US20100181205A1 - Method for treating waste containing precious metals and device for implementing said method - Google Patents

Method for treating waste containing precious metals and device for implementing said method Download PDF

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Publication number
US20100181205A1
US20100181205A1 US12/446,158 US44615807A US2010181205A1 US 20100181205 A1 US20100181205 A1 US 20100181205A1 US 44615807 A US44615807 A US 44615807A US 2010181205 A1 US2010181205 A1 US 2010181205A1
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waste
lead
feed line
electrolysis
outlet
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US12/446,158
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English (en)
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Christian Thpmas
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Terra Nova SAS
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Terra Nova SAS
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Assigned to TERRA NOVA reassignment TERRA NOVA ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: THOMAS, CHRISTIAN
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
    • B03B9/00—General arrangement of separating plant, e.g. flow sheets
    • B03B9/06—General arrangement of separating plant, e.g. flow sheets specially adapted for refuse
    • B03B9/061—General arrangement of separating plant, e.g. flow sheets specially adapted for refuse the refuse being industrial
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B11/00—Obtaining noble metals
    • C22B11/02—Obtaining noble metals by dry processes
    • C22B11/021—Recovery of noble metals from waste materials
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • C22B7/001—Dry processes
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • the present invention relates to a method for treating waste containing precious metals as well as a device for implementing this method.
  • a first object of the invention is a method for treating waste containing precious metals, comprising the following successive steps:
  • residues are recovered, which are treated by:
  • the step of refining the skimmed mixture comprises the following sub-steps:
  • the aforementioned method comprises before, simultaneously or after the step of recovering anodic sludges, the step of:
  • the step of refining the skimmed mixture comprises, after the sub-step of recovering anodic sludges, the following additional sub-steps:
  • each molten lead-based composition comprises 0-50% of tin, preferably 0-20% of tin.
  • the aforementioned method comprises, prior to the step of contacting the waste with a molten lead-based composition, the step of:
  • the copper extraction step comprises the following sub-steps:
  • the aforementioned method comprises, prior to the copper extraction, the following step:
  • the aforementioned method further comprises a preliminary step of milling the waste and/or analyzing milled waste.
  • the precious metals comprise one or more metals selected from gold, silver, platinum, palladium, rhodium, ruthenium, iridium, osmium and mixtures thereof.
  • the waste is selected from catalytic exhaust mufflers and electronic waste such as electronic cards.
  • more than 90% by mass, preferably more than 99% by mass of the precious metals contained in the waste are recovered according to the aforementioned method.
  • the supernatant materials comprise ceramics, glass fibers and/or ferrites.
  • Another object of the invention is an installation for treating waste containing precious metals, comprising:
  • At least one container for covering with lead at least one container for covering with lead
  • a molten lead-based composition feed line connected to the inlet of the lead covering container
  • a pretreated materials feed line connected to the inlet of the lead covering container
  • skimming means associated with the lead covering container
  • a skimmed mixture withdrawal line connected to the outlet of the lead covering container
  • a precious metals withdrawal line connected to the outlet of the means for refining the skimmed mixture.
  • the aforementioned treatment installation further comprises:
  • skimming residues withdrawal line connected to the outlet of the skimming means
  • At least one additional lead covering container fed by skimming residues withdrawal line on the one hand, and by an additional molten lead-based composition feed line on the other hand;
  • an additional skimmed mixture withdrawal line connected to the outlet of the additional lead covering container and feeding the molten lead-based composition feed line.
  • the means for refining the skimmed mixture by electrolysis comprise:
  • the means for refining the skimmed mixture by electrolysis comprise:
  • the aforementioned treatment installation further comprises:
  • a primary materials feed line connected to the inlet of the copper extraction means.
  • the copper extraction means comprise:
  • a depleted electrolyte feed line connected to the inlet of the selective dissolution container
  • the aforementioned treatment installation further comprises:
  • the aforementioned treatment installation further comprises:
  • milling and analyzing means fed by a raw waste feed line and feeding the waste feed line.
  • the aforementioned method is applied in the aforementioned installation.
  • the aforementioned installation is intended for implementing the aforementioned method.
  • the present invention makes it is possible to overcome the drawbacks of the state of the art. It more particularly provides a specific method for treating and recovering waste containing precious metals, which harmoniously combines metallurgical sequences and avoids dilution of the contained metals in a production flow of primary metals.
  • the invention also provides a single installation for separating the constituents from the waste and in particular for recovering precious metals.
  • the invention also has the advantageous features listed below.
  • the method according to the invention is very flexible and it may be adapted to foreseeable changes in the composition of electronic cards.
  • the method according to the invention does not have the drawback of using the customary technique of extracting precious metals by oxidization of lead, the so-called cupellation operation, followed by the operation for reducing lead oxide.
  • precious metals are kept in the metal form throughout the method, and the lead and tin are kept in the metal form right up to step (d) included. This makes it possible to minimize the carrying away of the precious metals by metal oxides.
  • the precious metals may be collected at a single outlet.
  • the invention may be applied with a controlled environmental impact.
  • FIG. 1 schematically illustrates an exemplary installation for treating waste according to the invention.
  • FIG. 2 illustrates exemplary milling and analyzing means which may be used within the framework of the waste treatment installation according to the invention.
  • the dotted arrows designate the gas flows.
  • the arrows with a double line designate solid flows.
  • FIG. 3 illustrates exemplary pyrolysis and postcombustion means which may be used within the framework of the waste treatment installation according to the invention.
  • the dotted arrows designate gas flows.
  • the arrows with a simple black line designate liquid flows.
  • the arrows with a double line designate solid flows.
  • FIG. 4 illustrates exemplary copper extraction means which may be used within the framework of the waste treatment installation according to the invention.
  • the dotted arrows designate gas flows.
  • the arrows with a simple black line designate liquid flows.
  • the arrows with a double line designate solid flows.
  • FIG. 5 illustrates a particular example of a lead covering container which may be used within the framework of the invention.
  • FIG. 6 illustrates exemplary refining means which may be used within the framework of the waste treatment installation according to the invention.
  • the dotted arrows designate the gas flows.
  • the arrows with a simple black line designate liquid flows.
  • the arrows with a double line designate solid flows.
  • an installation for treating waste schematically comprises the following components. Provision is made for a waste feed line 1 at the entry of the treatment installation.
  • This waste feed line 1 may optionally be connected to the outlet of the milling and analysis means 1 ter fed by a raw waste feed line 1 bis .
  • the waste feed line 1 like all the other feed, transfer or withdrawal lines mentioned in the present description may include a single route or several routes (branches) in parallel.
  • the waste feed line 1 feeds pyrolysis means 2 .
  • provision is made for means for feeding primary materials 6 which feed copper extraction means 37 .
  • a pre-treated materials feed line 14 which feeds a lead covering container 15 .
  • This embodiment is particularly well adapted to treating used electronic cards.
  • the pyrolysis means 2 are absent, and the waste feed line 1 directly feeds the copper extraction means 37 (in this case it is considered that the waste feed line 1 coincides with the primary materials feed line 6 ).
  • the copper extraction means 37 are absent, and the primary materials feed line 6 directly feeds the lead covering container 15 (in this case it is considered that the primary materials feed line 6 coincides with the pre-treated materials feed line 14 ).
  • both the pyrolysis means 2 and the copper extraction means 37 are absent, and the waste feed line 1 directly feeds the lead covering container 15 (in this case it is considered that the waste feed line 1 and the pre-treated materials feed line 14 coincide).
  • This alternative is particularly adapted to the treatment of used catalytic exhaust mufflers, since the latter practically contain no copper.
  • the outlet of the pyrolysis means 2 may be connected to a gas exhaust line 4 which may feed postcombustion means 5 .
  • the copper extraction means 37 may include a selective dissolution container 7 fed at the inlet by the pre-treated materials feed line 6 and fed by a depleted electrolyte feed line 11 on the other hand.
  • the pre-treated materials feed line 14 is then connected to the outlet of the selective dissolution container 7 , while a rich electrolyte transfer line 8 feeds electrolysis means 9 .
  • Means for stripping the cathodes 13 are provided in association with electrolysis means 9 , and a depleted electrolyte recycling line 10 is provided at the outlet of the electrolysis means 9 .
  • This depleted electrolyte recycling line 10 may feed the depleted electrolyte feed line 11 and/or a depleted electrolyte treating line 12 .
  • the lead covering container 15 which is fed by the pre-treated materials feed line 14 , is also fed by a molten lead-based composition feed line 24 .
  • Skimming means 16 are associated with the lead covering container 15 .
  • a skimmed mixture withdrawal line 21 which feeds means for refining the skimmed mixture 36 .
  • a precious metals withdrawal line 38 is provided at the outlet of the means for refining the skimmed mixture 36 .
  • This additional lead covering container 18 is then also fed by an additional molten lead-based composition feed line 31 .
  • Additional skimming means 19 are provided in association with the additional lead covering container 18 and an additional skimmed mixture withdrawal line 22 is provided at the outlet of the additional lead covering container 18 .
  • This additional skimmed mixture withdrawal line 22 may, just like the skimmed mixture withdrawal line 21 , feed the means for refining the skimmed mixture 36 .
  • the additional skimmed mixture withdrawal line 22 feeds the molten lead-based composition feed line 24 .
  • a complementary source of molten lead-based composition 23 may optionally be provided in order to complete this feed.
  • An additional skimming residues withdrawal line 20 may be provided at the outlet of the additional skimming means 19 .
  • the means for refining the skimmed mixture 36 more specifically provide means for casting anodes 25 , a system for transferring anodes 26 , Betts electrolysis means 27 .
  • the means for recovering lead-tin 29 and means for recovering anodic sludges 28 are provided at the Betts electrolysis means 27 .
  • the means for recovering lead-tin 29 feed (optionally together with a fresh lead feed line 30 which may be provided as an option) the additional molten lead-based composition feed line 31 .
  • the means for recovering anodic sludges 28 feed melting means 33 , which are further provided with an oxygen feed 32 .
  • Final skimming means 34 are provided in association with the melting means 32 .
  • the precious metals withdrawal line 38 is connected to the outlet of the melting means 32 , which also include a residues discharging line 35 .
  • the installation comprises means for receiving waste 101 , which may notably comprise an unloading hall, and which are for example suitable for receiving trucks.
  • Weighing means 102 are provided at these waste receiving means 101 , as well as storage means 103 .
  • dosing means 104 adapted for dumping waste on a main conveyor 105 (belt or the like).
  • the main conveyor 105 distributively feeds a first secondary conveyor 106 , a second secondary conveyor 107 and a third secondary conveyor 108 .
  • the first secondary conveyor 106 feeds a coarse mill 109 .
  • a fine mill 111 is also provided, fed by the second secondary conveyor 107 on the one hand and by a transfer line 110 on the other hand stemming from the outlet of the coarse mill 109 .
  • the mills 109 , 111 may each have a typical capacity of 5-10 t/h.
  • a collector conveyor 112 is provided at the outlet of the fine mill 111 and joins the third secondary conveyor 108 . On the path of the third secondary conveyor 108 , provision is also made for sampling means 113 (for example a ladle), with which analysis means 114 may be fed.
  • the third secondary conveyor 108 distributively feeds a first tertiary conveyor 115 and a second tertiary conveyor 117 .
  • the first tertiary conveyor 115 feeds a silo for storing waste 116 .
  • As for the second tertiary conveyor 117 it feeds a container 118 , at the outlet of which a return conveyor 119 feeds the storage means 103 .
  • An air decontamination system 120 is set up at the coarse mill 109 and the fine mill 111 and feeds a sleeve filter 121 , which may have a typical capacity of 5,000 Nm 3 /h.
  • the sleeve filter 121 is connected to a chimney 123 as well as to a fines recovery line 122 , which feeds the silo for storing waste 116 . It is obvious that one skilled in the art will be able to adapt the thereby described means to the needs of the installation, for example by varying the number or the type of mills or the capacity of the different mills used.
  • the waste feed line 201 is provided at the outlet of the aforementioned silo for storing waste 116 and feeds via hoppers three pyrolysis ovens 202 a , 202 b , 202 c arranged in parallel.
  • the pyrolysis ovens 202 a , 202 b , 202 c may be tubular screw ovens, electrically heated from the outside. As an example, ovens with a length of 5 m and a diameter of 40 cm, with a power of 100 kW, with a variable screw velocity, may be used. The number of ovens may be varied depending on the needs of each installation.
  • a calcinated waste recovery line 203 is provided at the outlet of the pyrolysis ovens 202 a , 202 b , 202 c and feeds two silos for storing calcinated waste 204 a , 204 b .
  • the number of these storage silos may be varied depending on the needs of each installation.
  • the calcinated waste recovery line 203 may be a jacketed conveyor provided with water cooling means.
  • a respective primary materials feed conduit 205 a , 205 b is provided (both of these conduits forming together the primary materials feed line 6 ).
  • each pyrolysis oven 202 a , 202 b , 202 c provision is made for a respective gas exhaust conduit 206 a , 206 b , 206 c (the whole of these conduits corresponding to the aforementioned gas exhaust line 4 ).
  • Each gas exhaust gas conduit 206 a , 206 b , 206 c feeds a respective post-combustion chamber 207 a , 207 b , 207 c .
  • a typical example of the volume of the post-combustion chamber 207 a , 207 b , 207 c is 15 m 3 .
  • Each post-combustion chamber 207 a , 207 b , 207 c is further fed by a respective air intake conduit 208 a , 208 b , 208 c.
  • a burnt gases collecting conduit 209 connects the outlet of the post-combustion chambers 207 a , 207 b , 207 c to the inlet of a vertical cooling chamber 210 .
  • a water coolant feed line 211 is also provided at the inlet of the cooling chamber 210 .
  • spraying ramps located in the high portion of the chamber may be provided.
  • a pre-cooled gases recovery conduit 212 is provided at the outlet of the cooling chamber 210 , and feeds a sleeve filter 214 .
  • An air intake conduit 213 is connected to the pre-cooled gases recovery conduit 212 .
  • the sleeve filter 214 may for example have a capacity of 4,000 Nm 3 /h.
  • a fines withdrawal conduit 215 on the one hand and a stripped gases withdrawal conduit 216 are connected to the outlet of the sleeve filter 214 .
  • the stripped gases withdrawal conduit 216 feeds a chimney 217 .
  • Each primary materials feed conduit 205 a , 205 b feeds a respective selective dissolution container 301 a , 301 b , which may for example be a closed 20 m 3 reactor in epoxy resin/fiber glass with a large thickness, provided with a lid and a stirrer with variable speed. It is possible to provide such a single container or on the contrary a larger number of them depending on the production needs.
  • Each selective dissolution container 301 a , 301 b is also fed by a depleted electrolyte feed conduit 303 .
  • An oxygen supply 304 is moreover provided at the bottom of each selective dissolution container 301 a , 301 b.
  • a respective selective post-dissolution emptying line 305 a , 305 b is provided at the outlet of each selective dissolution container 301 a , 301 b which feeds a respective press filter 306 a , 306 b .
  • a system for collecting solids 307 is placed at the outlet of the press filters 306 a , 306 b and feeds a drying oven 308 , at the outlet of which is found the pre-treated material conduit 309 (corresponding to reference 14 in FIG. 1 ).
  • the drying oven 308 may be a screw oven similar to those used for pyrolysis.
  • each press filter 306 a , 306 b is provided at the outlet with a respective filtered liquid withdrawal conduit 310 a , 310 b which feeds a single vat 302 .
  • the latter in turn feeds via a transfer line 311 , a tank for storing rich electrolyte 312 which may for example have a capacity of 60 m 3 .
  • the electrodeposition unit 314 comprises a certain number of electrolysis tanks 315 a , 315 b , 315 c , 315 d , 315 e , the number of tanks (five in this example) being adaptable to the production needs.
  • Each electrolysis tank 315 a , 315 b , 315 c , 315 d , 315 e comprises a certain number of electrolysis cells depending on the production needs, for example eight in the present example.
  • each electrolysis cell may have a useful volume of 4 m 3 and contain 31 stainless steel cathodes and 30 lead/calcium anodes with a useful surface area of 1 m 2 per face.
  • the electrolysis tanks 315 a , 315 b , 315 c , 315 d , 315 e are fed in parallel by a rich electrolyte transfer conduit 313 connected to the outlet of the tank for storing rich electrolyte 312 .
  • the electrodeposition unit 314 is completed by a system for stripping the cathodes 316 .
  • a depleted electrolyte recycling line 317 is provided, which feeds a first tank for storing depleted electrolyte 318 (for example with a capacity of 60 m 3 ) and a second tank for storing depleted electrolyte 319 (for example with a capacity of 25 m 3 ).
  • the first tank for storing depleted electrolyte 318 is the source for feeding the depleted electrolyte feed conduit 303 .
  • the second tank for storing depleted electrolyte 319 feeds a first stripping reactor 320 (for example with a capacity of 15 m 3 .).
  • This first stripping reactor 320 is also fed by a lime feed line 321 .
  • a first pulp withdrawal line 323 is connected, which feeds an additional press filter 324 .
  • the fines withdrawal conduit 215 described in connection with FIG. 3 feeds a second stripping reactor 325 (for example with a capacity of 5 m 3 ) provided with a water and lime supply (not shown).
  • a second pulp withdrawal line 326 At the outlet of the latter is found a second pulp withdrawal line 326 , which also feeds the additional press filter 324 .
  • a washed fines withdrawal line 327 , a lime sulfate withdrawal line 328 and an acid juice withdrawal line 329 are connected at the outlet of the additional press filter 324 .
  • the washed fines withdrawal line 327 may feed one of the selective dissolution containers 301 a , 301 b or both.
  • the acid juice withdrawal line 329 may feed a tank body, not shown, with additional devices downstream for treating halides.
  • a gas decontamination system 330 passes through the whole of the storage tanks 312 , 318 , 319 of the selective dissolution containers 301 a , 301 b and of the stripping reactors 320 , 325 and feeds a washing tower 331 .
  • the storage tanks 312 , 318 , 319 , the stripping reactors 320 , 325 and the washing tower 331 may be in epoxy resin/fiber glass with a standard thickness.
  • the washing tower 331 comprises at the outlet an additional acid juices withdrawal line 332 , which may in return feed the tank for storing depleted electrolyte 318 .
  • the washing tower 331 may have a capacity of 5 m 3 , be provided with standard lining and operate with water.
  • each container then comprises a kettle 401 (with a capacity of 50 tons for example) surrounded by a heating chamber 402 provided with burners 403 .
  • a stirrer 404 (for example a stirrer with a vertical axis propeller) is immersed into the kettle 401 .
  • the kettle 401 is fed by a feeder 407 , which, depending on the case, is connected to the inlet of the pre-treated materials feed line 14 or to the skimming residues withdrawal line 17 .
  • a skimming machine 405 On the side of the kettle 401 , a skimming machine 405 is provided, consisting in a scraper with a stainless steel jointed arm attached to a tilted plane.
  • An enclosing cover 406 allows the surface of the contents of the kettle to be isolated and is adapted so as to provide inertization with nitrogen.
  • Suction means 408 are provided above the kettle 401 and are connected to a sleeve filter not shown.
  • Means for discharging combustion gases 409 adapted to collecting gases emitted by the burners are connected to the heating chamber 402 .
  • the stirrer 404 may advantageously be disassembled in order to allow transfer of the contents of the kettle 401 .
  • anodes 25 Downstream from the lead covering containers 15 , 18 , means are found for casting anodes 25 , which notably comprise a kettle of the type described in FIG. 5 , but without necessarily the skimming and stirring devices. This kettle may comprise an enclosing cover and suction.
  • This portion of the installation comprises a Betts electrolysis unit 501 , which contains a plurality of rows 502 a , 502 b of Betts electrolysis cells (two in this example).
  • Each row 502 a , 502 b may for example comprise five cells, each cell including 30 anodes and 31 cathodes with a useful surface area of 1 m 2 per face, for a useful cell volume of 4 m 3 .
  • the rows 502 a , 502 b are fed in parallel with electrolyte from a Betts reactor 503 .
  • a return pumping system may be provided for facilitating circulation of the electrolyte.
  • the Betts reactor 503 is fed by a fluorosilicic acid feed line 504 on the one hand and by a litharge feed line 505 on the other hand.
  • a used Betts electrolyte collecting line 506 provides a return to the second tank for storing depleted electrolyte 319 of FIG. 4 .
  • An electrolysis decontamination system 507 provides collection of the gases at the Betts electrolysis 501 and at the Betts reactor 503 , and their transfer towards a washing tower 508 , with a typical volume of 5 m 3 .
  • a washing juice collecting line 509 provides a return towards the second tank for storing depleted electrolyte 319 of FIG. 4 .
  • the Betts electrolysis unit 501 is moreover provided with means for stripping cathodes 510 .
  • the means for stripping cathodes 510 provide a cathode feed line 511 which itself feeds a kettle 512 providing melting of the cathodes.
  • the kettle 512 is of the type described in FIG. 5 , but without necessarily skimming and stirring devices.
  • This kettle 512 may comprise an enclosing cover and suction. It feeds via a lead-tin feed line 513 , possibly together with a fresh lead feed line 30 , the additional molten lead-based composition feed line 31 (see FIG. 1 ).
  • the whole of the references 510 - 513 correspond to means for recovering lead-tin 29 .
  • the Betts electrolysis unit 501 is moreover provided with means for scraping anode stubs 514 which feed an anodic sludges collecting line 516 (the whole forming an example of anodic sludge recovery means 28 ).
  • This anodic sludges collecting line 516 feeds a unit for treating anodic sludges 517 which may comprise washing means, weighing means and/or means for storing in a safe.
  • a washed sludges transfer line 518 connects the unit for treating anodic sludges 517 to an oxidation oven (with a power of 800 kW, 1 ton capacity, for example), which also receives at the entry an air or oxygen intake line 519 .
  • an ingot collecting line 521 may ensure return to the safe storing means of the anodic sludge treatment unit 516 .
  • the litharge feed line 505 is also connected to the outlet of the oxidation oven 520 .
  • a fumes collecting line 522 is also provided at the oxidation oven 520 , it may be connected towards the same filtration system as the one provided at the lead covering containers.
  • Production capacity is of the order of 25,000 tons per year or of the order of 72 tons of waste per day. In the case when the waste is catalytic mufflers, it is possible to do without the pyrolysis and copper extraction steps.
  • the electronic cards are received at the means for receiving waste 101 .
  • the electronic cards arrive at the entry of the installation by batches (containers, big bags, barrels), which are weighed at the weighing means 102 , labelled, recorded and stored at the storage means 103 .
  • the cards may arrive in three main forms:
  • the cards are directed according to their nature: either successively towards the coarse mill 109 and then the fine mill 111 (case 1 above); or directly to the fine mill 111 (case 2 above); or directly to the silo for storing waste 116 (case 3 above).
  • the coarse mill 109 performs milling or grinding of the waste reducing them to a size of less than 25 mm
  • the fine mill 111 performs milling or grinding of the waste reducing them to the required size of less than 5 mm.
  • the sampling means 113 before entering the properly milled cards into the silo for storing waste 116 , the latter undergo automated sampling at the sampling means 113 , which periodically interrupt the flow of cards. For example, 300 kg of sample per 24 t batch may be sampled.
  • the sample is then analyzed by the analyzing means 114 after quartering in the laboratory in order to achieve a final sample mass of 4-5 kg. It is preferred to only treat a given batch of waste when the result of the analysis is known, in order to adapt the treatment parameters. This is why, before the sample analysis is carried out, the cards return via the return conveyor 119 to the storage means 103 .
  • the premises of the mills 109 , 111 are decontaminated, and the fines suspended in air are recovered and re-injected into the silo for storing waste 116 .
  • the milled electronic cards are then extracted at the base of the silo for storing waste 116 and feed the hoppers located above the entry of each of the three pyrolysis ovens 202 a , 202 b , 202 c .
  • the bulk density of the product is 0.7 at the entry of the ovens.
  • Pyrolysis is useful for degrading and removing the organic materials contained in the cards. This is a controlled combustion of carbonaceous chains, which is carried out while maintaining the metals of the waste in the metallic state.
  • the dwelling time in the ovens may be comprised between 20 and 90 min and is preferentially 30 min.
  • the operating temperature may be comprised between 350 and 550° C. and preferably have the value of about 400° C. By controlling the temperatures, the negative pressure and the screw velocity, it is possible to keep the operation under control.
  • Each oven typically has a treatment capacity of 1 t/h. Pyrolysis gases rich in phenolic compounds emerge at 400° C. from each oven.
  • the calcinated cards exiting each oven are cooled on the calcinated waste recovery line 203 (jacketed conveyor) and are then stored in the silos 204 a , 204 b feeding the copper leaching.
  • the product appears with a black appearance due to residual carbon from pyrolysis of the plastics. It has a density of about 0.5.
  • the pyrolysis gases from each oven are burnt at a high temperature in the post-combustion chamber 207 a , 207 b , 207 c (dwelling time of 2 s) in order to destroy all the carbonaceous molecules and possible dioxins and furans.
  • the oxidizing air is preheated to 400° C. in order to provide proper inflammation of the gases.
  • a controlled air supplement is required for regulating the chamber exit temperature to 1,100° C. and avoiding formation of NO R .
  • a supplemental 800 kW burner ensures that the temperature is sufficient for the combustion to occur, notably during the transient phases. Continuous control of the entry and exit post-combustion temperatures is achieved and the incoming dilution air may be regulated.
  • the gases at 1,100° C. arrive in the cooling chamber 210 in order to be subjected therein to water quenching.
  • the coolant water is fed at a flow rate of 10 m 3 /hour.
  • the water is entirely transformed into steam by absorbing a considerable portion of the energy of the gases.
  • the cooled gases exit the chamber at about 200° C. By controlling the exit temperature, it is possible to regulate the injected water flow rate.
  • the daily throughput of calcinated cards coming from the silos 204 a , 204 b containing 12 t of copper is treated in selective dissolution containers 301 a , 301 b (closed reactors) in 11 leachings, each lasting 4 hours.
  • the operation is as follows: transfer to the pump of 15 m 3 of copper-depleted and acid-rich electrolyte (at 85° C.) from the tank for storing depleted electrolyte 318 .
  • the depleted electrolyte is a solution containing sulphuric acid (50-200 g/L, preferably about 100 g/L) and soluble iron as iron sulphate (5-20 g/L, preferably about 10 g/L) which has to be maintained in the form of Fe 3+ (with oxygen) for efficiently etching the copper.
  • sulphuric acid 50-200 g/L, preferably about 100 g/L
  • soluble iron as iron sulphate 5-20 g/L, preferably about 10 g/L
  • Maintaining the temperature is provided by injecting fresh steam. Finally, the contents of the reactor are filtered on the press filter 306 a or 306 b or both. The copper-rich juices are transferred towards the tank for storing rich electrolyte 312 feeding the electrolysis cells.
  • the electrolyte is enriched with iron and nickel which are dissolved at the same time as copper.
  • a daily purge has to be carried out on the depleted electrolyte exiting the electrolysis cells. It is sent to the second tank for storing depleted electrolyte 319 and its treatment is carried out in the first stripping reactor 320 twice daily.
  • These very acid juices containing iron, nickel and a little copper are treated with lime up to a pH of 8.5. Calcium sulphate precipitates carrying along metal hydroxides.
  • This pulp is filtered on the additional press filter 324 .
  • the obtained residue (10-15 t/d) is placed in a landfill site.
  • the juices are recycled to the first tank for storing depleted electrolyte 318 .
  • the fines of the filter of the pyrolysis are treated in the second stripping reactor 325 every 2 days in the presence of water and some lime at pH 9.
  • the halides (mainly chlorides and bromides) pass into the solution.
  • the pulp is filtered on the additional press filter 324 : the residue (500 kg) is recycled to the selective dissolution containers 301 a , 301 b and the juices (3 m 3 ) enriched in halides are stored in a tank body for subsequent treatment.
  • the whole of the reactors, storage tanks, filters, are decontaminated and the vapors and droplets are absorbed by the washing tower 331 .
  • the obtained acid juices are regularly purged and recycled to the tank for storing depleted electrolyte 318 .
  • the depleted electrolyte is raised to 85° C. and maintained at this temperature by means of a coil fed with steam.
  • the rich electrolyte is cooled to 50° C. by a coil fed with cold water. This cold water may then be used in the chamber for vaporizing the hot gases from the post-combustion of the pyrolysis.
  • the wet solid residues (40 t/d) stemming from the press filter 306 a and 306 b are rich in precious metals. They are dried in the drying oven 308 . They are powdery and have a black color, the glass fibers which are the main compound thereof being broken during the stirring in the etching tank. The solid and liquid flows are regularly sampled and analyzed.
  • the flow stemming from the rectifiers passes in series from electrolysis cell to electrolysis cell and in parallel at the electrodes of each cell.
  • Current density may be from 50 to 400 A/m 2 , preferably about 200 A/m 2 and the temperature of the electrolyte may be from 20 to 80° C., preferably from 45 to 50° C.
  • the concentration of ferric ions is maintained as low as possible, and in any case at a level less than 10 g/L. When the total iron concentration reaches a value of 10-30 g/L, a portion of the electrolyte is purified by precipitation of iron and filtration of the precipitate.
  • the rich electrolyte coming from the tank for storing rich electrolyte 312 is sent into the 1st row of eight cells.
  • the cells are positioned as a cascade so as to allow circulation of the electrolyte and a pump sends back the juices from the last cell to the first.
  • the circulating flow rate is of the order of 15 m 3 /h.
  • the electrolyte takes 24 hrs for being depleted in copper which is deposited on the cathodes. By adding a surfactant, a fine and regular copper deposit may be obtained.
  • the depleted electrolyte is pumped towards the tank for storing depleted electrolyte 318 .
  • the cells are then again filled with rich electrolyte. Each row may be emptied and then filled with electrolyte every 4.5-5 hrs.
  • the step of selective copper extraction is important when the starting material contains a large copper proportion. Indeed, copper is able to form stable compounds which are insoluble in liquid lead, said compounds often containing precious metals. This is why it is necessary to get rid of the largest amount possible of copper before starting with the following lead covering and refining steps, otherwise a large amount of precious metals would be lost in said stable compounds.
  • the selective copper extraction step enables quasi the whole of the copper to be selectively extracted as a commercial product (pure copper cathodes), which may be re-melted as ingots.
  • the metals dissolved in the electrolyte iron, aluminium, nickel
  • electrodeposition of copper may be replaced with an operation of copper sulphate crystallisation, which is a commercial product.
  • the lead covering step comprises contacting the pre-treated materials (i.e. after milling, optional pyrolysis, optional copper extraction) with a molten lead-based composition in the lead covering container 15 .
  • the molten lead-based composition comprises lead in majority and may comprise from 0 to 50% tin, preferably less than 20% tin. This composition is in the liquid state. It is used as a collector and extractor of precious metals, which are found solubilized in a non-oxidized form.
  • the lead and optionally the tin of this composition partly stem from added metals contained in electronic cards, and partly from metals recovered subsequently.
  • Dissolution is carried out in the following way: stirring is started and it generates a vortex of molten lead in the kettle.
  • the feeder 407 pours the materials to be covered with lead into the core of the vortex.
  • the operation lasts for about 15 minutes.
  • the temperature may then be comprised between 350 and 550° C. and preferably is about 500° C.
  • a phase of skimming or phase of separating the elements without any affinity for lead is started subsequently.
  • stirring is stopped, and the inert portions with their precious metals (ceramics, glass fibers, ferrites . . . ) having been washed away move up to the surface where they float.
  • the skimming machine 405 is then started and with it the supernatant materials may be recovered. When these supernatant materials have been removed from the lead bath, the operation is repeated. Skimming may be carried out at a temperature comprised between 250 and 450° C., for example of about 270° C. for a lead-tin alloy with 30% by weight of tin.
  • the supernatant materials may again be treated in the same way in the additional lead covering container 18 . Indeed, a small amount of lead (and of precious metals) is carried away with the supernatant materials during skimming, and it is therefore useful to repeat the operation in a second kettle in order to avoid loss of precious metals.
  • the inert materials collected upon skimming at the additional lead covering material 18 are sent to a landfill as ultimate waste after having been optionally sampled and analyzed.
  • the molten lead-based composition contained in the additional lead covering container 18 has a small concentration of precious metals (less than 100 g per ton) and it is sent back by pumping towards the lead covering container 15 .
  • the lead covering phase may last for several days. It is considered that it is completed when the precious metal content in the molten lead-based composition reaches a threshold value, for example located between 2 and 4 kg per ton of lead.
  • a threshold value for example located between 2 and 4 kg per ton of lead.
  • One may then proceed with an optional decoppering operation, consisting of adding sulphur in the lead-based composition vortex, in order to form copper mattes which are sent back into a selective dissolution container 301 a , 301 b for extracting copper.
  • the molten lead-based composition with the solubilized precious metals is sent to a storage kettle from which this composition is cast into anodes (this forms the means for casting anodes 25 ).
  • the precious metals contained in the thereby cast anodes may be released.
  • lead and tin are removed from the anodes by electrolysis in a fluorosilicic medium, which is known as the Betts process, at the Betts electrolysis unit 501 .
  • the electrolysis cells are fed with an electrolyte for example containing about 90 g/L of lead and 80 g/L of free acid.
  • This electrolyte is prepared by solubilizing litharge (PbO) in fluorosilicic acid at the Betts reactor 503 .
  • Electrolysis may be carried out for example at a current density of 350 A/m 2 and at an electrolyte temperature of 40° C.
  • the solid lead and tin of the anodes are dissolved in the electrolyte, while the deposits of lead and tin build up on the cathodes.
  • surfactant By adding surfactant in the electrolyte, it is possible to make this deposit fine and smooth. The precious metals themselves remain at the anodes.
  • the electrolyte does not concentrate impurities or only very little.
  • a total purge may only be carried out once or twice a year.
  • the electrolyte is sent to the level of the second tank for storing depleted electrolyte 319 for a lime treatment in the first stripping reactor 320 , and a new electrolyte is prepared.
  • a partial purge may be required for lowering the lead content with sulphuric acid in the Betts reactor 503 .
  • the reactor 503 and the electrolysis cells are decontaminated and the gas effluents are sent to the washing tower 508 .
  • the washing juices are treated in the first stripping reactor 320 via the second tank for storing depleted electrolyte 319 .
  • Six days are required for consuming 80% of the anodes which therefore release their precious metals (432 kg) as anodic sludges, i.e. dissolved anode residues.
  • the anodic sludges may, depending on the cases, fall into dust in baskets or have an adhering cell structure.
  • electrolysis is interrupted before complete dissolution of the anodes. Anodic sludges may thereby be recovered by scraping.
  • the produced Ph/Sn cathodes represent 108 t for these six days. Two strippings of cathodes are advantageously performed every three days and two scrapings of the anodes at the same time. The cathodes are recycled towards the kettle 512 in order to produce commercial lead-tin in ingots and/or for feeding the additional lead covering container 18 with a molten lead-based composition.
  • the anodic sludges are washed, weighed and stored in a safe.
  • the anodic sludges are melted once to twice a week in the oxidation oven 520 at a temperature of 1,000° C.
  • This step of melting anodic sludges, in the presence of oxygen gas (or air) enables at least a portion of the lead and of the tin to be oxidized, which were still contained in the anodic sludges.
  • Litharge (PbO) forms at the surface: it is cast into plates and it may dope the electrolyte with lead when necessary.
  • the fumes from the oven are channeled towards the lead covering filter.
  • the liquid precious alloy may be cast into ingots (25 kg) which are stored batchwise in a safe. All the ingots are sampled and then weighed before being marketed.
  • the method described above is designed in order to limit as much as possible the losses of precious metals at all stages of the method.
  • the fine fragments of milled waste which pass into ambient air at the milling may again be introduced into the system;
  • the metal fraction carried away with the carbonaceous gas during pyrolysis may be recovered;
  • the copper which was not extracted during the selective extraction step by dissolution is recovered as copper mattes at the lead covering container 15 and is re-injected into the main circuit.
  • Tables 1 and 2 below give an estimation of the chemical composition of the products during the different steps of the treatment method, in the case when the waste is typical used electronic cards.

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  • Mechanical Engineering (AREA)
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  • Metallurgy (AREA)
  • Environmental & Geological Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Geology (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Electrolytic Production Of Metals (AREA)
  • Processing Of Solid Wastes (AREA)
  • Incineration Of Waste (AREA)
  • Gasification And Melting Of Waste (AREA)
US12/446,158 2006-10-20 2007-10-19 Method for treating waste containing precious metals and device for implementing said method Abandoned US20100181205A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR0609219A FR2907352B1 (fr) 2006-10-20 2006-10-20 Procede de traitement de dechets contenant des metaux precieux et dispositif pour la mise en oeuvre de ce procede.
FR0609219* 2006-10-20
PCT/FR2007/001728 WO2008047010A2 (fr) 2006-10-20 2007-10-19 Procede de traitement de dechets contenant des metaux precieux et dispositif pour la mise en oeuvre de ce procede

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JP (1) JP5284970B2 (fr)
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US20130276284A1 (en) * 2010-04-15 2013-10-24 Advanced Technology Materials, Inc. Method for recycling of obsolete printed circuit boards
US9221114B2 (en) 2011-12-15 2015-12-29 Advanced Technology Materials, Inc. Apparatus and method for stripping solder metals during the recycling of waste electrical and electronic equipment
US20170158975A1 (en) * 2015-12-04 2017-06-08 Lubor JANCOK Device for the production of fuel gas from materials of organic and/or inorganic origin
CN108505069A (zh) * 2018-03-30 2018-09-07 西安瑞鑫科金属材料有限责任公司 一种从铱铑合金废料中回收铱、铑的方法
US10202668B2 (en) * 2015-08-27 2019-02-12 All Green Recycling, Inc. Metal recovery processes
US10597753B2 (en) * 2015-08-27 2020-03-24 All Green Recycling, Inc. Systems and methods of efficiently recovering precious metals using an alkaline leach, ultrasound, and electrolysis

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EP2584262A1 (fr) 2011-10-21 2013-04-24 Cockerill Maintenance & Ingenierie S.A. Procédé de traitement pyrolytique de résidus organiques et inorganiques en four à étages pour la récuperation de sous-produits valorisables
WO2013057073A1 (fr) 2011-10-21 2013-04-25 Cockerill Maintenance & Ingenierie S.A. Procede de traitement pyrolytique de résidus organiques et inorganiques en four a etages pour la récupération de sous-produits valorisables
KR101192290B1 (ko) 2012-06-27 2012-10-17 한국지질자원연구원 연속식 용융염 전해 장치
KR101192292B1 (ko) 2012-06-27 2012-10-17 한국지질자원연구원 일체형 챔버를 이용한 용융염 전해 방법
CN102994759B (zh) * 2012-11-28 2015-09-30 大连东泰产业废弃物处理有限公司 一种废弃催化剂中贵金属的回收装置
CA2983350A1 (fr) 2015-04-21 2016-10-27 University Of Saskatchewan Procedes de lixiviation et d'extraction simultanees de metaux precieux
CN114959271B (zh) * 2022-05-18 2024-01-23 济源豫金靶材科技有限公司 一种溅射银残靶材的回收方法

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US9221114B2 (en) 2011-12-15 2015-12-29 Advanced Technology Materials, Inc. Apparatus and method for stripping solder metals during the recycling of waste electrical and electronic equipment
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US10597753B2 (en) * 2015-08-27 2020-03-24 All Green Recycling, Inc. Systems and methods of efficiently recovering precious metals using an alkaline leach, ultrasound, and electrolysis
US20170158975A1 (en) * 2015-12-04 2017-06-08 Lubor JANCOK Device for the production of fuel gas from materials of organic and/or inorganic origin
US9809768B2 (en) * 2015-12-04 2017-11-07 Lubor JANCOK Device for the production of fuel gas from materials of organic and/or inorganic origin
CN108505069A (zh) * 2018-03-30 2018-09-07 西安瑞鑫科金属材料有限责任公司 一种从铱铑合金废料中回收铱、铑的方法

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FR2907352B1 (fr) 2009-02-20
JP5284970B2 (ja) 2013-09-11
WO2008047010A2 (fr) 2008-04-24
CA2666767A1 (fr) 2008-04-24
FR2907352A1 (fr) 2008-04-25
MX2009004208A (es) 2009-09-04

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