JP5284970B2 - Method for treating waste containing precious metals and apparatus for carrying out the method - Google Patents

Description

  The present invention relates to a method for treating waste containing noble metals and an apparatus for carrying out the method.

  Increasing use of calculators, cell phones, electronic equipment and other short-lived high-tech devices has increased the amount of waste, including rare and precious metals. In this situation, there arises a problem of processing and recovering the metal contained in the waste. Such waste is a non-ferrous rare and valuable metal source.

  Electronic waste is currently collected, transported and processed in large-scale industrial facilities for non-ferrous metals, where several plants are required to be used continuously, lead, copper and Zinc is extracted and these high-value materials are diluted in the raw material stream of mining or secondary sources. Thus, current methods are optimal for producing large amounts of lead, copper and pure zinc, but are difficult to apply to producing rare or noble metals that are present in small amounts.

  Therefore, it would be desirable to design a waste disposal method that can recover a high percentage of precious metals contained in waste.

The first object of the present invention is to
Contacting the waste containing the noble metal with the first molten lead-based composition;
- by Jokasu the first mixture obtained, and the first mixture after skimming containing the noble metal, recovering the suspended solids, respectively (b), and - a first mixture obtained by the Jokasu Recovering the noble metal by refining by electrolysis (c) ,
A waste treatment method comprising the following steps :
The debridement step (b),
-Contacting the recovered suspended matter with the second molten lead-based composition (b-1),
-Removing and recovering the resulting second mixture (b-2), and
-Including the step (b-3) of supplying the second mixture after removal containing the obtained noble metal to the step (a) as at least a part of the first molten lead-based composition;
The first molten lead-based composition contains at least the second mixture after the removal, contains lead as a main component, 0 to 50% tin and a low concentration (less than 100 g per ton) noble metal. ,
The second molten lead-based composition contains lead separated from the noble metal and / or fresh lead in the step (c), contains lead as a main component, and contains 0 to 50% tin. It is to provide a waste disposal method .

In certain embodiments, purifying the first mixture described above Jokasu (c) is,
-Forming an anode by molding the first mixture removed (c-1) ,
-Electrolyzing a fluorosilicic acid solution using the anode (c-2) ,
-Recovering anodic sludge containing precious metal (c-3)
Equipped with a.

In a particular embodiment, the method comprises before or after or simultaneously with the step (c-3) of recovering the anodic sludge.
Recover lead and optionally cathode deposits of tin and supply them as at least part of the first and / or second molten lead-based composition;

In a particular embodiment, after the sub-step (c-3) of anodic sludge recovery, the step (c) of purifying the first mixture thus removed comprises the following sub-steps:
-Melting the recovered anodic sludge in the presence of oxygen (c-4) ,
A step of removing molten anodic sludge (c-5) , and a step of forming an ingot by molding molten and removed anodic sludge (c-6) ,
Is provided.

In a particular embodiment, the first and second molten lead-based compositions contain less than 20% tin.

In certain aspects, prior to contacting the waste with the molten lead-based composition,
-Extracting copper from waste by selective dissolution.

In certain aspects, the copper extraction step comprises
-Selectively dissolve waste in the presence of sulfuric acid, iron sulfate and oxygen;
The resulting solution is treated by filtration and / or electrolysis and / or precipitation;
-Collect copper on the one hand and other metal impurities on the other,
Substeps are provided.

In certain aspects, prior to the copper extraction step, the method comprises:
-Combusting waste by pyrolysis to produce carbonaceous gas, and if necessary,
-Post-combustion of the carbonaceous gas,
Comprising steps.

  In certain embodiments, the method further comprises a preliminary step of grinding the waste and / or analyzing the ground waste.

  In certain embodiments, the noble metal comprises a metal selected from gold, silver, platinum, palladium, rhodium, ruthenium, iridium, osmium, and mixtures thereof.

  In certain embodiments, the waste is selected from electronic waste such as catalyst exhaust mufflers and electronic cards.

  In a particular embodiment, 90% by weight or more, preferably 99% by weight or more of the noble metal contained in the waste is recovered.

In a particular embodiment, the suspended material includes ceramics, glass fibers and / or ferrite.

Another object of the present invention is a facility for treating waste containing precious metals,
-At least one lead-coated container filled with a first molten lead-based composition, wherein the waste pre-treated material is brought into contact with the first molten lead-based composition to prepare a first mixture ( 15),
- is connected to the inlet of該鉛coating container (15), the line for supplying the first molten lead-based composition (24),
- which is connected to the inlet of the lead covering container (15), the line for supplying the pretreated substance (14),
-A removal means (16) in cooperation with the lead-coated container (15);
- connected to the outlet of the lead covering container (15), a line to eject the said first mixture as Jokasu (21),
- it is connected to the first mixture taken out to the line (21) that the Jokasu, wherein said means for purifying the electrolyte of the first mixture after skimming (36), and - a first mixture that said Jokasu comprising means outlet to the connected precious metal extraction line (36) (38) to purify,
further,
-A line (17) connected to the outlet of the removal means (16) and for removing suspended matter generated by removal;
-Connected to the line (17) for taking out the suspended solids on the one hand, and connected to the line (31) for supplying the second molten lead based composition on the other side, the suspended solid and the second molten lead based composition At least one additional lead-clad container (18) to prepare a second mixture by contacting
-Additional removal means (19) associated with the additional lead-clad container (18), and
-A line connected to the outlet of the additional lead-clad container (18) and connected to the first molten lead-based composition supply line (24) to take out the second mixture after removal containing noble metals. (22)
The first molten lead-based composition contains at least the second mixture after the removal, contains lead as a main component, 0 to 50% tin and a low concentration (less than 100 g per ton) noble metal. ,
Waste treatment in which the second molten lead-based composition contains lead and / or fresh lead separated from the noble metal by the refining means (36), contains lead as a main component, and contains 0 to 50% tin. Is to provide facilities.

In a particular embodiment, the means (36) for purifying the first mixture after said decontamination by electrolysis comprises :
-Anode molding means (25),
-A Betz electrolysis means (27) and-an anodic sludge recovery means (28).

In a particular embodiment, the means (36) for purifying the first mixture after said decontamination by electrolysis comprises :
A lead-tin recovery means (29) connected to the second molten lead-based composition supply line (31);

In certain embodiments, further
A copper extraction means (37), one outlet of which is connected to the pretreatment substance supply line (14), and a main raw material supply line (6) connected to the inlet of the copper extraction means (37).

In a particular embodiment, the copper extraction means (37)
At least one selective melting container (7) connected to the main raw material supply line (6),
A consumable electrolyte supply line (11) connected to the inlet of the selective dissolution container (7),
Electrolysis means (9),
-Enriched electrolyte transfer means (8) for connecting the selective dissolution container (7) to the electrolysis means (9);
A cathode stripping means (13) and a consumable electrolyte circulation means (10) connected to the outlet of the electrolysis means (9).

In certain embodiments, further
A waste pyrolysis means (2) connected to the inlet of the main raw material supply line (6),
-A waste supply line (1) connected to the pyrolysis means (2); and-if necessary, provided at the outlet of the pyrolysis means (2) and connected to the post-combustion means (5). A gas discharge line (4).

In certain embodiments, further
-It is connected to the raw material waste supply line (1bis), and further comprises grinding and analysis means (1ter) connected to the waste supply line (1).

  In a particular embodiment, the aforementioned method can be applied to the aforementioned equipment.

  In a particular embodiment, the aforementioned equipment is intended to be used for carrying out the aforementioned method.

  The present invention makes it possible to solve the disadvantages of the prior art. More particularly, it provides a specific method for treating and recovering waste containing precious metals, which coordinated the metallurgical approach to dilute the metals contained in the main metal production flow. To avoid. The present invention further provides a single facility for separating components from waste, particularly for recovering precious metals.

In certain embodiments, the invention has the features listed below.
-The method of the invention is very responsive and can cope with predictable changes in the composition of the electronic card.
-The process according to the invention does not have the disadvantage of using the conventional technique of extracting noble metals by lead oxidation, the so-called ash-blow operation followed by lead oxide reduction.
In the present invention, the metal can be maintained in the metal form as much as possible, and the precious metal is kept in the metal form throughout the method. Hold lead and tin in metallic form until step (d). Thereby, it is possible to minimize the precious metal being carried away by the metal oxide.
In the present invention, precious metals can be collected in a single output.
-The present invention can be applied taking into account the controlled environmental impact.

It is the schematic which illustrates the facility for waste disposal by this invention. The schematic illustrating the grinding and analysis means used in the framework of the waste treatment facility according to the invention. Dotted arrows indicate gas flow. Double arrows indicate solid flow. The schematic illustrating the pyrolysis and post-combustion means used in the framework of the waste treatment facility according to the invention. Dotted arrows indicate gas flow. Simple black arrows indicate liquid flow. Double arrows indicate solid flow. The schematic diagram illustrating the copper extraction means used in the framework of the waste treatment facility according to the present invention. Dotted arrows indicate gas flow. Simple black arrows indicate liquid flow. Double arrows indicate solid flow. FIG. 4 shows a special example of a lead-clad container used in the framework of the present invention. The schematic diagram illustrating the purification means used in the framework of a waste treatment facility according to the invention. Dotted arrows indicate gas flow. Simple black arrows indicate liquid flow. Double arrows indicate solid flow.

  The present invention is described in detail below, but these do not limit the present invention.

[Waste treatment equipment]
FIG. 1 schematically shows a waste treatment facility according to the invention, which comprises the following elements:

  A waste supply line 1 exists at the entrance of the treatment facility. The waste supply line 1 may be connected to the outlet of the pulverization and analysis means 1ter supplied from the raw material waste supply line 1bis.

  As with other supply, transfer and intake lines described herein, the waste supply line 1 may have a single path or multiple parallel paths (branches).

In a variant of the invention, the waste supply line 1 is connected to the pyrolysis means 2. A main raw material supply unit 6 is connected to the outlet of the thermal decomposition unit 2, and a copper extraction unit 37 is connected to the unit 6. A pretreatment substance supply line 14 is connected to an outlet of the copper extraction means 37, and a lead-coated container 15 is connected to the line 14. This aspect is particularly suitable for processing used electronic cards.

In another modification, there is no pyrolysis means 2 and the waste supply line 1 is directly connected to the copper extraction means 37 (in this case, the waste supply line 1 coincides with the main raw material supply means 6. Conceivable).

In another modification, the copper extraction means 37 is not provided, and the main raw material supply means 6 is directly connected to the lead-coated container 15 (in this case, the main raw material supply means 6 coincides with the pretreatment substance supply line 14. it is conceivable that).

  In yet another variation, both the pyrolysis means 2 and the copper extraction means 37 are absent, and the waste supply line 1 is directly connected to the lead-coated container 15 (in this case, the waste supply line 1 and the pretreatment material). The supply lines 14 are considered to coincide). This variant is particularly suitable for the treatment of used exhaust mufflers, since the mufflers are substantially free of copper.

When a pyrolysis means is present, its outlet is connected to a gas discharge line 4 which is connected to a post-combustion means 5.

If the copper extraction means 37 is present, the means 37 may include a selective dissolution container 7 having one inlet connected to the main raw material supply means 6 and the other inlet connected to the consumable electrolyte supply line 11. good. Next, a pretreatment substance supply line 14 is connected to the outlet of the selective decomposition container 7, and the enriched electrolyte transfer line 8 is connected to the electrolysis means 9. A cathode stripping means 13 is installed in association with the electrolysis means 9, and a consumable electrolyte circulation line 10 is connected to the outlet of the electrolysis means 9. The consumable electrolyte circulation line 10 is connected to a consumable electrolyte supply line 11 and / or a consumable electrolyte treatment line 12.

The lead-coated container 15 connected to the pretreatment substance supply line 14 is also connected to a molten lead-based composition supply line 24. The removal means 16 is linked to the lead-coated container 15. The first mixture take-out line 21 removed is connected to the outlet of the lead-coated container 15, and the first mixture purification means 36 removed is connected to the line 21. A noble metal take-out line 38 is installed at the outlet of the removed first mixture purification means 36.

Line 17 to eject the floating substances generated by skimming is installed at the outlet of the skimming unit 16, the line 17 is connected to an additional lead covering container 18. This additional lead-clad container 18 is then connected to an additional molten lead-based composition supply line 31. An additional removal means 19 is installed in conjunction with the additional lead-clad container 18, and a removed second mixture removal line 22 is connected to the outlet of the additional lead-clad container 18. This additional dehumidified second mixture take-out line 22 is connected to the demixed mixture purification means 36 in the same manner as the deraised first mixture take-out line 21. However, in a preferred variant, the stripped second mixture removal line 22 is connected to a molten lead-based composition supply line 24. A replenishment source of the molten lead-based composition 23 may be installed to complete the supply. A second mixture withdrawal line 20 that Jokasu may be provided an outlet for additional skimming means 19.

More specifically, the stripped mixture purification means 36 includes an anode molding means 25, an anode transfer system 26, and a Betts electrolysis means 27. The Betz electrolysis means 27 is provided with a lead-tin recovery means 29 and an anodic sludge recovery means 28. The lead-tin recovery means 29 (optionally with a fresh lead supply line 30) is connected to an additional molten lead-based composition supply line 31.

The anodic sludge recovery means 28 is connected to the melting means 33, and the oxygen supply section 32 is provided in the means 33. The last removal means 34 cooperates with the melting means 33. The noble metal removal line 38 is connected to the outlet of the melting means 33, which means 33 includes a residue line 35.

  Referring now to FIG. 2, the first stage of the waste treatment facility for receiving, pulverizing and analyzing incoming waste (reference numbers 1bis, 1ter in FIG. 1) will be described in detail.

In this example, the installation comprises waste receiving means 101, which comprises an unloading hole suitable for receiving trucks, for example. The waste receiving means 101 is provided with a weighing means 102 in addition to the storage means 103. At the outlet of the storage means 103, an administration means 104 for discharging waste on a main conveyor 105 (belt or the like) is provided. The main conveyor 105 is connected to the first secondary conveyor 106, the second secondary conveyor 107, and the third secondary conveyor 108.

The first secondary conveyor 106 is connected to the coarse grinding mill 109. The fine grinding mill 111 is connected on the one hand to the second secondary conveyor 107 and on the other hand to the transfer line 110 starting from the outlet of the coarse grinding mill 109. The mills 109 and 111 may each have a capacity of 5 to 10 t / hour. The collector conveyor 112 is installed at the outlet of the fine grinding mill 111 and is connected to the third secondary conveyor 108. A sample means (for example, a handle) 113 is installed in the path of the third secondary conveyor 108, and an analysis means 114 is connected to it.

Further, the third secondary conveyor 108 is connected to the first tertiary conveyor 115 and the second tertiary conveyor 117. The first tertiary conveyor 115 is connected to a storage 116 for storing waste. The second tertiary conveyor 117 is connected to the container 118, and a return conveyor 119 is connected to the storage means 103 at the outlet . An air decontamination system 120 is installed in the coarse mill 109 and the fine mill 111 and connected to the sleeve filter 121, the typical capacity of which is 5000 Nm ³ / hour. The sleeve filter 121 is connected to a chimney 123 and a fine material recovery line 122, which is connected to a storage 116 for storing waste.

  It is clear that the person skilled in the art can apply the means described so far to meet the requirements of the installation, for example by changing the number and type of mills or changing the capacity of different mills used. It is.

With reference to FIG. 3, a feasible example of the portion of the processing facility between the waste supply line 1 (hereinafter 201) and the main raw material supply means 6 (hereinafter 205a and 205b) will be described in detail.

In this example, the waste supply line 201 is provided on the outlet side of the storage 116 for storing the waste, and is connected to the pyrolysis ovens 202a, 202b, and 202c arranged in parallel through a hopper. Yes. The pyrolysis ovens 202a, 202b, and 202c may be tubular screw ovens that are electrically heated from the outside. For example, an oven having a length of 5 m, a diameter of 40 cm, a power of 100 kW, and a variable screw speed can be used. The number of ovens will vary depending on the needs of each facility.

The calcined waste collection line 203 is provided on the outlet side of the pyrolysis ovens 202a, 202b, 202c, and is connected to the two calcined waste storages 204a, 204b. The number of these stores varies depending on the needs of each facility. The baking waste collection line 203 may be a conveyor having a jacket equipped with water cooling means. Main raw material supply pipes 205a and 205b are provided at the outlets of the respective fired waste storages 204a and 204b (both these pipes form a main raw material supply line 6).

Further, gas discharge pipes 206a, 206b, 206c (all of these pipes correspond to the gas discharge pipe 4 described above) are provided at the outlets of the respective pyrolysis ovens 202a, 202b, 202c. The gas discharge pipes 206a, 206b, and 206c are connected to post-combustion chambers 207a, 207b, and 207c, respectively. An example of a typical capacity of the post combustion chambers 207a, 207b, 207c is 15 m ³ . Air introducing pipes 208a, 208b, and 208c are connected to the post combustion chambers 207a, 207b, and 207c, respectively.

Burnt gas collection pipe 209, each post combustion chambers 207a, 207b, the exit 207c, are connected to the inlet of the vertical cooling chamber 210. A water coolant supply line 211 is also connected to the inlet of the cooling chamber 210. For example, a spray ramp may be provided at a high place in the cooling chamber. A preliminary cooling gas recovery pipe 212 is provided on the outlet side of the cooling chamber 210 and is connected to the sleeve filter 214. An air introduction pipe 213 is connected to the preliminary cooling gas recovery pipe 212. The sleeve filter 214 has a capacity of, for example, 4000 Nm ³ / hour. A fine substance recovery line 215 and a removed gas recovery pipe 216 are connected to the outlet of the sleeve filter 214. The removed gas recovery pipe 216 is connected to the chimney 217.

  With reference to FIG. 4, some feasible examples of processing equipment with copper extraction means 37 are described in detail below.

Each main raw material supply pipe 205a, 205b is connected to a selective dissolution container 301a, 301b, respectively. Each container is provided with a 20 m ³ thick epoxy resin / glass fiber, for example, equipped with a lid and a variable speed stirrer. It may be a closed reactor. Although a single container may be installed in this way, a plurality of containers may be installed according to production needs. A consumable electrolyte supply line 303 is also connected to each selective dissolution container 301a, 301b. Furthermore, an oxygen supply unit 304 is connected to the bottom of each selective dissolution container 301a, 301b.

Selective post melt removal lines 305a, 305b are connected to the outlets of the selective melt containers 301a, 301b and to the press filters 306a, 306b. A solids collection system 307 is located on the outlet side of the press filters 306a, 306b and is connected to a drying oven 308 at the outlet of the oven 308 to the pretreated material tube 309 (reference numeral 14 in FIG. 1). Connected) is connected. The drying oven 308 may be a screw oven as used for thermal decomposition.

Further, filtrate outlet pipes 310 a and 310 b are provided at the outlets of the press filters 306 a and 306 b, respectively, and each pipe is connected to a single bat 302. The bat 302 is then connected via a transfer line 311 to a tank 312 for storing an enriched electrolyte having a capacity of, for example, 60 m ³ .

The other major element of this part of the facility is an electrodeposition unit 314. The electrodeposition unit 314 includes a certain number of electrolytic tanks 315a, 315b, 315c, 315d, and 315e, and the number of tanks (in this example, five) can be determined according to production needs. Each of the electrolytic tanks 315a, 315b, 315c, 315d, and 315e includes a certain number (for example, eight in this example) of electrolytic cells according to production needs. For example, each electrolytic cell has 31 cathodes made of stainless steel and an anode made of lead / calcium having an effective volume of 4 m ³ and an effective surface area of 1 m ² on each side. The electrolytic tanks 315a, 315b, 315c, 315d, and 315e are connected in parallel to the enriched electrolyte transfer pipe 313 connected to the outlet of the tank 312 that stores the enriched electrolyte. Finally, the electrodeposition unit 314 is provided with a cathode stripping system 316.

A consumable electrolyte recirculation line 317 is provided at the outlet of the electrodeposition unit 314. The line 317 contains a first tank 318 (for example, having a capacity of 60 m ³ ) for storing the consumable electrolyte and a consumable electrolyte. It is connected to a second tank 319 for storage (for example having a capacity of 25 m ³ ). The first tank serves as a source for supplying the consumable electrolyte supply line 303. The second line 319 is connected to a first stripping reactor 320 (eg having a capacity of 15 m ³ ). A lime supply line 321 is connected to the first stripping reactor 320. A first pulp removal line 323 is connected to the first stripping reactor 320, and the line 323 is connected to an additional press filter 324.

Further, the fines recovery line 215 described in FIG. 3 is connected to a second stripping reactor 325 (for example, having a capacity of 5 m ³ ) equipped with a water and lime supply unit (not shown). A second pulp removal line 326 is connected to the outlet of the reactor 325, and an additional press filter 324 is connected to the line 326. The outlet of the additional press filter 324 is connected with a washed fines take-out line 327, a lime sulfate take-out line 328, and an acidic juice take-out line 329. The cleaned fine substance take-out line 327 may be connected to one or both of the selective dissolution containers 301a and 301b. The acid juice take-out line 329 may be connected to a tank body (not shown) together with additional equipment on the downstream side for processing halides.

The gas removal system 330 passes through all of the storage tanks 312, 318, 319, selective dissolution containers 301 a, 301 b and stripping reactors 320, 325 and is connected to the washing tower 331. The storage tanks 312, 318, 319, selective dissolution containers 301a, 301b and stripping reactors 320, 325 may be in standard thickness epoxy resin / glass fiber. The washing tower 331 may be connected to an acid juice extraction line 332 at an outlet thereof, and the line may be connected to the consumable electrolyte storage tank 318 in a circulation manner. The washing tower 331 has a capacity of 5 m ³ and a standard lining and may be operated with water.

  Referring back to FIG. 1, the lead-clad container 15 and the additional lead-clad container 18 may be those illustrated in FIG.

Each container comprises a kettle 401 (for example having a volume of 50 tons) surrounded by a heating chamber 402 fitted with a burner 403. A stirrer 404 (eg, having a vertical axis propeller) is immersed in the kettle 401. The kettle 401, feeder 407 is connected is connected to a line 17 to eject the floating substances generated by the outlet or skimming before treatment supply line 14 as required to the feeder 407. The sides of the kettle 401, skimming machine 405 is installed, the skimming device 405 consists of a scraper with a stainless steel joint arm attached to the inclined surface. The enveloping cover 406 allows the contents of the kettle contents to be separated and is applied for nitrogen deactivation. A suction means 408 is installed above the cosmetic and is connected to a sleeve filter (not shown). Combustion gas discharge means 409 applied to the collection of gas discharged from the burner is connected to the heating chamber 402. The stirrer 404 disassembles and enables the contents of the kettle 401 to be transferred.

Downstream of the lead-coated containers 15 and 18, the anode forming device 25 is provided, which is provided with a kettle of the type shown in FIG. 5, skimming and stirring means may be omitted. The kettle may be provided with a surrounding cover and a suction device.

  The last main part of the installation is related to purification and is related to the reference numerals 27, 33, 34 in FIG. Reference numerals 27, 33, and 34 will be described with reference to FIG.

This equipment part comprises a Bet's electrolysis unit 501, which includes a plurality (two in this example) of Bet's cell series 502a, 502b. Each electrolytic cell row 502a, 502b includes, for example, five electrolytic cells, each electrolytic cell includes 30 anodes and 31 cathodes, the effective surface area per surface is 1 m ² , and the cell volume is 4 m ³ . is there. The electrolytic solution is supplied in parallel from the Bets reactor 503 to the electrolytic cell rows 502a and 502b. A return pump system may be provided to facilitate the circulation of the electrolyte. A fluorosilicic acid supply line 504 is connected to one end of the Betz reactor 503, and a lead monoxide supply line 505 is connected to the other end. At the outlet of the Betz electrolysis unit 501, a used Betz electrolyte collection line 506 is provided and returned to the second tank 319 for storing consumable electrolyte in FIG.

The electrolytic removal system 507 performs gas collection in the Betz electrolysis unit 501 and Betz reactor 503 and transfer to the washing tower 508 and has a typical capacity of 5 m ³ . The washing juice collection line 509 returns toward the second tank 319 for consumable electrolyte storage in FIG.

The Betz electrolysis unit 501 is also provided with a cathode peeling means 510. The cathode stripping means 510 has a cathode supply line 511 for supplying the cathode to the kettle 512 to melt the cathode. Kettle 512 is of the type described in FIG. 5, skimming and stirring means may be omitted. The kettle may be provided with a surrounding cover and a suction device. The cathode melt is supplied with a lead-tin supply line 513 and possibly a fresh lead supply line 30 and an additional molten lead-based composition supply line 31 (see FIG. 1). The entirety of reference numerals 510 to 513 corresponds to the lead-tin recovery means 29.

The Betz electrolysis unit 501 is further provided with an anode stub collecting means 514, which is connected to the anode sludge collecting means 516 (the whole constitutes an example of the anodic sludge collecting means 28). This anodic sludge recovery means 516 is connected to an anodic sludge treatment unit 517, which unit 517 comprises cleaning means, metering means and / or safety storage means. The cleaned sludge transfer line 518 connects the anodic sludge treatment unit 517 to an oxidation oven 520 (eg, 800 kW power, 1 ton capacity), which has an air or oxygen intake line 519 at its inlet. . An ingot collection line 521 is connected to the outlet of the oxidation oven 520 to ensure return to the safe storage means of the anode sludge collection means 516. The resurge supply line 505 is also connected to the outlet of the oxidation oven 520. A fume collection line 522 is also provided in the oxidation oven 520, which may be connected towards the same filtration system provided in the lead-coated container.

[Waste disposal method]
A method for treating a waste, which is a used electronic card, containing a noble metal will be exemplified below. In this case, the method comprises five main processes.
―Crush,
-Pyrolysis,
-Copper extraction by selective dissolution (leaching)
-Lead coating and-Purify.

  This example corresponds to the use of the processing equipment described above in connection with FIGS. The production capacity is 25,000 tons of waste per year, or 72 tons per day. If the waste is a catalyst muffler, it is possible to dispense with pyrolysis and copper extraction steps.

  The waste receiving means 101 receives the electronic card. The electronic cards arrive in batches (containers, large bags, barrels) at the entrance of the equipment, are weighed by the weighing means 102, labeled, recorded, and stored in the storage means 103.

The card is accepted in three main forms.
1) All cards need to be crushed twice before processing.
2) The card before crushing requires simple crushing before processing.
3) A properly crushed card is less than 5 mm in size and does not require additional crushing before processing.

  Depending on the properties of the card in the transport system described above, the card is sequentially sent to the coarse grinding mill 109 and the fine grinding mill 111 (the case 1), or directly sent to the fine grinding mill 111 (the case 2), or This is because it is sent directly to the storage 116 (the case 3). Coarse mill 109 crushes or crushes the waste to a size of less than 25 mm, while crush mill 111 crushes or crushes the waste to a size of less than 5 mm. Further, before the appropriately crushed card is put into the storage 116, the storage 116 performs automatic sampling of the card by the sample means and periodically interrupts the flow of the card. For example, a sample of 300 kg is sampled every 24 t batch. The sample is then analyzed by the analysis means 114 after being assigned in the laboratory to a final sample volume of 4-5 kg. In order to apply the processing parameters, it is preferable to process only a predetermined batch of waste when the analysis results are known. This is why the card returns to the storage means 103 through the return conveyor 119 before performing sample analysis.

  The sites of the mills 109 and 111 are decontaminated, and fine substances floating in the air are collected and reintroduced into the waste storage.

  Next, the crushed electronic card is extracted in the storage 116 and supplied to a hopper located above the respective inlets of the three pyrolysis ovens 202a, 202b, 202c. The bulk density of the product at the entrance of the oven is 0.7. Thermal decomposition is useful for degrading and removing organic matter contained in the card. This is controlled combustion of the carbon chain and is performed while maintaining the metal in the waste in a metallic state.

  The residence time in the oven is 20 to 90 minutes, preferably 30 minutes. The operating temperature is 350 to 550 ° C., preferably 400 ° C. or higher. By controlling temperature, negative pressure and screw speed, the operation can be put under control. Each oven has a throughput of 1 t / hour. A pyrolysis gas rich in phenolic compounds is generated at 400 ° C. from each oven.

  The baked card taken out from each oven is cooled on a baked waste collection line 203 (a conveyor having a jacket) and stored in the storage 116. Due to residual carbon from the pyrolysis of the plastic, the product has a black appearance. Its density is about 0.5.

  The pyrolysis gas from each oven is burned at a high temperature in the post-combustion chambers 207a, 207b, and 207c (residence time is 2 seconds), and decomposes all carbonaceous molecules and dioxins and furans that may exist. As a result, all the carbon chains are recovered in the form of energy and can be used in actual processes. Preheat the oxidizing air to 400 ° C. to give the gas an appropriate ignitability. In order to avoid the generation of NOx by controlling the combustion chamber outlet temperature to 1100 ° C., it is required to control the air supply. The use of an additional 800 kW burner ensures the temperature required for combustion, especially in the transition state. Continuously control inlet and outlet post-combustion temperatures and control incoming dilution air.

The 1100 ° C. gas reaches the cooling chamber 210 where it is cooled with water. The cooling water is supplied at a flow rate of 10 m ³ / hour. Water is completely converted into steam by absorbing a significant portion of the energy of the gas. The cooled gas is withdrawn from the combustion chamber at a temperature of about 200 ° C. By controlling the outlet temperature, the flow rate of the injected water can be controlled.

  The gas is then cooled to about 150 ° C. with air and enters the sleeve filter 214. The sleeve holds fine solid particles, particularly particles containing halide. The removal takes place at the next copper leaching site. All removed gas is rejected by the chimney 217. Perform continuous tracking (gas analysis, dust level).

  Copper extraction requires a series of wet operations: leaching in oxidizing acid medium, residue filtration, use of several reactors, storage tanks, filter and pump, and electrolytic cell set and current generator It is performed by the electrodeposition of copper.

The daily processing of the baked cards from the reservoirs 204a, 204b with 12t of copper takes place in selective dissolution containers 301a, 301b (closed reactors), each performing 11 leachings lasting 4 hours. Processing is as follows. From the consumable electrolyte storage tank 318, the electrolyte (about 85 ° C.) enriched with copper and acid is transferred to a 15 m ³ pump. The 4.8 ton calcined card is then introduced into the bottom of the reactor with fine oxygen bubbling. The exhausted electrolyte is a solution containing sulfuric acid (50 to 200 g / L, preferably about 100 g / L) and soluble iron (5 to 20 g / L, preferably about 10 g / L) as iron sulfate. In order to perform this etching effectively, it must be maintained in the form of Fe ³⁺ (including oxygen).

  The temperature is maintained by injecting fresh steam. Finally, the reactor contents are filtered by press filters 306a, 306b or both. The copper-enriched juice is transferred to the enriched electrolyte storage tank 312 connected to the electrolytic cell.

  The electrolyte is enriched with iron and nickel dissolved simultaneously with copper. Daily purification of the consumable electrolyte coming out of the electrolytic cell is necessary. The consumable electrolyte is sent to the second consumable electrolyte storage tank 319, and the treatment is performed twice a day in the first stripping reactor 320. These very acidic juices containing iron, nickel and a small amount of copper are treated with lime until the pH is 8.5. Calcium sulfate precipitates with the metal hydroxide. This muddy thing is filtered with an additional press filter 324. The resulting residue (10-15 t / day) is located at the landfill site. Juice is recirculated to the first consumable electrolyte storage tank 318.

The pyrolysis filter fines are treated in a second stripping reactor 325 twice a day in the presence of water and pH 9 lime. Halides (primarily chloride and bromide) dissolve in solution. The muddy material is filtered with an additional press filter 324. The residue (500 kg) is recycled to the selective dissolution containers 301a, 301b, and the halide-enriched juice (3m ³ ) is stored in a tank for subsequent processing.

  The reactor, storage tank, and filter are all decontaminated, and water vapor and liquid suitability are absorbed by the washing tower 331. The resulting acidic juice is periodically purified and recycled to the consumable electrolyte storage tank 318.

  During the process, the depleted electrolyte is heated to 85 ° C. and maintained at this temperature with a coil supplied with steam. The enriched electrolyte is cooled to 50 ° C. by a coil supplied with cold water. This cold water is then used in a chamber for extinguishing the hot gases from the pyrolysis post-combustion.

  The wet solid residue (40 t / day) from the press filters 306a and 306b contains a large amount of noble metal. The residue is dried in a drying oven 308. The residue is powdery and black, and the glass fiber as the main component is decomposed by being stirred in the etching tank. Solid and liquid streams are periodically sampled and analyzed.

In the electrodeposition step, the flow from the rectifier flows in series from the electrolytic cell to the electrolytic cell, and flows in parallel to the electrodes of each cell. The current density is 50 to 400 A / m ² , preferably about 200 A / m ² , and the temperature of the electrolyte is 20 to 80 ° C., preferably 45 to 50 ° C. The iron ion concentration is kept as low as possible and in any case is a level of less than 10 g / L. When the total nickel concentration reaches 10-30 g / L level nickel, iron is precipitated, the precipitate is filtered, and a part of the electrolyte is purified.

The enriched electrolyte coming from the enriched electrolyte storage tank 312 is sent to the first row of 8 electrolytic cells. The electrolyzers are arranged in a cascade to allow the electrolyte solution to circulate. The pump delivers juice from the last cell to the first cell. The circulation flow rate is on the order of 15 m ³ . The electrolyte is consumed in 24 hours in the copper deposited on the cathode. When a surfactant is added, a finely controlled copper precipitate is obtained. The exhausted electrolyte is pumped toward the consumable electrolyte storage tank 318. The electrolytic cell is then refilled with the enriched electrolyte. Each row is emptied and filled with electrolyte every 4.5-5 hours.

Every 5 days, the electrolyte train is broken down. The recovered copper cathode (12t) is washed with water and the copper is separated from its stainless steel support with suitable machinery. The resulting copper is sampled and stored.

  It should be noted that it is preferable to periodically sample and analyze all solid and liquid streams.

  If the starting material contains a large amount of copper, a selective copper extraction step is important. Indeed, copper can form stable compounds that are insoluble in liquid lead, which compounds often contain noble metals. This is the reason why the maximum amount of copper must be removed before the start of the subsequent lead coating and purification step, otherwise a large amount of noble metal is lost in the stable compound.

  Furthermore, the selective copper extraction step makes it possible to selectively extract apparently all copper as a product that can be sold (pure copper cathode), which is remelted into an ingot.

  Metals (iron, aluminum, nickel) dissolved in the electrolytic solution are removed by a regular operation for regeneration of the electrolytic solution.

  It should be noted that the electrodeposition of copper may be replaced by an operation of crystallization of the commercially available copper sulfate.

  Depending on the type of waste, one or both of copper extraction by pyrolysis and selective dissolution can be omitted. This is an example where the waste consists of a catalyst muffler. In this case, the carbon chain and copper content are not the reason for the presence of these steps, and the crushed spent catalyst muffler is led directly to the lead coating step.

  The lead coating step involves contacting the pretreatment material (i.e. after grinding, selective pyrolysis, selective copper extraction) with the molten lead-based composition in the lead coated container 15. The molten lead-based composition contains lead as the main material and contains 0 to 50% tin, preferably less than 20% tin. This composition is liquid. It is used to collect and extract noble metals and dissolves in non-oxidized form. Lead in this composition and optionally tin that may be included is partly due to the added metal contained in the electronic card and the other due to the subsequently recovered metal.

  Dissolution is performed in the following manner. When stirring is started, a vortex of molten lead is generated in the kettle. A feeder 407 injects material collected with lead into the center of the vortex. This operation lasts about 15 minutes. The temperature is then brought to 350 to 550 ° C, preferably about 500 ° C.

A face is then subsequently started that separates the elements without an ablation phase or an affinity for lead. At this face, stirring is stopped and the precious metal and inert washed parts (ceramics, glass fibers, ferrite, etc.) rise to the surface and float. Next, the remover 405 is started and the suspended matter is recovered. This suspended material is removed from the lead bath and the operation is repeated. The stripping for a lead-tin alloy with 30 wt% tin is performed at a temperature of 250 to 450 ° C, for example about 270 ° C.

Suspended material is again processed in the same manner in an additional lead-clad container 18. Certainly, since a small amount of lead (and noble metal) is carried away with suspended solids during removal , it is useful to repeat the operation with a second kettle to avoid loss of the noble metal. Inert material collected by decontamination in additional lead-clad containers 18 is sent to the landfill as final waste after sampling and analysis as necessary. The molten lead-based composition contained in the additional lead-clad container 18 has a low concentration (less than 100 g per ton) of noble metal and is pumped back towards the lead-clad container 15.

  The lead coated face lasts for several days. Completion is considered when the precious metal content in the molten lead-based composition reaches a threshold, for example 2 to 4 kg per ton of lead.

  A selectable decoppering operation consisting of adding sulfur to the vortex of the lead-based composition is then performed to form a copper mat that is sent back to the selective dissolution containers 301a, 301b for copper extraction.

  Next, the molten lead-based composition having the dissolved noble metal is sent to a storage kettle where the composition is molded into an anode (which constitutes the anode molding means 25).

In the next Betz purification step, the precious metal contained in the anode thus formed is released. In this step, the Betz electrolysis unit 501 removes lead and tin from the anode by electrolysis in a fluorosilicate medium known as the Betz process. For example, an electrolytic solution containing about 90 g / L of lead and 80 g / L of free acid is supplied to the electrolytic cell. This electrolyte is prepared by stabilizing Resurge (PbO) in fluorosilicic acid in a Betz reactor 503. The electrolysis is performed at a current density of 350 A / m ² and an electrolyte temperature of 40 ° C., for example. During electrolysis, solid lead and tin dissolve in the electrolyte while lead and tin deposits are formed on the cathode. When a surfactant is added to the electrolytic solution, the precipitate can be made fine and smooth. The noble metal itself remains at the anode.

  In this configuration, the electrolyte does not concentrate impurities or very little. The entire purification may be performed once or twice a year. In this case, the electrolyte is sent to the level of the second tank 319 that stores the consumable electrolyte for lime treatment in the first stripping reactor 320 and a new electrolyte is prepared. In the Betz reactor 503, partial purification is required to reduce the lead content using sulfuric acid. The reactor 503 and the electrolytic cell are cleaned, and the gas effluent is sent to the washing tower 508. The washing juice is processed in the first stripping reactor 320 through the second tank 319 that stores the consumable electrolyte.

  In this example, each of the two electrolytic cells in two rows has 60 × 5 = 300 450 kg anodes. It takes 6 days to consume 80% of the anode, releasing its precious metal (432 kg) as anodic sludge, a dissolved anode residue. Depending on conditions, the anodic sludge falls as powder in the basket or adheres to the structure of the electrolytic cell. Preferably, the electrolysis is interrupted before the anode is completely dissolved. Thereby, the anodic sludge can be scraped off and recovered.

  The Pb / Sn cathode produced in 6 days is 108t.

  The two cathodes are preferably stripped every 3 days, and the two anodes are scraped simultaneously. The cathode produces lead-tin for ingots that can be recycled and sold to the kettle and / or supplied to the additional lead-coated container 18 along with the molten lead-based composition.

  The anodic sludge is washed, weighed and stored in a storage. The anodic sludge is preferably dissolved once or twice a week in an oxidation oven 520 at 1000 ° C. If this anodic sludge melting step is performed in the presence of oxygen gas (or air), it still allows oxidation of at least a portion of the lead and tin contained in the anodic sludge. Resurge (PbO) is formed on the surface, molded into a plate, and if necessary, doped with electrolyte with lead. Fume from the oven is directed towards the lead-coated filter. The liquid is cast into ingots (25 kg) and stored in batches in a storage. All ingots are sampled and weighed prior to marketing.

The method is designed to reduce the loss of precious metals as much as possible at all stages of the method.
That means
In the fines recovery line 122, fine fragments of the crushed waste that passes through the atmosphere during pulverization are reintroduced into the system.
-In the fines recovery line 215, the metal portion carried away with the carbonaceous gas during the thermal decomposition is recovered.
In the cleaned fines removal line 327, the part of the substance to be treated, carried away by electrolysis, can be reinjected into the main circuit.
-In addition to the lead-clad container 15, the use of an additional lead-clad container 18 can recover precious metals that have been inadvertently carried away by inert materials during the main lead-clad step.
-Further, due to the dissolution, the copper not extracted in the selective dissolution step is recovered as a copper mat in the lead-coated container 15 and reinjected into the main circuit.

  Therefore, according to the present method, 90 or 95% by weight, preferably 99% by weight or more, more preferably 99.0% by weight or more of the precious metal originally contained in the waste can be recovered in a fine state.

  Tables 1 and 2 below show an estimate of the chemical composition of the product between the different steps of the treatment method when the waste is a typical used electronic card.

101. Waste receiving means 102. Measuring means 103. Storage means 104. Dosing means
105, main conveyor 106, first secondary conveyor 107, second secondary conveyor 108, third secondary conveyor 109, coarse grinding mill 110, transfer line 111, fine grinding mill 112, collector conveyor 114, analysis means 115, first tertiary conveyor 116, storage 117, second tertiary conveyor 118, container 119, return conveyor 120, air contamination removal system 121, sleeve filter 122, fines recovery line 123, chimney 201, waste supply line
205a, 205b, main raw material supply means 202a, 202b, 202c, pyrolysis oven 203, calcined waste collection lines 204a, 204b, calcined waste storage 205a, 205b, main raw material supply pipes 206a, 206b, 206c, gas exhaust pipe 207a, 207b, 207c, post combustion chambers 208a, 208b, 208c, air introduction pipe 209, burned gas collection pipe 210, vertical cooling chamber 211, water coolant supply line 212, precooling gas recovery pipe 213, air introduction pipe 214, sleeve filter 215, fine matter recovery line 216, gas recovery pipe 217, chimney 301a, 301b, selective dissolution container 302, vat 303, consumable electrolyte supply line 304, oxygen supply section
305a, 305b, selective post lysate removal lines 306a, 306b, selective lysis container 307, solid collection system 308, drying oven 309, tube of pretreated material
310a, 310b Filtrate extraction pipe 311 Transfer line 312, Enriched electrolyte storage tank 313 Enriched electrolyte transfer pipe 314 Electrodeposition unit
315a, 315b, 315c, 315d, 315e, electrolytic tank 316, cathode stripping system
317. Consumable electrolyte recirculation line 318. First tank 319. Second tank 320. First stripping reactor 321. Lime supply line 323. First pulp take-out line 324. Additional press filter 325. Second stripping reactor 326, second pulp take-out line 327, fines take-out line
328 · Lime sulfate removal line 329 · Acid juice removal line
330 · Gas removal system 331 · Washing tower 332 · Acid juice extraction line 401 · Kettle 402 · Heating chamber 403 · Burner 404 · Stirrer 405 · Remover 406 · Enclosure cover 407 · Feeder 408 · Suction means
409 · Combustion gas discharge means 501 · Betz electrolysis units 502a and 502b · Betz electrolyzer row 503 · Betz reactor 504 · Fluorosilicate supply line
505 · Lead monoxide supply line
506 · Used Betz electrolyte collection line 507 · Electrolysis removal system 508 · Washing tower 509 · Washing juice collection line 510 · Cathode stripping means 511 · Cathode supply line 512 · Kettle 513 · Lead-tin supply line 514 · Anode stub collection means 516-Anode sludge collecting means
517 ・ Anode sludge treatment unit 518 ・ Cleaned sludge transfer line
519 ・ Air or oxygen intake line 520 ・ Oxidation oven 521 ・ Ingot collection line 522 ・ Fume collection line

Claims (25)

-Contacting the waste containing noble metal with the first molten lead-based composition (a),
-Removing the first mixture obtained and recovering the first mixture after removal containing the noble metal and suspended solids (b), and-removing the first mixture Recovering the noble metal by refining by electrolysis (c),
A waste treatment method comprising the following steps:
The debridement step (b),
-The step (b-1) of bringing the recovered suspended matter into contact with the second molten lead-based composition;
-Step (b-2) for removing and recovering the obtained second mixture, and-removing the obtained second mixture containing the noble metal from the first molten lead-based composition. Including at least a part (b-3) of supplying to the step (a),
It said first molten lead-based composition, at least the includes a second mixture after skimming, a main component of lead, comprises 0-50% tin and the low concentration of precious metals of less than per 100 g tonne ,
The second molten lead-based composition contains lead separated from the noble metal and / or fresh lead in the step (c), contains lead as a main component, and contains 0 to 50% tin. Waste disposal method.
Purifying the first mixture described above Jokasu (c) is,
-Forming an anode by molding the first mixture removed (c-1) ,
-Electrolyzing a fluorosilicic acid solution using the anode (c-2) ,
-Recovering anodic sludge containing precious metal (c-3)
The method according to claim 1, further comprising a. Before and after the step (c-3) recovering said anode sludges or simultaneously,
3. The method of claim 2 , wherein lead cathode deposits are recovered and supplied as at least part of the first and / or second molten lead-based composition. Before or after or simultaneously with the step (c-3) of collecting the anodic sludge,
3. The method of claim 2, wherein lead and tin cathode deposits are recovered to provide at least a portion of the first and / or second molten lead-based compositions. After sub-step of the anode sludge collected (c-3), the step of purifying the first mixture described above skimming (c) has the following substeps,
-Melting the recovered anodic sludge in the presence of oxygen (c-4) ,
A step of removing molten anodic sludge (c-5) , and a step of forming an ingot by molding molten and removed anodic sludge (c-6) ,
The method according to any one of claims 2-4 comprising a. The method according to any one of claims 1 to 5, wherein the first and second molten lead-based compositions contain less than 20% tin. Prior to step (a) to the waste is contacted with the first molten lead-based composition,
7. A method according to any one of claims 1 to 6, comprising extracting copper from the waste by selective dissolution. The copper extraction step comprises :
- sulfuric acid, in the presence of ferrous sulfate and oxygen, and selectively dissolving the waste,
Treating the resulting solution by filtration and / or electrolysis and / or precipitation;
-Recovering copper on the one hand and impurities of other metals on the other hand,
The method of claim 7 comprising substeps. Before the copper extraction step,
- by thermal decomposition the combustion of the waste, the method according to claim 7 or 8 comprising the answering step to produce a carbonaceous gas. The method according to claim 9, further comprising performing post-combustion of the carbonaceous gas. Furthermore, the method according to any one of claims 1 to 10 comprising a preliminary step of performing an analysis of grinding and / or ground waste of the waste. It said noble metal is gold, silver, platinum, palladium, rhodium, ruthenium, iridium, osmium, and methods according to any one of claims 1 to 11 comprising a metal selected from mixtures thereof. 13. A method according to any one of claims 1 to 12 , wherein the waste is selected from electronic waste such as catalytic exhaust mufflers and electronic cards. The method according to any one of claims 1 to 13, 90 wt% or more of the noble metals contained in the waste is recovered. The method according to any one of claims 1 to 14, wherein 99% by mass or more of the noble metal contained in the waste is recovered. The floating material, ceramics, method according to any one of claims 1 to 15 comprising glass fibers and / or ferrite. A facility for treating waste containing precious metals,
-At least one lead-coated container filled with a first molten lead-based composition, wherein the waste pre-treated material is brought into contact with the first molten lead-based composition to prepare a first mixture ( 15),
A line (24) connected to the inlet of the lead-coated container (15) for supplying the first molten lead-based composition;
-A line (14) connected to the inlet of the lead-clad container (15) for supplying the pretreated material,
-Removal means (16) in cooperation with the lead-coated container (15),
-A line (21) connected to the outlet of the lead-clad container (15) for taking out the first mixture removed;
-Means (36) connected to a line (21) for taking out the first mixture removed, and purifying the first mixture after the removal by electrolysis; and-purifying the removed first mixture. A noble metal removal line (38) connected to the outlet of the means (36)
further,
-A line (17) connected to the outlet of the removal means (16) for removing suspended matter generated by removal;
-On the one hand, connected to the line (17) for taking out the suspended solids, and on the other hand, connected to the line (31) for supplying the second molten lead-based composition, the suspended matter and the second molten lead-based composition At least one additional lead-clad container (18) to prepare a second mixture by contacting
-An additional removal means (19) associated with the additional lead-clad container (18); and-supply of the first molten lead-based composition connected to the outlet of the additional lead-clad container (18) A line (22) connected to the line (24) and for removing the second mixture after removal of the noble metal,
It said first molten lead-based composition, at least the includes a second mixture after skimming, a main component of lead, comprises 0-50% tin and the low concentration of precious metals of less than per 100 g tonne ,
Waste treatment in which the second molten lead-based composition contains lead and / or fresh lead separated from the noble metal by the refining means (36), contains lead as a main component, and contains 0 to 50% tin. Facility. It means for purifying the first mixture after the skimming by electrolysis (36)
-Anode molding means (25),
18. The waste treatment facility according to claim 17 , further comprising: a Betz electrolysis means (27) and an anodic sludge recovery means (28). It means for purifying the first mixture after the skimming by electrolysis (36)
19. The waste treatment facility according to claim 18 , comprising lead-tin recovery means (29) connected to the second molten lead-based composition supply line (31). The waste treatment facility according to any one of claims 17 to 19, wherein the first and second molten lead-based compositions contain less than 20% tin. Furthermore,
- Copper extraction means (37) while the outlet is connected to the pre-treatment supply line (14), and - the copper extraction means according with the connected to the inlet (37) The main raw material supply line (6) Item 20. The waste treatment facility according to any one of items 17 to 20 . Copper extraction means (37)
-At least one selective melting container (7) connected to the main raw material supply line (6);
A consumable electrolyte supply line (11) connected to the inlet of the selective dissolution container (7),
Electrolysis means (9),
-Enriched electrolyte transfer means (8) connecting the selective dissolution container (7) to the electrolysis means (9),
The waste treatment facility according to claim 21 , comprising: a cathode stripping means (13), and a consumable electrolyte circulation means (10) connected to an outlet of the electrolysis means (9). Furthermore,
- the main raw waste pyrolysis means connected to the inlet of the supply line (6) (2), and - pyrolysis unit (2) to comprise a connected waste feed line (1) according to claim 21 or The waste treatment facility described in 22 . Furthermore,
The waste treatment facility according to claim 23, comprising a gas discharge line (4) provided at an outlet of the pyrolysis means (2) and connected to the post-combustion means (5). Furthermore,
25. Disposal according to any one of claims 17 to 24 , further comprising grinding and analysis means (1ter) connected to the raw material waste supply line (1bis) and further connected to the waste supply line (1) Material processing equipment.

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