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    • 专利摘要:
    24 ABSTRACT A method for recovery of evaporable substanoes compríses meltíng (210) of amaterial cornprísíng evaporable rnetals and/ or evaporable metal compoundsínto a molten slag. The rnolten slag is agítated (212) by a subrnerged jet ofhot gas. The hot gas ís controlled (214) to have an enthalpy of at least 200MJ/ krnol, and preferably at least 300 MJ /krnol At least a part of theevaporable metals and/ or evaporable metal compounds are fumed off (216)from the molten slag. An arrangement for the method is based on a furnace With a plasma torch submerged into molten slag in the furnace. (Fig. 2)
    公开号:SE1251067A1
    申请号:SE1251067
    申请日:2012-09-21
    公开日:2014-03-22
    发明作者:Matej Imris；Sven Santén；Bror Magnus Heegard
    申请人:Valeas Recycling Ab；
    IPC主号:
    专利说明:

    lO PLASMA INDUCED FUMIN G TECHNICAL FIELD The present invention relates in general to arrangements and methods forrecovery of evaporable substances, and in particular to arrangements and methods for plasma induced fuming.
    BACKGROUND During many years, recovery of metal values from metallurgical Wastematerials has been developed. Such recovery is beneficial for many reasons.One is that Waste materials, e.g. EAF (Electric Arc Furnace) dust, and slag ofdifferent kinds often contains such high amounts of heavy metals that theyare unsuitable for immediate deposition. Rest products comprising elementslike Sn, Zn and Pb are preferably not returned in to the nature Without anyprotective treatment. Furthermore, the value of these elements is also notnegligible. By recovering these elements, the environment is saved at the same time as useful metals are obtained.
    It is since long known to use different types of fuming processes to recoverevaporable substances both from primary sources, such as roasted Zn oresand from secondary sources, such as EAF dust, leaching residues andsecondary slags. A typical simple slag fuming process produces a moltenmetallurgical slag. The slag is typically exposed to reducing agents and isheated to relative high temperatures. Vapours of volatile metals, such as e. g.zinc and lead, are transferred into the gas phase above the slag and thevapours are removed for further treatment to obtain the metalliccomponents. One typical such example is found e.g. in the published patentapplication GB 2 181 746 A or the US patent US 5,942,023.
    In the US patent US 4,57l,260, a method for recovering metal values from materials containing tin and/ or zinc is disclosed. The method is basically a Kaldo process where a surface of a rotating slag bath is exposed for oxygenand fuel. Flux and coke are added to achieve a suitable viscosity and appropriate agítation.
    A disadvantage With most early slag fuming arrangements is that theefficiency in removing the volatile metals was not always the best. Relatively high contents of hazardous substances were remaining in the final slag.
    Today literature and operational practice often mention and apply hightemperature treatment of volatile containing materials. The highternperatures are necessary to ensure high fuming rates and high yields. Asan example Zn fuming from fayalite slags can be used. Here the slag issuperheated above its normal melting point of 1100 °C. This superheating ofthe slag results in excellent fuming, however, it results also in high refractory wear and higher energy consumption of the process.
    Water cooled vessels are typically used to overcome the short lifecycle of therefractory, however, at a high cost of heat loss that comes with it. Thereforethe smelters typically have to compromise between high wear, low fuming rates and high heat losses.
    The above mentioned issues with high refractory wear and high energy costwere addressed in published international patent applicationWO 2005/ 031014. There, high Zn fuming rates without any need tosuperheat the slag are described. According to that approach, the meltingpoint of the slag is increased to 1300 °C by adding suitable fluxes. By doingso, there is limited or no need for the slag to be superheated to obtain highfuming rates. The reason is that the desired temperature for high fumingrates is typically around 1300 °C, and since the melting point of the slag isaround 1300 °C, superheatíng is typically not necessary. Such a slag is saidto build a protective freeze lining on top of the refractory on water cooledwalls and this approach therefore minimizing the wear of the lining. The fuming process according to WO 2005/031014 however comes at the cost of lO BO energy needed to heat all of the slag volume in the reactor up to 1300 °C,and at the cost for fluxes that need to be added to increase the melting point of the slag.
    Another approach is disclosed in the published US patent US 4252563.There it is described a continuous of slag fuming process where the slag isfumed in two consecutive slag treatment zones. In the first zone, the slag issubjected to heat treatment for fuming off volatile, preferably sulphidebound, constítuents. In the subsequent second furnace zone, the slag issubjected to reduction treatment, where oxides are reduced to theirelementary form and fumed off. If the slag is subjected to further separationafter the fuming process, it can be subjected to a further Sfd zone for copperrecovery. However this Sfd zone has again to be heated since the temperatureof the slag after zone 2 drops considerably. The slag temperature is adjustedin the first zone so that the reduction and fuming treatment in the secondzone can be carried out essentially without any further heating of the slag.Preheated air and pulverized coal is used for heating the slag, giving theprocess a need for a robust off-gas system. Utilization of coal as fuel givesthe process límitations for energy input and oxygen potential. At relativelystrong reduction conditions, huge amounts of coal have to be supplied tocover the energy demand for heating and reduction. This gives rise to very high amounts of exhausted greenhouse gases.
    The use of submerged plasma torches generating a gas agitating the slagbath and for feeding of reducing agents is known, e.g. as disclosed in thepublished US patent application US 2010/0050814.
    Despite the development in this technical area, there are still remainingproblems. In particular, by solving the earlier problems With lining Wear andfuming rate, the costs for fluxes, heating and cooling is increased, as Well as, in some cases, the high emissions of carbon oxides. lO SUMMARY A general object of the present invention is to improve recovery of evaporablesubstances. A particular object of the present invention is to reduce the useof slag formers, to reduce the requested amount of supplied energy and still ensure a loW Wear on the refractories in the reactor.
    The above objects are achieved by arrangements and methods according tothe enclosed independent claims. Preferred embodiments are specified by thedependent claims. In general, in a first aspect, a method for recovery ofevaporable substances comprises melting of a material comprisingevaporable metals and/ or evaporable metal compounds into a molten slag.The molten slag is agitated by a submerged jet of hot gas. The hot gas iscontrolled to have an enthalpy of at least 200 MJ/ kmol, and preferably atleast 300 MJ /kmol At least a part of the evaporable metals and/or evaporable metal compounds are fumed off from the molten slag.
    In a second aspect, an arrangement for recovery of evaporable substances,comprises a furnace, a heating arrangement, a plasma torch system and afume handling system. The heating arrangement is arranged for melting amaterial comprising evaporable metals and/ or evaporable metal compoundsin the furnace into a molten slag. The plasma torch system is submerged viaa tuyere into the molten slag and is arranged for agitating the molten slag bya submerged jet of hot gas. The plasma torch system is adapted to beoperated to give the hot gas an enthalpy of at least 200 MJ/ kmol, andpreferably at least 300 MJ/ kmol. The fume handling system is configured tocollect the evaporable metals and/ or evaporable metal compounds that are fumed off from the molten slag.
    One advantage with the present invention is that the required amount ofenergy for the plasma induced fuming is reduced, While keeping theextraction efficiency on a comparable level. Another advantage is that the need of slag formers is reduced and thereby also the final amount of slag lO that has to be disposed. Furthermore valuable compounds can be collectedin a matte and/or metal phase. Other advantages are described inconnection With the different embodiments in the detailed description section.
    BRIEF DESCRIPTION OF THE DRAWINGS The invention, together with further objects and advantages thereof, maybest be understood by making reference to the following description takentogether With the accompanying drawings, in Which: FIG. 1 is a schematic illustration of an arrangement for recovery ofevaporable substances; and FIG. 2 is a flow diagram of steps of an embodiment of a method for recovery of evaporable substances.
    DETAILED DESCRIPTION Throughout the drawíngs, the same reference numbers are used for similar or corresponding elements.
    The invention stated in this patent describes recovery of volatile non-ferrous metals from secondary and primary materials.
    The use of submerged plasma torches generating a gas agitating the slagbath and for feeding of reducing agents is known since long. The introducedgas gives a thorough agitation of the melt at the same time as heat is addedto the melt. Furthermore, additional substances can be added in the plasma gas, e.g. reducing agents.
    An advantage With the use of a submerged plasma torch is that the amountof heat added to the melt is independent of the amount of added reducingagents. In systems, Where different carbon compounds are utilized for creating the heat, the oXygen potential and the heat generation Will be 6 intimately connected. By use of the plasma torch, virtually any oxygen potential can be combined With any amount of heat generation.
    In prior art slag fuming methods, development efforts have been driven byevaluating equilibrium or quasi~equilibrium homogeneous conditions in theslag bath. When the average temperature of the slag is high enough, the slagfuming rate becomes high. Volatile elements leave the slag bath by the upper slag bath surface and enter into the gas phase above the slag.
    One idea of the present approach is to instead to utilize dynamic effects andinhomogeneous conditions. If a submerged plasma torch is used, theagitation and the supply of gas into the slag bath cause conditions that arefar from homogeneous or equilibrium-like. Such local conditions could be utilized to further improve the fuming properties.
    It has also surprisingly been found that by using a submerged plasma torchintroducing gas With an extremely high enthalpy, high slag fuming rates areachievable far below the earlier indicated requested average slagtemperatures. In other Words, even if the average slag temperature is farbelow the prior art high fuming rate temperatures, volatile elements areefficiently extracted from the slag. This indicates that a completely new fuming mechanism must have been activated.
    The gas bubbles With the extreme high enthalpy have surprisingly been seento eXtract evaporable substances at very high rate. The life time of a bubbleis very short, nevertheless, large amounts of volatile elements anyway havemanaged to leave the slag to enter into the bubbles. It Was found that theboosting effect of the plasma gas became noticeable When the gas enteringthe slag has an enthalpy of minimum 200 MJ / kmol. Preferably, the gasentering the slag has an enthalpy of minimum 300 MJ/ kmol. Enthalpies upto 369 MJ /kmol have been successfully tested. The temperature of theinterface between the liquid slag and the gas bubble then becomes much higher than the average slag temperature is. Because of this hot interface, l0 7 the mass transfer of the elements that are to be fumed is accelerated, givinghigh fuming rates of metallic and/ or oxidic vapours. The high mass transferof metallic and/ or oxidic vapour may furthermore be enhanced bycontrollíng the gas jet from the plasma system. The gas jet can thereby beadapted to give the most suitable oxygen potential and zero partial pressure of the elements/ compounds Which are to be fumed.
    Since the average slag temperature no longer is the crucial criticalparameter, the average slag temperature can be selected according to otherpreferences. For instance, the average slag temperature can be adapted tocreate a protectíve freeze lining on the Water cooled walls. The average slagtemperature can thereby be controlled in dependence of the slag compositíonto assume a value appropriate for freeze lining. The present' approach thusopens an alternative process for high fuming rates at average slagtemperatures, even as low as 1100 °C. If the slag compositíon is appropriate,a protectíve freeze lining Will be created on the Water cooled walls.Furthermore, no refractory is needed in such a setting, since such a slag isfreezing promptly on the surface of the steel Walls. The slag is heated to thetemperatures needed to create freeze lining by controllíng the gas flow of the submerged plasma jet having the mentioned high enthalpies.
    As mentioned further above, the plasma jet is also possible to utilíze forensuring strongly agitated slag and for providing ability to Work at any oxygen potential at a same energy input.
    Fig. 1 illustrates schematically an embodiment of an arrangement l forrecovery of evaporable substances. The arrangement 1 comprises a furnace10. Material 22 comprising evaporable metals and / or evaporable metalcompounds is introduced through an inlet 21 into the furnace 10. A heatingarrangement 20 is arranged for melting the material 22 introduced into thefurnace 10 into a molten slag 24. In the present embodiment, the heatingarrangement 20 comprises a plasma torch system 28 and a tuyere 29. The plasma torch 28 is thus arranged for supplying the energy necessary for melting the material 22, at least When it reaches the surface 25 of the slagbath. Preferably, the plasma torch system 28 is designed to be capable ofproducing hot gas of a temperature of above 3000 °C, and most preferablyabove 4000 °C.
    In alternative embodiments, the heating arrangement 20 may comprise othermeans turning the material 22 introduced into the furnace 10 into a moltenslag 24. One example could be a pneumatic raw material feeding into theslag bath via a tuyere 29. Such heaters are then preferably combined Withthe effect of the plasma torch system 28 for achievíng the melting. Furtheralternatively, the material 22 could be molten before being entered into the furnace 10.
    In the embodiment of Fig. 1, the plasma torch system 28 is via a tuyere 29submerged into the molten slag 24. The plasma torch system 28 is therebyalso arranged for agitating the molten slag 24 by means of a submerged jet26 of hot gas. The hot gas 27 creates bubbles in the molten slag 24, causinga violent stirring of the molten slag 24 on their way up to the surface 25 ofthe slag bath. The plasma torch is adapted to be operable to give the hot gas27 an enthalpy of at least 200 MJ /kmol, and preferably of at least 300MJ/kmol. By this high enthalpy evaporable metals and/ or evaporable metalcompounds are fumed off from the molten slag 24 into the bubbles of hot gas27. A smaller amount of evaporable metals and/ or evaporable metalcompounds are also fumed off directly into a gas volume 12 above themolten slag surface 25. The bubbles of hot gas 27 are rapidly transported tothe molten slag surface 25, and there releasing the content in the hot gas 27 into the gas volume 12.
    The present embodiment further comprises a fume handling system 30. Thefume handling system 30 is configured to collect the evaporable metalsand/ or evaporable metal compounds in the gas volume 12 that has beenfuming off from the molten slag 24, either directly via the molten slag surface or via the bubbles of hot gas 27. The metals and/or metal compounds are handled in accordance With prior art methods for valuation of the finalmetals and/or metal compounds 31. The particular Way in Which theevaporable metals and/ or evaporable metal compounds are handled is notcrucial for the operation of the slag fuming arrangement as such and is therefore not further discussed.
    The present embodiment also comprises a slag outlet 40 allowing moltenslag depleted in evaporable metals and/ or evaporable metal compounds tobe tapped off. The present embodiment of the arrangement l has a furnacethat is arranged for performing a continuous process. In other Words, thepresent embodiment is intended for a continuous operation, Where thematerial 22 continuously or intermittently is introduced into the furnace 10.The material 22 rnelts When coming into contact With the hot gas in the gasvolume 12 or When being contacted With the molten slag surface 25. Duringthe agitation by the bubbles generated by the plasma torch gas jet 26, themolten slag becomes depleted in evaporable metals and/ or evaporable metalcompounds, that instead evaporates into the bubbles. The molten slagdepleted in evaporable metals and/ or evaporable metal compounds maycontinuously or intermittently be removed from the furnace 10 by the slag outlet 40.
    In an alternative embodiment, the furnace 10 can also be operated in abatch manner, Where the material 22 first is entered into the furnace 10,then treated into a molten slag depleted in evaporable metals and/or evaporable metal compounds and finally removed from the furnace 10.
    In one preferred embodiment, the heating arrangement 20 comprises acontroller 23 arranged for Operating the heater arrangement 20 for keepingthe molten slag 24 at a predetermíned average temperature. Thepredetermíned average temperature is preferably selected in dependence ofthe slag composition. Since most slags are composed to have a meltingtemperature of around 1100 °C, the predetermíned average temperature should not exceed such value by too much. For systems having standard slag compositions, the controller 23 is preferably arranged for operating theheater arrangement 20 for keeping the molten slag 24 at an averagetemperature below 1200°C, and preferably below 1150°C. For other systems,having other slag melting temperatures, the controller 23 is preferablyarranged for operating the heater arrangement 20 for keeping the moltenslag 24 at an average temperature of less than 100°C above a meltingtemperature of the slag, and preferably less than 50°C above a melting temperature of the slag.
    In a preferred embodiment, the furnace 10 is equipped with a cooled wall 15,in order to create a freeze lining and be able to reduce the Wear of thefurnace wall. The predetermined average temperature of the slag is then alsopreferably selected in dependence of the performance of the cooled wall 15.The controller 23 is then arranged for balancing the predetermined averagetemperature of the slag to the reactor Wall cooling to create a protective frozen slag layer 16 on the reactor wall 15.
    As briefly mentioned above, one of the advantages in using a plasma torchfor supplying the energy into a slag bath is that one easily can obtain controlof an amount of introduced reduction agents without putting constraints onthe total supplied power. ln one preferred embodiment, the arrangement 1further comprises introduction means 17 arranged for adding carbon orhydrocarbon into the tuyeres 29 submerged into the slag bath transportingthe hot gas from the plasma jet 26. This enables adjusting of an oxygenpotential of the hot gas 27. The oxygen potential is possible to be adjustedwithin the range of 104 to 1044 atm. If the introduced reducing agentsreduce the molten slag, such reactions are typically endothermic and furtherenergy has typically to be provided to keep a constant temperature. Whenusing a plasma torch, the controller 23 is easily arranged for controlling the plasma torch to supply the necessary energy for reducing the molten slag. ln combination with the recovery of the volatile metals, also other metals can be extracted from the material 22 introduced into the furnace 10. In one 11 embodiment, the introduction means 17 is arranged for adjusting an oxygenpotential in the slag to be suitable for selectively reducing metal compoundsin the slag into a molten metal phase. Examples of typical such metals thatare possible to reduce from the slag are Cu, Ni, Ag, Au, Pt and Pd. Themolten metal phase 44 is collected in the bottom of the furnace 10. Themolten metal phase is removed, continuously or intermittently, via an outlet42. The furnace 10 is for this purpose provided With a refractory 45 at the bottom.
    In another embodiment, Where the material 22 introduced into the furnace10 and thereby also the slag comprises sulphur or sulphur compounds, alsoa matte phase can be obtained. The introduction means 17 is then arrangedfor adjusting an oxygen potential in the slag for preventing the sulphur frombeing oxidízed. Metals may then be recovered in a molten matte phase.Examples of typical such metals that are possible to recover from the slagare Fe, Cu, Ni, Ag, Au, Pt and Pd. The molten matte phase is collected in thebottom of the furnace 10. The molten matte phase is removed, continuously or intermittently, via an outlet.
    In yet another embodiment, both a metal phase and a matte phase can beobtained, by proper adjustment of the oxygen potential and the sulphurcontent. As a non-limiting example, Au, Pt and Pd can be reduced into ametallic phase, Whereas Cu and Ni form the matte phase. The matte phasetypically appears on top of the metal phase, since it typically has a lowerdensity than the metal phase and since the tWo phases are more or lessunsolvable in each other. The matte phase and the metal phase can be extracted from the furnace by separate outlets or by a common outlet.
    Fig. 2 is a flovv diagram of steps of an embodiment of a method for recoveryof evaporable substances. The method begins in step 200. ln step 210, amaterial comprising evaporable metals and/ or evaporable metal compoundsis molten into a molten slag. The molten slag is in step 212 agitated by a submerged jet of hot gas. Preferably, the energy for melting the material is 12 supplied by the submerged jet of hot gas. In step 214, the hot gas iscontrolled to have an enthalpy of at least 200 MJ/ kmol, and preferably atleast 300 MJ /kmol. Preferably, the hot gas has a temperature upon enteringthe molten slag above 3000°C, and preferably above 4000°C. At least forordinary types of slag compositions, it is preferable to let control the moltenslag to have an average temperature below 1200°C, and preferably belowl150°C. Since the slag melting temperature may díffer With the actual slagcomposition, it is preferable to control the molten slag to an averagetemperature of less than l00°C above a melting temperature of the slag, andpreferably less than 50°C above a melting temperature of the slag. Oneadvantage of holding the molten slag at these temperatures is that a freezelining is easier to maintain. At least a part of the evaporable metals and/ orevaporable metal compounds is fumed off from the molten slag in step 216.Preferably, a majority part of the evaporation takes place into the hot gas.The energy for fuming of the material is preferably supplied by thesubmerged jet of hot gas. The process ends in step 299.
    In Fig. 2, the process is illustrated as a single batch process. Hovvever, in apreferred embodiment, the method is operated as a continuous process. Inother Words, the different steps are preferably performed at least partially simultaneous and in a continuous or intermittent manner.
    Preferably, the method further comprises adjustment of an oXygen potentialof the hot gas by adding carbon or hydrocarbon into the hot gas. The oxygenpotential can be adjusted Within the range of 104 to 10-14 atm. The energyfor reducing the molten slag is supplied by the submerged jet of hot gas.
    Test runs have been performed according to the above presented ideas. Inone particular experiment the slag Was held at a temperature of 1100 °C andhot gas With an enthalpy of 280 MJ/ kmol Was introduced submerged intothe slag. 1000 kg of EAF dust, 100 kg of coke and 100 kg of sand Was utilized in this test run as input material. The ingoing material Was roasted 18 Material EAF dust Coke SandArnount kg: 1000 100 100Compound Wt% WtO/o Wt%S102 4.0 85.7MnO 2.0 P2O5 0.4 CrgOg, 0.3 NíO 1.0 MgO 1.9 CuO 0.4 Cu 0.0 TíOz 0.1 A1203 0.9 9.8FeO 0.0 2.0FegOg 24.7 CaO 4.8 2.5NagO 1.1 KQO 0.8 ZnO 41.1 Zn 0.0 PbO 4.7 Pb 0.0 C 2.2 99.6 S 0.0 0.4 H20 5.1 0.0 KCl 2.9 NaCl 1.5 S03 0.0 O 0.5 SUM 100.0 100.0 100.0 Table 1. Input quantítíes 14 Material Metal Slag Gas Recovered productAmount kg: 6.9 491.6 701.5 495.6Cornpound Wt% wt% Wt% vvt%S102 25.5 MnO 4.0 P2O5 0.7 CrgOg 0.7 N10 0.8 Ni 68.7 MgO 3.9 CuO 0.2 Cu 31.3 TíOQ 0.1 A12O3 3.9 FeO 45.6 FegOe, 0.0 CaO 10.2 NazO 2.3 KQO 0.7 ZnO 1.3 81.6Zn V 46.3 PbO 0.0 9.5Pb 6.2 C 17.4 H20 (Vapour) 3.7 KCl 4.1 5.8NaCl 2.2 3.0O 19.6 S02 0.1 H 0.4 SUM 100 100 100 100 Table 2. Output quantitíes prior to feeding to remove the sulphur from the material. The compositionsof the components are given in Table 1. Note that the plasma gas andreducíng agents are not included in the balance calculations. During theoperation, a total of 701.5 kg of gas was extracted, from Which 495.6 kgrecovered products eventually Was collected. In this particular experiment,the oxygen potential Was held at a level appropriate for reducíng the CuOinto metallic copper, and FegOg, into FeO, while Zn and Pb Were extracted inthe gas phase. Air Was used as the plasma gas and the oxygen potential Wascontrolled by introducing propane into the hot gas. The output of theexperiment is shown in Table 2. As a conclusion, the level of ZnO Was in thepresent test run reduced from 41.1 Wt% in the EAF dust to 1.3 Wt% in thefinal slag, Which corresponds to an extraction degree of 934%. Such levels ofZn extraction has earlier only been achieved at slag temperatures over 1300 °C.
    In another particular experiment the slag Was again held at a temperature of1100 °C and hot gas With an enthalpy of 280 MJ/ kmol Was introducedsubmerged into the slag. 1000 kg of EAF dust, 100 kg of coke and 100 kg ofsand was utilized in this test run as input material. The compositions of thecomponents are given in Table 3. S and S03 are present in the system. Notethat the plasma gas and reducíng agents are not included in the balancecalculatíons. During the operation, a total of 704.3 kg of gas Was extracted,from Which 485.5 kg recovered products, mainly ZnO, was collected. In thisparticular experiment, the oxygen potential was held at a level appropriate toprevent sulphur oxidation, therefore recovering the Cu and Ni, respectively,into copper~nickel matte, and FegOg. into FeO and FeS, While Zn and Pb Wereextracted in the gas phase partially as metal vapours. Air Was used as theplasma gas and the oxygen potential Was controlled by introducing propaneinto the hot gas jet. The output of the experiment is shown in Table 4. As aconclusion, the level of ZnO in the present test run was reduced from 40.3Wt% in the EAF dust to 1.3 Wt% in the final slag, Which corresponds to an extraction degree of 985%. 16 Material dust Coke SandAmount kg: 1000 100 100Cornpound WtO/o Wt% WtO/oSíOz 3.9 85.7MnO 1.9 P2O5 0.3 CrgOs 0.3 NíO 1.0 MgO 1.9 CuO 0.4 Cu 0.0 TíOz 0.1 AIQOs 0.9 9.8FeO 0.0 2.0FegOg 24.2 CaO 4.7 2.5NagO 1.1 KzO 0.3 ZnO 40.3 Zn 0.0 PbO 4.6 Pb 0.0 C 2.2 99.6 S 0.6 0.4 H20 5.0 0.0 KCI 2.8 NaC1 1.5 S03 1.5 O 0.5 SUM 100.0 100.0 100.0 Table 3. Input quantítíes 17 Material Matte Slag Gas Recovered productAmount kg: 17.1 478.6 704.3 485.5Compound WtO/f; Wt% Wt°/c> Wt%S102 26.0 Mn0 4.0 P205 0.7 C1^203 0.7 Ní0 0.8 Nis 42.2 7 MgO 3.9 C110 0.2 CugS 15.3 Tí02 0.1 111203 4.0 F60 44.7 FeS 42.5 Ca0 10.3 Na20 2.3 1420 0.7 Zn0 1.3 81.6ZnS 0.0 Zn 45.2 Pb0 0.0 9.5PbS 0.0 Pb 6.1 C 17.3 H20 (vapour) 3.6 KCI 4.0 5.8NaC1 2.1 3.00 19.8 S02 1.5 S 0.2 H 0.4 SUM 100 100 100 100 Table 4. Output quantítíes lO 18 Minor amounts of platinum group metals and noble metals Were also present in the experiments presented above. It Was found that at least 98% of theAu, Pt and Pd Were recovered into the metal or matte phase. The Ag Wascollected to 50-60% in the metal or matte phase, While 40~50% ended up inthe filter cake.
    The embodiments described above are to be understood as a few illustrativeexamples of the present inventíon. It Will be understood by those skilled inthe art that various modifícations, combinations and changes may be madeto the embodiments without departing from the scope of the presentinventíon. In particular, different part solutions in the different embodimentscan be combined in other configurations, Where technically possible. The scope of the present invention is, however, defined by the appended claims.
    权利要求:
    Claims (27)
    [1] 1. l. A method for recovery of evaporable substances, comprising the stepsof: melting (210) a material comprising at least one of evaporable metalsand evaporable metal compounds into a molten slag; agitating (212) said molten slag by a submerged jet of hot gas; and fuming off (216) at least a part of said at least one of evaporablemetals and evaporable metal compounds from said molten slag,characterized by the further step of controlling (214) said hot gas to have an enthalpy of at least 200MJ/ kmol, preferably at least 300 lVlJ/kmol.
    [2] 2. The method according to claim l, characterized in that said step offuming off (216) at least a part of said at least one of evaporable metals andevaporable metal compounds from said molten slag compríses evaporation ofsaid at least one of evaporable metals and evaporable metal compounds are fumed off into said hot gas.
    [3] 3. The method according to claim 1 or 2, characterized in that saidmolten slag has an average temperature of less than 100°C above a meltingtemperature of said slag, preferably less than 50°C above said melting temperature of said slag.
    [4] 4. The method according to any of the claims 1 to 3, characterized inthat said molten slag has an average temperature below 1200°C, preferably below 1l50°C.
    [5] 5. The method according to any of the claims 1 to 4, characterized inthat said hot gas has a temperature upon entering said molten slag above3000°C, preferably above 4000°C. lO
    [6] 6. The method according to any of the claims 1 to 5, characterized inthat the energy for melting and/ or fuming of said material is supplied by said submerged jet of hot gas.
    [7] 7. The method according to any of the claims 1 to ö, characterized byadjusting an oXygen potential of said hot gas by adding carbon or hydrocarbon into said hot gas.
    [8] 8. The method according to any of the claims 1 to 7, characterized byadjusting an oXygen potential in said slag by adding solid carbon and/ or hydrocarbon into said slag.
    [9] 9. The method according to claim 7 or 8, characterized in that said oXygen potential is adjusted Within the range of 10-4 to 10-14 atm.
    [10] 10. lO. The method according to any of the claims 7 to 9, characterized inthat said step of adjusting an oXygen potential in said slag comprisesadjusting an oXygen potential in said slag for reducing metal compounds insaid slag into a molten metal phase; and by the further step of removing said molten metal phase.
    [11] 11. The method according to any of the claims 7 to 10, characterized inthat said slag comprises sulphur or sulphur compounds; said step of adjusting an oXygen potential in said slag comprisesadjusting an oxygen potential in said slag for preventing sulphur from beingoxidized, collecting metal compounds in said slag into a molten matte phase; and by the further step of removing said molten matte phase.
    [12] 12. The method according to any of the claims 1 to 11, characterized inthat the energy for reducing Said molten slag is supplied by said submerged jet of hot gas. lO 21
    [13] 13. The method according to any of the claims 1 to 12, characterized in that the method is a continuous process.
    [14] 14. An arrangement (1) for recovery of evaporable substances,cornprising: a furnace (10); heating arrangement (20) arranged for melting a material (22)comprising at least one of evaporable metals and evaporable metalcompounds in said furnace into a molten slag (24); a plasma torch system (28) submerged via a tuyere (29) into saidmolten slag (24) and arranged for agitating said molten slag (24) by asubmerged jet (26) of hot gas (27); and a fume handling system (30) configured to collecting said at least oneof evaporable metals and evaporable metal compounds being fuming off fromsaid molten slag (24),characterized in that said plasma torch system (28) is designed to be operated to give saidhot gas (27) an enthalpy of at least 200 MJ/kmol, preferably at least 300MJ/ kmol.
    [15] 15. The arrangement according to claím 14, characterized in that saidfume handling system (30) is arranged to collect said at least one ofevaporable metals and evaporable metal compounds being fuming off from said molten slag into said hot gas (27).
    [16] 16. The arrangement according to claím 14 or 15, characterized in thatsaid controller (20) of said heating arrangement is arranged for keeping saidmolten slag (24) at an average temperature of less than 100°C above amelting temperature of said slag, preferably less than 50°C above a melting temperature of said slag.
    [17] 17. The arrangement according to any of the claims 14 to 16, characterized in that said heating arrangement (20) comprises a controller 22 (23) arranged for Operating said heater arrangement (20) for keeping saidmolten slag (24) at an average temperature below 1200°C, preferably below1 1 50°C
    [18] 18. The arrangement according to any of the claims 14 to 17,characterized in that said controller (23) of said heating arrangement (20)is arranged for balancing a temperature of said slag to the reactor Wall cooling to create a protective frozen slag layer (16) on the reactor Wall (15).
    [19] 19. The arrangement according to any of the claims 14 to 18,characterized in that said plasma torch system (28) is capable of producing hot gas of a temperature of above 3000°C, preferably above 4000°C.
    [20] 20. The arrangement according to any of the claims 14 to 19,characterized in that said controller (23) of said heating arrangement (20)is arranged for Operating said plasma torch system (28) to supply the energy necessary for melting said material (22).
    [21] 21. The arrangement according to any of the claims 14 to 20,characterized by introduction means (17) arranged for adding carbon orhydrocarbon into said hot gas jet for adjusting an oxygen potential of said hot gas.
    [22] 22. The arrangement according to any of the claims 14 to 20,characterized by introduction means arranged for adding carbon and/ or hydrocarbon into said slag for adjusting an oxygen potential of said slag.
    [23] 23. The arrangement according to claim 21 or 22, characterized in thatsaid introduction means (17) is arranged for adjusting an oXygen potential Within the range of 10-4 to 10-14 atm.
    [24] 24. The arrangement according to any of the claims 21 to 23, characterized in that said introduction means (17) is arranged for adjusting 23 an oxygen potential in said molten slag (24) for selectively reducíng metal compounds in said slag.
    [25] 25. The arrangement according to any of the claims 21 to 24,characterized in that said slag comprises sulphur or sulphur compounds; said introduction means (17) is arranged for adjusting an oxygenpotential in said slag to prevent sulphur from being oxidized and forcollecting metal compounds in said slag into a molten matte phase; and by further comprising an outlet for said molten matte phase.
    [26] 26. The arrangement according to any of the claims 12 to 25,characterized in that said controller (23) of said heating arrangement (20)is arranged for Operating said plasma torch system (28) to supply the energy necessary for reducing said molten slag (24).
    [27] 27. The arrangement according to any of the claims 12 to 26,characterized in that said furnace (10) is arranged for performing a continuous process.
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    同族专利:
    公开号 | 公开日
    JP6378683B2|2018-08-22|
    EP2898106B1|2019-02-20|
    KR20150076168A|2015-07-06|
    EP2898106A4|2016-06-15|
    WO2014046593A1|2014-03-27|
    KR102176989B1|2020-11-10|
    US20150232961A1|2015-08-20|
    JP2015535883A|2015-12-17|
    ES2726818T3|2019-10-09|
    SE537235C2|2015-03-10|
    US10006100B2|2018-06-26|
    EP2898106A1|2015-07-29|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    SE1251067A|SE537235C2|2012-09-21|2012-09-21|Process and arrangement for the recovery of vaporizable substances from a slag by means of plasma induced vaporization|SE1251067A| SE537235C2|2012-09-21|2012-09-21|Process and arrangement for the recovery of vaporizable substances from a slag by means of plasma induced vaporization|
    ES13838833T| ES2726818T3|2012-09-21|2013-08-29|Plasma-induced vaporization|
    KR1020157010317A| KR102176989B1|2012-09-21|2013-08-29|Plasma induced fuming|
    PCT/SE2013/051014| WO2014046593A1|2012-09-21|2013-08-29|Plasma induced fuming|
    JP2015533013A| JP6378683B2|2012-09-21|2013-08-29|Plasma induced transpiration|
    EP13838833.5A| EP2898106B1|2012-09-21|2013-08-29|Plasma induced fuming|
    US14/429,561| US10006100B2|2012-09-21|2013-08-29|Plasma induced fuming|
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