide of the metal.



   The molten metal is brought at 7 into a refining furnace in which the treatment is carried out, for example, by blowing in air or by injecting reagents such as iron oxides, scale, silicon, magnesium, aluminum, etc. the refined iron is finally collected at 8. It can in particular be collected by pouring into the ingot molds, by spraying, by injection of pressurized gasoline, by direct precipitation in water or any other known means.



     The slag is discharged at 9 and used for all desired purposes.



     If one wishes to obtain oxides plus oxides from the metal or the iron suboxide, the metal product from the fusion 6 is brought into an oxidation furnace 11 in which the metal product is treated by any means suitable, in particular by blowing in an oxidizing gas, spraying or molten product with cooling in air, peroxidation of the solid metal sprayed or burnt in the presence of oxygen, etc.



   In particular, by this oxidation it is possible to obtain

 <Desc / Clms Page number 26>

 
 EMI26.1
 magnetic iron oxide Fe 0, then ofi pulverizes this liquid magnetic oxide FeO4 with the aid of a compressed inert gas such as nitrogen, then this oxide is poured into a liquid such as water, this
 EMI26.2
 . which stabilizes the EN-genetic oxide and avoids its oxidation. by water.



  This separation operation of the magnetic iron oxide
 EMI26.3
 is carried out in 12. .r¯rès stabilization of this mgnetic iron oxide; it is dried in 13, it is pulverized with zec by a suitable grinding1 in 14 and finally it is conditioned in 15, so as to bring it to a state where it can be directly delivered to the cOIr ... t: 1ercè-.



   Cn. Can also perform wet grinding. followed by draining and drying.



   The various gases which come into play in the previous installation circulate as follows:
 EMI26.4
 First, a gas generator rich in carbon oxides and hydrogen 16 is supplied at the i by a stream of water vapor coming from a heater 18 and at 19 by a stream of oxygen coming from gas bottles. liquid air 20, a gas rich in carbon monoxide-and-hydrogen is formed in this generator, this richness being able to reach 80 to 90% and even more if necessary.



   This gas is thus sent to the reduction furnace 4, the use of oxygen pour'la. formation of this reducing gas' thus makes it possible to obtain this high carbon monoxide content allowing
 EMI26.5
 itself the reduction under conditions of low tempsra.ture and therefore under conditions of optimum thermal efficiency.



   The gases flowing from the reduction and leaving the reduction furnace 4 in 21 are used at 22, 23 and 24 for the heating required by the sintering, melting and refining operations. As a result, these gases are stripped of most of their heat. ries and the yield of the entire process is increased.
 EMI26.6
 



  The flue gases leaving these a 1-ittage, smelting and refining apparatus are connected at 25, pass into the regenerator of the melting furnace 10, then into the dehydration and calcination furnace 3; then, in the boiler 18 and finally in an economizer 26, in which these gases are stripped of the major

 <Desc / Clms Page number 27>

 part of the calories which they still contain ;, finally these gases are evacuated at 27 towards the. ' fireplace.



     The recovery thus effected is pushed to the extreme limit; in practice, the gases are evacuated to the atmosphere at 27 at the outlet of the economizer 26 at a temperature. at most equal to 150 whereas -these gases, at their exit from the .fusion furnace were at a temperature of 1750 to 1800 o / De made.on obtains a very thorough recovery.des calories from the reducing gases.



   The steam produced in the boiler 18 can be used not only for the formation of the hydrogen-rich reducing gas, but also for any other applications required by the installation. In particular, this steam can be directed at 28 to the dryer 13 and ensure there in a closed vessel, following the release of heat from this steam, 1 the drying of the wet magnetic iron oxide and -from the stabilization apparatus. .



   The water vapor given off in this drying apparatus is fed at 29 into a condenser. is condensed therein, and can be, at the same time as the purge water, sucked by a pump 30 and delivered at 31 into the economizer 26 and into the generator boiler 18.



   On the other hand, the liquid air cylinder 20 which produces the oxygen supplied at 19 into the gas generator thus makes it possible to obtain gas rich in carbon monoxide and gives birth at the same time. significant amounts of nitrogen that can be used in the previous installation at all points necessary to create a neutral atmosphere, in particular, this nitrogen can be used in the device 12 for the stabilization of magnetic oxides, as well as in dryers 13 for drying the magnetic oxide coming from the stabilization apparatus.



   Ultimately, the liquid air 20 is totally used both by its oxygen and by its nitrogen.



   Numerous modifications can be made to the overall installation shown schematically in FIG. 13. In particular, a device which makes it possible to regenerate the gases after a first reducing action on the ore can be produced in many ways. A regenerator allowing

 <Desc / Clms Page number 28>

 
 EMI28.1
 the planned regeneration is shown below and by way of example in Figure 14.



  This regenerator device consists essentially of a carbon column. 32 heated externally: this contribution of cbaleur is intended to compose the losses pir the radiation of the apparatus and to supply 11 energy necessary for the endothermic reactions, of which it is the sièG3: reduction of. Goy to CO; due to the water vapor in E2 and GO, crack1 !!.!;, 7 rt.y üxo-- carbide .etc ....



   The coal column is crossed by the current of
 EMI28.2
 gas to be regenerated: this effect, column 32 is loaded with alternate layers of carbon 33 and catalysts 34; for example iron oxide. These loads are carried out by airlock 35
 EMI28.3
 arranged at the top of the. column 3w and allowing the interruption of the charges of carbon and catalysts, without occurring pax following the release of ga-z ether to the outside.



   The heating of the charcoal column 32 is provided by an outer casing 35 in which the heating is provided, for example, by air or oxygen burners 36.



   The gases to be regenerated, that is to say, the gases coming from the reduction furnace and in which a significant quantity of oxide
2 de.carbon CO has been transformed into carbon dioxide C0. and brought to 37 at the bottom of the coal column 32. This gas stream rises vertically along f.ldans the coal column; carbon gas
 EMI28.4
 bonique CO2 and reduced in the carbon to the form of oxide of aarborie CO:
C + CO2 = 2 CO
Likewise, the water vapor supplied to 39 is reduced by carbon and transformed into carbon oxide and hydrogen according to the formula:

      
 EMI28.5
 H0 + C-CO + H2
We. ultimately obtains at the upper part of the coal column at 38, a regenerated gas rich in carbon monoxide and in hydrogen, i.e., a gas which has recovered most of its reducing parts and can thus be

 <Desc / Clms Page number 29>

 used again in the reduction furnace.,
In converters, the coal column therefore fulfills an essentially chemical role (reduction), and not thermal (combustion) the heat necessary to carry out the reactions being supplied by the burners.



   The 'fumes coming from the heating chamber 35 and leaving at 40 can be reintroduced at 41 into the air stream of gas to be regenerated, penetrated with it into the coal column 32 and thus increase the total volume of gas to be regenerated.
 EMI29.1
 



  This increases the total yield of i'ins.tail a.tiont.



  Likewise, part of the reducing gases which are gases
 EMI29.2
 rich in chp-rboi-i oxide and hydrogen and which, therefore; have a very high calorific value, can be supplied in 42 Ds.ns air or oxygen burners and participate in the combustion
 EMI29.3
 tion of these burners by ensuring the cl-iÉituf: CL5kre of the assembly 35 and consequently the cl-iouffp: ge-of the coal column 32.

   Mid effect 1 & r> 5G: bnéu? *. TJ.on ou ga.z treated leads to an increase in the total gas volume, which makes it possible to use the excess of the converted gases for any auxiliary application, for heating of. converter itself. The converter
 EMI29.4
 FIG. 14 finally comprises a device. 52 d: v.cLZ :: tiou des ashes continuous or intermittent operation.
 EMI29.5
 



  Numerous modifications can be made to the converter shown in schematic figure 14 '. In particular another mode of r6allàauloii.de this converter is shown in FIG. 1'5. This conuertisse.ur comprises a coal column 32 with alternating layers of fuel and catalyst 32 and 11. These successive layers of char-
 EMI29.6
 bon and catalytic converter are loaded by the etolliche 35 airlock.



  The gas to be regenerated rich in -1 ggz carbon dioxide CO 3 is fed to 37 ;. the water vapor necessary for the foriiiation of the gas to water by reduction of the vapors by charcoal is supplied to 39; the regenerated gas comes out at 38,
Instead of providing external heating of the converter, by an external casing 35,
 EMI29.7
 in the converter of figure 15 a heater, internal

 <Desc / Clms Page number 30>

 
 EMI30.1
 of the. coal column. To this end, de't4 opening into the very interior of the column 32 of the converter and thus ensuring the heating to a suitable temperature of this column.



   The overall operation of this converter is
 EMI30.2
 quite similar to that of the converter already described with the aid of figure 14.



  '3n varying modes of c: i.1auff.:; E da convortissur above described [;, we can achieve the contribution of C'-ilc? T¯ "necessary by the direct combustion of a ps-rtie 1JDiz 32 stain either with 1 1 air or with oxygen.



  In this case, the functiom: .3-r.ant, dù. C (} l1.v0:;. 'TisB': H.ú: is similar to that of -: = zoane dsrs which cho: r :::: 1 ra.r¯3iL a double role of fuel. And of reducer, aV0, however the following light: it is that the reduction only applies to the Garbonic gases providing for the combustion of coal and to the water prior to a possible injection of steam to equalize -t on the gases to be converted which pass through the carbon layer brought to the required reaction temperature 'L FIG. 16 represents a diagram of an overall iistallation in accordance with the invention: but very simplified .



  This facility operated at the. the following way: the mine-
 EMI30.3
 line of iron undergoes in 4 a reduction in the conditions already indicated; it then undergoes fusion in 6.



   The gases follow the following circuit: the gases leaving
 EMI30.4
 reduction furnace 4 in 45 anxied reduction to -a conception of about 60% carbon oxide and hydrogen. These gases are burnt in oxygen burners 46 and thus ensure the fusion in 6 of the previously reduced ore.



   The gases are thus burned and transformed into non-combustible gases, namely carbon dioxide CO2 and water vapor H2O which exit at 47 from the melting furnace.



   The purity of the converted gases being above all a function of the purity of the carbon used, it is possible, if harmful impurities accumulate in the circuit, to eliminate or maintain them.
 EMI30.5
 . their percent-ge.co, istsnt by performing continuous purges 7

 <Desc / Clms Page number 31>

 or discontinuous as indicated in 48.



   The gases then pass through a dust collector 49 to get rid of the entrained ore dust ,, Ves gases which must now be regenerated are admitted at 37 into a converter 50 exactly conforming to that shown in FIG. 15.



   The regenerated gases and containing a proportion of 8 to 90% of carbon monoxide and hydrogen finally exit at 51 and return to the reduction furnace '.



   A completely closed gas circulation circuit is thus produced.



   'Ultimately, the installation of figure 16 represents characteristics quite similar to those of the installation of figure 13.,
However, this installation is greatly simplified and includes only the two essential operations! a) reduction of the ore; b) smelting of the reduced ore.


    

Claims (1)

CLAIMS 1 - Process for the reduction of mineral or organic products with a view to their purification or their transformation, characterized because the product to be treated is stirred on superimposed trays and this product is dropped from tray to tray in as it is stirred, while the reducing gas is circulated between the plates, which facilitates the reduction owing to the large contact surface between the. reducing gas and the litter to be treated, this process thus making it possible to process large quantities of products in a space-saving enclosure * 2 - Process according to claim 1 and charac- terized 'because the product to be reduced is first calcined in order to remove volatile impurities' by stirring the product to be treated on superimposed trays and by dropping this product from the tray into tray as it is brewed, while <Desc / Clms Page number 32> EMI32.1 that one. circulated. hot gases between platBaL #. Said product is then dropped onto the first reduction plate and is then caused. reduction in accordance with the previous paragraph. 3 - Method according to one of claims 1 or 2 characterized because qufon regenerates the reducing gas by the action of a catalyst or glowing carbon. 4 - Method according to one of claims 1 to EMI32.2 3 characterized because it sends the fumes from the regeneration chamber. reducing gas on the product to be treated to calcine it before the reduction operation, which improves thermal efficiency. 5 - Method according to one of claims 1 to 4 characterized because quton sends part of the reducing gas to EMI32.3 fégenerate on the product to be reduced, while re-generating 112-Lu, re part before sending it to the product to be reduced. 6 - Method according to one of claims 1 to 5 for the manufacture of hydrogen characterized because one 'sends a stream of water vapor on iron or one of its. oxides such as magnetite which combine with oxygen in the water, liberating EMI32.4 1-iydrogen, a, the oxidizing product being regenerated by reduction su! - EMI32.5 before the procedures in accordance with one or other of the preceding paragraphs: 7 - Process according to one of rsvendlication4 from 1 to 5 for lshaZôgination of mineral or organic products for their purifica-tion or their transformation characterized because the product to be treated is brewed on. trays'-saper- posed and that this-product is dropped from the plates!, in tray EMI32.6 as the stirring progresses, that the halogenating gas is made to circulate between the plates, which favors the halogenation, as a result of the large contact surface between the halogenating gas and the material to be treat; this process thus permitting to treat large quantities of products in a space-saving enclosure. 8 - Method according to one of the claims of EMI32.7 1 to 5 for the chloride & 1on of mineral or organic products <Desc / Clms Page number 33> with a view to their purification or their transformation characterized because the product to be treated is stirred on trays, superimposed and this product is dropped from tray to tray as it is stirred, while the the chlorinating gas is circulated between the plates, which promotes chlorination due to the large contact surface between the chlorinating gas and the material to be treated, this process thus making it possible to treat large quantities of products in an enclosure reduced footprint *. 9 - Process according to one of claims 1 to 5 for the. calcination of mineral or organic products with a view to their purification or their transformation in which the product c treat is stirred on superimposed trays and is done. This product falls from tray to tray aufur and as it is stirred, while the hot calcination gases are circulated between the trays, a calcination process characterized, because the hot calcination gases are produced at different stages of the tray and at well-determined temperatures for each of these stages, which makes it possible to adjust the temperature of the product to be treated under the best conditions, according to the combinations that are to be produced at the different stages. 10 - Process according to one of claims' from 1 to 5 pour'la distillation of mineral products or orge.niques for their purification or their transformation characterized in that the product to be treated is stirred on Superimposed trays heated internally by a circulation of heating fluid and that this product is dropped from tray to tray as it is stirred. The products of distillation amounting to. through the trays to be then condensed. It * - A method according to one of claims 1 to 5 for the drying of solids, characterized because the brewed. material to be dehydrated by superppsés trays, internally heated by a circulation of heating fluid and which this material is dropped from tray to tray as it is stirred, the dehydration vapor rising through the trays to be evacuated. 12 - Method according to one of the claims of <Desc / Clms Page number 34> EMI34.1 1 to 11 and characterized because we carry out the previous-oper9.Ìorls! at a pressure lower than atmospheric pressure. 13 - Process according to one of reven # i & ations from 1 to 12 and characterized because the thickness of the layer of treated product is variable depending on the reactions to be carried out. 14 - Method according to one of claims 1 to 13 and characterized because the heating of the product is carried out on part of the trays. EMI34.2 15 - Process according to one of reveniicRtions from 1 to 14 and characterized because the gases intended for the treatment of the product are brought into contact with the product on part of the plateaux. 16 - Method according to one of claims 1 EMI34.3 to 15 and characterized because each plate or series of plates is heated separately so as to obtain defined temperature zones on each plate, which makes it possible to carry out various successive or simultaneous reactions each corresponding to one or EMI34.4 several temperature zones. 17 - Method according to one of claims 1 to 16 and characterized because quron circulates a fluid of EMI34.5 cooling in certain trays so as to absorb heat on the trays where the reactions are exothermic, which makes it possible to limit the reaction temperature and also to ensure the conservation of the material used. EMI34.6 .8 - Process according to one of claims 1 to 17 and characterized because catalysts are incorporated in the product to be treated or in the gaseous fluid, of: n.az2iée promote the reactions and increase their speeds * 19 - Process according to the 'one of the révendicelûiona from 1 to 18 and characterized because a mixture of different products to be treated is circulated from top to bottom in several ap- EMI34.7 such mounted in series one below the other and in which the various necessary gas streams are circulated 58.ires, the mixture of products' to be treated circulating through i; ¯vi ty. 20 - Process in accordance with one of rev611dlicatio, 1S from 1 to 19 and characterized because the rate of rac- tion is controlled by varying the rate of stirring of the products <Desc / Clms Page number 35> EMI35.1 processed on the trays, the speed adjustment a. a very low value allowing reactions to be carried out on pu1verulent forend, while reducing dust concentration. 21 - Compliant process. to one of the revenàioations.s from 1 to 20 and è% .racLéris "5. par. that the products to be treated are brought to the powdery state to facilitate the reactions which thus become faster and more complete. EMI35.2 22 - Process according to one of claims 1 to 21 and characterized because the reaction gas flows low ct h ^ i: 'i. f: i1. direction iJ1oVr8;: 7 du..produ.i to be treated, which achieves a methodical circulation and makes it possible to best adjust the temperature differences between the reaction gas, and the product at trw3.t3r 23 - Installation for the reduction of product according to the processes of claims 1 to 22 or similar processes and characterized by a calcination furnace (41) purifying, first the product to be reduced and a reduction furnace ( 40) say EMI35.3 placed under the calcination furnace so that the product to be treated circulates by gravity from one furnace to the other. 24 - Installation for the reduction of product according to claim 23 and characterized because the gases leaving the reduction furnace are sent to a converter (42) which regenerates the reducing gas by the action of the catalyst or incandescent carbon '. 25 - Installation according to claim 23 and EMI35.4 characterized by the fact that the fumes coming from the converter (42) for regenerating the reducing gas are sent to the calcination furnace (41) as a calcining agent, which allows al11é -: - to improve the thermal balance of the installation .., v 26 - Establishment according to one of the claims. from 23 to 25 characterized because part of the gases leaving the reduction furnace (40) is returned to the inlet of this furnace, while the other part is regenerated in the converter (42) before its introduction into the reduction furnace (40). 27 Distillation or drying apparatus for carrying out the process in accordance with claims 23 to EMI35.5 25 and aLi7 similar methods and characterized for plates (rotating between the fixed plates, the plates <Desc / Clms Page number 36> EMI36.1 rotary sweeping the product to be distilled pulley le4ce? cre from plate to plate, these plates being traversed by a heating fluid to bring the product to the temperature of distillation or drying. 28 - Apparatus according to claim 27 and characterized because the heating fluid is steam or hot water under pressure in a closed circuit. 29 - Apparatus according to one of claims 27 or 28 and characterized by a vacuum pump which creates a partial vacuum in the distillation or drying chamber in order to reduce la'temps- rature of the operation. 30 - Process for the treatment of ores containing iron oxide; characterized because 11-the ore is heated until complete fusion, so that the impurities constituting the gangue are scarified, float the mass of molten oxide and are thus easily separated from this oxide. 31 - Process according to claim 30 and characterized because one adds to the treated ore un'fondant lime, soda, silica for example. 32 - Method according to one of claims 30 to 31 and, characterized because one operates in an oxidizing medium to obtain iron sesquioxide. 33 - Method according to one of claims 30 to 32. and characterized because one operates, on the contrary, in a slightly reducing medium to obtain iron protoxide FeO or magnetic oxide Fe3O4, so as to eliminate as much as possible in this case, the sesquioxide of iron, 34 - Process according to one of claims 30 to - 33 and characterized because one subjects the molten iron oxide to a sudden cooling to the ordinary temperature away from air to obtain Fe3O4 at a slower cooling for example, in the ambient medium to obtain Fe2O3 and 8 a cooling, from a temperature of 7000 minimum rapid and abrupt as for Fe3O4 when we want to obtain FeO, 35 - Process according to one of claims 30 to 34 and intended for the case of ores containing metal oxides <Desc / Clms Page number 37> volatile chemicals, for example zinc oxide, a process characterized by first heating the ore so as to remove the volatile oxide which is then recovered by condensation, then treating the residual ore by the preceding processes. 36 - The installations for carrying out the processes / according to claims 30 to 35 and similar processes and in particular a melting furnace comprising burners, .un .. device 'for loading. ores ,. a smoke evacuation duct and two orifices, one for the outlet of the slag, the other for the outlet of the molten oxide. 37 - Process for obtaining iron metal 'and its oxides from the ore characterized because the ore oxide is first reduced to the state of metal' or suboxide,. The reduced product thus separates the metal or the suboxide from the impurities, and these impurities are effectively removed in the form of slag. 38 - Process according to claim 37 and characterized because after having separated the iron metal or the suboxide or the oxide so as to obtain an oxide with the desired content of oxygen (FeO Fe3o4 Fe2O3). 30 - Process according to claim 38 and characterized because the metal iron or suboxide is oxidized until the iron peroxide (sesquioxide Fe2O3) is obtained, that is to say the oxide with a maximum oxygen content. 40 - Process according to claims 38 or 39 and characterized because the oxides obtained are reduced and in particular the iron sesquio Fe2O3, so as to obtain an oxide in a less oxidized stage and in particular the magnetic oxide from 37 to 40. 41 - Process according to claims 37 to 40 and characterized because reducing gases with a high carbon monoxide CO content (preferably greater than 60%) are applied to the reduction of iron ore, which makes it possible to carry out reduction at relatively low temperatures. 42 A method according to claim 37 and characterized because the reducing gases are produced by passing oxygen instead of air over the carbon. 43 - Method according to one of claims 37 to 42 <Desc / Clms Page number 38> . and. characterized because the reducing gas is hydrogen. 44- Method according to one of claims 37 to 43 and characterized by raw reducing gases are rich in carbon monoxide and hydrogen, these reducing gases being obtained for example by passing water vapor over incandescent carbon d 'or formation of a gas in water 45 - Method according to one of claims 37 to 44 and characterized because the water vapor obtained in the process is applied in part to the manufacture of reducing gases and in part to any other operation, for example drying the metal or oxides. 46 - Process according to one of claims 37 to 45 and characterized because the reducing gases are passed over the iron ore to reduce it, then these gases are regenerated and they are made to pass again through iron ore, these gases thus circulating in a closed cycle which ensures a completely methodical reduction of the ore and perfectly homogeneous results. 47 - Process according to claim 46 and characterized because the reducing gases rich in carbon monoxide are regenerated by passing them through a carbon column. 48 - Process according to claim 47 and characterized because one, brings the coal column to a temperature suitable for regeneration, by external heating, by internal heating or- = by partial combustion of this coal column it-. even. 49 -. A method according to claim 48 and characterized because the gases from the heating of the coal column (combustion gases from burners, combustion gases from the coal column itself, etc ...) are combined with the reducing gases, all of these gases being reduced by the coal column, this assembly then being effectively applied to the reduction of the iron ore treated. 50. ' Method according to one of claims 47 to 49 and characterized because the heating of the combustion of the charcoal column is regulated, so as to regulate the composition of the reducing gas and consequently its efficiency <Desc / Clms Page number 39> EMI39.1 51 L Process according to one of re46àa4ifside 37 to.> 50, and characterized because this heating or combustion is carried out EMI39.2 There is no catalyst, in particular iron oxides, which can still control the reduction of the reducing gas. 5? Process according to one of claims 37 to 51 and characterized because the hot reducing gases leaving the reduction furnace are applied for the heating necessary for the EMI39.3 various pro operations (ed6., such as' sintering, fusion, refining, etc ... which allows very advanced calorie recovery * 53 - Compliant process%. Claim 52 is characterized because the hot reducing gases leaving the reduction furnace and still containing significant contents of combustible gas such as carbon monoxide and hydrogen are burnt in the melting furnace. 54 - Process according to one of claims 37 to 53 and characterized because the reduction operations are carried out EMI39.4 (reduction of m1ner:; d of iron reduction of sesquioxide of fier) by brewing: .a on the trays of a retif furnace, the reducing gases circulating in reverse sound of the isated product. 55'0- A method according to one of claims from 'A7 to 54 and characterized because the ore is calcined before reducing it, so as to remove the volatile impurities, of yreference in the presence of reagents such as bases . 56¯- Method according to one of claims 37 to EMI39.5 55 and characterized because we melt the product faallit-int the fusion of 1s. gangue and formtlo, no slag. 57 - Process according to one of the revendi.ca'bol1'S dē 37 to 56 and characterized because after the operation 'reduction, the reduced metal product is sintered so as to agglomerate the ore before melting and to thus avoiding the formation of dust and the corresponding losses * 58 - A method according to claim 57 and characterized -because your sintered metal product reduced 'in the presence of EMI39.6 fluxes, such as, bases which facilitate sintering <Desc / Clms Page number 40> 59 - Process according to one of claims 37 to 58 and characterized because the iron metal or the suboxide is oxidized to obtain all the oxides and in particular the magnetic iron oxide Fe3O4. 60 - Method according to one of claims 37à EMI40.1 59 and characterized because one pulverizes the oxide ma? TiGqe liqulde 34 Fe3O4 with the aid of an inert gas compressed such as- then one EMI40.2 flows this oxide in a liquid such as water, which txï, īt.ise the Rtagnetic oxide and prevents. its oxidation by the wing 61 - Process according to claim CO and character- EMI40.3 ized because the stabilized wr..3nétiue oxide is dried and then pulverized dry, then delivered to the coianerce * 62 - Process coiforrie with one of claims GO or 5. and characterized because it is ground in the wet state, l 'Gxyde; xigi, ltLqu.3 stabilized and then dried 630- Process conforms to one of claims' 59 gas and characterized because the oxide is reduced!; A31Htique FeO4 of' i: 1.: ;; , nii? re to obtain the suboxide FeO which can be stabilized by cooling. sow quickly in water. 64 - Method according to one of claims 37 to EMI40.4 63 and characterized because the iron nmtal or the suboxide is oxidized by blowing an oxidizing gas by spraying the molten product with air cooling by peroxidation of the solid metal spray. EMI40.5 ized or ground in the presence of oxygen or other similar means. 65 - Process according to one of claims 37 to EMI40.6 64 and characterized because q = .1 the iron metal is refined -obtained by reduction of the oxide of the ore "so as to remove certain impurities (carbon, manganese, etc.) from the link to obtain a .ra.éta.1 pure, this refining being carried out for example, by blowing air or by adding r6acvif s., such as iron oxides (scales,) silicon, aluminum., etc. Finally, the refined metal is collected, for example by casting in ingots, by spraying, by injection of EMI40.7 inert gases under pressure, by direct precipitation in water or any other means known in sok. EMI40.8 660- Process according to one of claims 37 <Desc / Clms Page number 41> at 65 and characterized because the metal is oxidized after refining, which makes it possible to obtain very pure oxides. 67 '- Process in accordance with one. of claims 37 to 66 and characterized because the burnt gases originating from the various operations (sintering, melting, refining, etc.) are collected and all or part of them regenerated by reduction of these burnt gases, m so as to obtain reducing gases and these regenerated reducing gases are applied to the reduction of iron oxide, 68 - Process according to one of claims 37 to 67 and characterized because one obtains from liquid air on the one hand oxygen for the manufacture of the reducing gas, on the other hand, nitrogen, for the formation neutral atmosphere, for example, in order to collect and protect the molten metal from any oxidation. 69 - Process according to one of claims 37 to 68 and characterized because the flue gas from the various operations (sintering, melting, refining, etc.) is collected and applied to operations of reheating, in one or other of the phases of the process (calcination, vaporization of water, etc.)