• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    For the recycling of electrical batteries, in particular of a mixture of high-power batteries for equipment of any chemical composition, and also of assembled printed circuit boards and electronic components, a pyrolysis of the unsorted mixture is carried out at a temperature between 450 DEG and 650 DEG , then an electrolysis of the pyrolysis slag is carried out and subsequently a separation of the electrolysis products and removal of the products accumulating at the electrodes is carried out. In this process, which is economically profitable, no environment-polluting residues are produced and an initial sorting of material becomes unnecessary.
    公开号:SU1621818A3
    申请号:SU874203888
    申请日:1987-12-11
    公开日:1991-01-15
    发明作者:Ханулик Йозеф
    申请人:Реситек С.А. (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to electrical engineering and relates to chemical current sources and printed circuit boards.
    The purpose of the invention is to increase efficiency and reduce environmental pollution.
    FIG. 1 shows a flow chart of the pyrolysis and subsequent processing of the gaseous products formed; in fig. 2 - electrolysis scheme.
    The method is carried out as follows.
    The pyrolysis of the starting material 1 is carried out in a sealed furnace 2, inside which a reduced pressure of 20-50 mm Hg is created. and which is provided with lining 3. Between the outer
    The side of the walls of the furnace 2 and the lining 3 creates a jacket of protective gas located at atmospheric pressure. The gaseous reaction products 4 formed during pyrolysis are passed through a cooler 5, in which condensate and metal vapors 6 are separated and taken off. The gaseous components are then sent to a scrubber 7, in which they are washed with a countercurrent 5-10% hydrogen boron, This HBT 4 8 and as a refrigerant is returned to the refrigerator 5. The washing acid used in the scrubber 7 is either returned to the process again or, if it is depleted and contains significant amounts of hydrogen boron as well as hydrofluoric acid. Isd
    00
    00

    CM
    All metal fluorine borates are used to treat pyrolysis slag.
    The gas stream 9 leaving the cooling unit of the refrigerator 5 is sucked in by the fan 10 through the cyclone 11, passed under pressure through the dust removal filter 12 and sent to the combustion unit 13, where air 14 is also fed and from which the resulting flue gases are discharged through the chimney 15.
    Before being supplied to the combustion unit 13, a portion of the gas stream may (Branded off and, as a reducing protective gas 16, be fed into the jacket of the pyrolysis furnace 2. In order to eliminate the danger of an explosion in the hot pyrolysis furnace, it may be necessary to add to this flow of shielding gas of a certain amount - flue gases 17.
    The dust 18 from the dust removal filter 12 together with the slag 14 from the pyrolysis furnace 2 is fed to the second stage, electrolysis. In this case, it may be advisable to pre-dilute the pyrolysis spar with washing with acid 8 - BUTTERFLUOROFLUORIC ACID
    that The suspension resulting from this is filtered and the filtrate is directed to the crystallization of the salts contained in it, and the residue on the filter to electrolysis.
    In this case, electrolysis can be carried out by two different methods, namely, at high temperature, when the pyrolysis package melts and the resulting melt plays the role of an electrolyte, or at low temperature, when the pyrolysis slag is dissolved in the electrolyte. Both methods allow the separation of slag into the main metals contained in it and isolate them. Thus, this stage is economically feasible since it produces a relatively large amount of rare and expensive metals.
    It is most preferable to conduct electrolysis at low temperatures using hydrofluoric acid as the electrolyte, since almost all metals and their compounds are dissolved in hydrofluoric acid.
    To conduct electrolysis, pyrrhizal slag 19 is fed to electrolyzer 20, which can be completely


    l
    P
    five
    five
    five
    sealed and with the help of a partition 21, for example a diaphragm, divided into anode and cathode space. The hydrogen boron hydrofluoric acid electrolyte 22 solution, preferably a 50% aqueous solution, supplied to the electrolyzer 20.
    Pyrolysis slag 15 is loaded into a plastic cylinder 23, the lower part of which, immersed in an electrolyte, is made of polymer-coated mesh 24. Pyrolysis slag 19 in the form of unground batteries is pressed downward by a metal or graphite plate 25 under pressure. Plate 25 is the anode. It does not touch the electrolyte solution 22, hydrofluoric acid, and therefore has a long service life.
    Under the anode there is an anode space 26 bounded by a plastic casing, which collects anode anodes 27. This sludge consists mainly of solid waste, such as powdered graphite, manganese dioxide, porcelain, glass, and, in addition, small amounts of mercury droplets and sintered oxides The processes occurring at the anode can be represented by the following equation:
    Me -ne V: ten,
    which is valid for all metals used in the manufacture of batteries. As a result, hydrofluoric acid salts are formed which, with few exceptions, are soluble. Thus, batteries are electrolytically decomposed and passed into solution. This also releases oxygen, which is desirable for the decomposition of graphite. The collected anode slurry may then be recycled for reuse in the manufacture of batteries.
    The cathode is made in the form of a sheet of tin 28, for example iron. The following metals are deposited on the cathode: Fe, Ni, Zn, Cd, Ag, Cu, Hg, Co, Pb and Au. Less noble metals, Thai as A1, K, Li, Na and t „d. it does not precipitate. More noble metals 29 are deposited in metallic form on the cathode sheet 28 or in the form of cathode sludge 30, which is collected in the cathode space 31 located in the cathode, made in the form of a plastic receiving bath. These metals are separated by metallurgical or electrochemical method and then returned for reuse.
    Since hydrogen and small amounts of chlorine are released at the cathode, it is advisable to blow fresh air into the electrolysis unit 32 on one side of the electrolyzer and to produce suction from the opposite side in order to prevent the formation of detonating gas. The suction mixture of gases and vapors to separate the aerosols and the solids entrained by it is passed through filter 33 and then cleaned in scrubber 34. It is advisable to carry out the washing with the washing liquid that was used to treat the pyrolysis slag 19 before electrolysis. Thus, chlorides are removed from the process.
    In addition, small amounts of by-products 35, such as colloidal mercury and possible products, are collected on the bottom of the cell 20.
    Over time, electrolyte n drops other impurities, such as various fluoroborates and trace elements; In this case, the electrolyte can be purified from them by distillation, which, to prevent thermal
    hydrolysis of, for example, HgO, forming hydrofluoric acid kisses from unstable compounds of the Hg () a type.
    The electrolyte can be continuously pumped through the pump through the filter device 36.
    Electrolytic decomposition can be accelerated by the use of agitators and ultrasonic probes.
    The voltage applied by the electrolyzer can be very small. In test setups, a voltage of about + 6V was used. In practice, however, it is possible to work with even less stress. The operating current density may be 20-50 A / dm2.
    lots held in a vacuum. Collecting in the distillation process in the lower part of the distillation apparatus, metal fluorine borates may be pyrolyzed at a temperature of the order of. This produces the corresponding fluorides and, in addition, gaseous boron fluoride is released, which is soluble in water and can again be converted to hydrofluoric acid by the addition of hydrofluoric acid to the electrolysis process.
    40
    45
    Pyrolysis products from the bottom of the distillation apparatus and metal fluorides can also be separated by fractional crystallization and returned for reuse.
    In order to isolate I g of metal at the cathode, it is necessary to pass about 1-1.5 ampere hours through it. This means a consumption of 0.2-0.3 farad of electricity per 1 kg of metal.
     Due to the internal resistance, the electrolyte is heated to the desired operating temperature of 40-80 ° C. At this temperature, the graphite is oxidized at the anode in hydrofluoric acid and pulverized.
    Using hydrofluoric acid as electrolyte

    ten
    218186
    Depending on the nature of the metal, it can absorb 200-400 g of metal per liter.
    In order to increase the profitability of the process, it is possible to regenerate using hydrofluoric acid as the electrolyte. Such a regeneration at the first stage is already carried out in the electrolyzer itself due to the deposition of metals whose ions are in solution. As a result, the balance in acid. the lot is not broken.
    Metals that, due to their electrochemical properties, do not precipitate in an acidic medium (such metals include, for example, aluminum, potassium, lithium and nltrium), can be separated after the start of crystallization due to the high concentration of fluoroborates by precipitating sodium, potassium and lithium on the amalgam cathode. The metals deposited on the amalgam cathode can be easily separated.
    Over time, electrolyte n drops other impurities, such as various fluoroborates and trace elements; In this case, the electrolyte can be purified from them by distillation, which, to prevent thermal
    15
    20
    25
    Hydrofluoric acid hydrofluoric acid 30 decomposition is carried out in vacuo. During the distillation process in the lower part of the distillation apparatus, the metal fluoroborates may be pyrolyzed at a temperature of the order of. This produces the corresponding fluorides and, in addition, gaseous boron fluoride is released, which is soluble in water and can again be converted to hydrofluoric acid by the addition of hydrofluoric acid to the electrolysis process.
    Pyrolysis products from the bottom of the distillation apparatus and metal fluorides can also be separated by fractional crystallization and returned for reuse.
    Example 1. A mixture of small-sized batteries was taken to test the method, the ton of which contained approximately the following quantities of substances, kg: manganese dioxide 270; iron 210; zinc 160; coal 60; ammonium chloride 35; nickel 20; copper 20; potassium hydroxide 10; mercury 3; cadmium. 0, 5; silver. 0.3.
    A mixture of used batteries is fed to the oven. Pyrolysis is carried out at a temperature of 3.5 hours in a closed air environment. The resulting water vapor displaces the oxygen of the air and forms an inert atmosphere. Thereafter, gases such as CO, Ny, STZ, and COg are formed (with a composition of 30-50% water vapor%, CO and CH4, and 10-30% COa acting as a reducing agent). The process takes place at a reduced pressure of 30 mm Hg. At the same time, water constantly drops in drops to replenish water vapor and g, preventing the formation of an explosive mixture. The vapor and gas stream is directed through the chiller where it separates and removes condensates and metal vapors. The gaseous constituents are fed to the wash column, where they are washed in a pgotchtok flow with an aqueous solution of borofluoric acid, and then as
    ten
    55
    20
    hollows (0.01 wt.%), manganese (0.05 wt.%) and copper (0.07 wt.%).
    After the batteries are completely dissolved, the composition of the products is as follows: zinc 1.8 May. %; iron 16.5 wt%; cadmium 8.3 may. %; Nickel 25.8 May. %; Chrome 2.4 May. %; manganese 0.3 May. %; copper 44.9 may. %
    Waste is collected under the anode — powdered graphite, manganese dioxide, porcelain, glass, oxides, as well as a small amount of mercury,
    The composition of the anode products following, wt.%: Manganese dioxide 95; silver 1-2; mercury 0.5; graphite 3,
    The duration of the process of dissolution and electrolysis is about 15 hours at the current ZOOOOA.
    Precipitated metals are transferred for reuse in the metallurgical industry. Manganese dioxide is reused for battery production. Regenerated at
    The cooler is nipraal back in cold-electrolysis with hydrofluoric acid again for the next batches of products.
    Dilc, then arokuskayut through cyclonic separates and dust filter and burn in air; / xs "
    During pyrolysis, mercury is produced, which enters the atmosphere after it. thirty
    The pyrolysis slag is rummed with dilute borfluoroethiotic acid; poluchen: n / l the suspension is filtered, the filtrate is fed into a septic tank, where manganese dioxide sludge is collected as a product. Alkali metal-containing water is used for the subsequent cleaning.
    The precipitate from the fi lt T tion is placed in
    35
    Example 3. Under the conditions of the example, pyrolysis is carried out for 5 hours, the process of dissolution and electrolysis is carried out at 50 ° C for 20 hours at a current of 20,000A.
    The proposed method provides the extraction of all components, while
    50% rustor bo Rigorist gadfly a similar 40 - no residues, contaminants
    acids and electrolysis. At the same time, the partly spontaneously -mch & C dissolves first, and y e npff room temperature
    environment that must be disposed of and removed. The chemicals required to carry out the process can be regenerated and reused.
    hollows (0.01 wt.%), manganese (0.05 wt.%) and copper (0.07 wt.%).
    After the batteries are completely dissolved, the composition of the products is as follows: zinc 1.8 May. %; iron 16.5 wt%; cadmium 8.3 may. %; Nickel 25.8 May. %; Chrome 2.4 May. %; manganese 0.3 May. %; copper 44.9 may. %
    Waste is collected under the anode — powdered graphite, manganese dioxide, porcelain, glass, oxides, as well as a small amount of mercury,
    The composition of the anode products following, wt.%: Manganese dioxide 95; silver 1-2; mercury 0.5; graphite 3,
    The duration of the process of dissolution and electrolysis is about 15 hours at the current ZOOOOA.
    Precipitated metals are transferred for reuse in the metallurgical industry. Manganese dioxide is reused for battery production. Regenerated at
    electrolysis hydrofluoric acid
    The lot is reused for the next batch of products.
    Example 2. Under the conditions of example 1, pyrolysis was carried out at 650 ° C, and electrolysis at 80 ° C. The pyrolysis time was 2.5 hours, the dissolution and electrolysis process was 10 hours at a current of 40000 A.
    Example 3. Under the conditions of Example 1, pyrolysis is carried out for 5 hours, the dissolution and electrolysis process is carried out at 50 ° C for 20 hours at a current of 20,000A.
    The proposed method provides the extraction of all components, while
    environment that must be disposed of and removed. The chemicals required to carry out the process can be regenerated and reused.
    Afterwards, at the temperature of 60 ° C at a current density of 0.05 A / cm2 and at the right of 6 V, the rest of the metals are transformed into ra. First on the cathode
    However, the proposed method is not only clean from an ecological point of view, since in its implementation there is no need
    EHHR, t Hydrogen hydrophosphate is precipitated in the removal of polluting
    n loui-ta regenarized. Following zinc, in accordance with the electrochemistry of a number of voltages, other metals are precipitated
    product environment, but also economically justified, since the initial materials used in its implementation, namely, spent batteries, old elements of electronic circuits and defective printed circuit boards with radio components, are free, and valuable metals containing relatively large quantities
    flps-f c-ohm after partial dilution of e-ng-iji white: w. zinc (51 MLS.%), iron (1.5 wt.%), cad-C5S7 wt.%, nickel (1 wt.%),
     is used in closed-loop
    However, the proposed method is not only clean from an ecological point of view, since in its implementation there is no need
    five
    product environment, but also economically justified, since the raw materials used in its implementation, namely, spent batteries, old electronic circuit elements and defective printed circuit boards with radio components, are free, and valuable metals contained in relatively large quantities
    recovered with little energy, and since it produces intermediates that can again be used in industry. The proposed method is very economical from an energy point of view, since at all stages a high concentration of metals is maintained and no dilution occurs, which would lead to a significant increase in entropy.
    Due to the fact that the implementation of the proposed method provides the possibility of complete decomposition of the processed materials and extraction of all the main components, waste that was previously considered more or less of low value becomes a valuable source of raw materials.
    Thus, the invention makes it possible to create and maintain a closed cycle of basic or raw materials, in which it is only necessary to compensate for the small and inevitable losses due to the techniques used.
    权利要求:
    Claims (7)
    [1]
    1. The method of utilization of electric batteries, printed circuit boards with radio components and electronic circuit elements by pyrolysis of the unassembled mixture without air access at 450-650 ° C, treatment of pyrolysis slags with acid, filtration of the suspension, electrolysis, extraction and separation of metals deposited on the electrodes, This is due to the fact that, in order to increase efficiency and reduce environmental pollution, hydrogen peroxide acid is used as an acid for slag treatment, which is also used as an electrolyte for electrolysis at 50-80 ° C
    Q
    j 0
    five
    0
    $$ y 15-
    and regenerated by distillation.
    [2]
    2. A method according to claim 2, in which the gaseous pyrolysis products are passed through a cooler, then a 5-10% aqueous solution of boron hydrofluoric hydrofluoric acid is rinsed in countercurrent, passed through a cyclone and a dust removal filter, and burned in air.
    [3]
    3. Method according to paragraphs. 1 and 2, that the metals that are formed during electrolysis at the cathode section are separated by metallurgical, electrochemical or chemical ny-v and sent for reuse, and the slime formed at the anode section is reused manufacture of electric batteries.
    [4]
    4. Method according to paragraphs. 1 and 3, characterized in that the anodic sludge formed during electrolysis is treated with hydrofluoric acid to be separated from traces of metal, and the insoluble residue is filtered off and reused for the production of electric batteries.
    [5]
    5. Method pop. 1-3, characterized in that the electrolyte is regenerated by crystallization and separation of the substances dissolved therein.
    [6]
    6. The method according to claim 1, characterized in that the hydrofluoric acid products formed during the distillation are subjected to pyrolysis to convert them into fluorides, which are sent for reuse.
    [7]
    7. A method according to claim 1, characterized in that non-precious metals dissolved in the electrolyte during electrolysis are continuously or periodically deposited on the mercury cathode in the form of amalgams.
    22
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    ZA879342B|1989-04-26|
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    DK406688A|1988-09-01|
    DK406688D0|1988-07-20|
    EP0274059B1|1992-02-05|
    EP0274059A2|1988-07-13|
    AU1042088A|1988-06-30|
    CS274297B2|1991-04-11|
    YU224187A|1989-02-28|
    PT86348B|1993-08-31|
    PL150019B1|1990-04-30|
    FI883698A|1988-08-09|
    PT86348A|1989-01-17|
    BR8707567A|1989-02-21|
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    WO1988004476A1|1988-06-16|
    OA08900A|1989-10-31|
    IN172198B|1993-05-01|
    NO171289B|1992-11-09|
    IL84741A|1991-08-16|
    CS908487A2|1990-08-14|
    IE873364L|1988-06-12|
    FI883698A0|1988-08-09|
    NO171289C|1993-02-17|
    AT72501T|1992-02-15|
    JPS63197592A|1988-08-16|
    AU597464B2|1990-05-31|
    FI92444B|1994-07-29|
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    US4874486A|1989-10-17|
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    IE59264B1|1994-01-26|
    DD264716A5|1989-02-08|
    NO883619L|1988-08-12|
    IL84741D0|1988-05-31|
    MX168761B|1993-06-07|
    NO883619D0|1988-08-12|
    GR3004483T3|1993-03-31|
    PL269370A1|1988-08-18|
    TR23132A|1989-04-10|
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    KR880008470A|1988-08-31|
    HU202017B|1991-01-28|
    BG60505B1|1995-06-30|
    EP0274059A3|1988-07-27|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    CH496086|1986-12-12|
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