US20100230518A1 - System and process for battery recycling - Google Patents
System and process for battery recycling Download PDFInfo
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- US20100230518A1 US20100230518A1 US12/701,693 US70169310A US2010230518A1 US 20100230518 A1 US20100230518 A1 US 20100230518A1 US 70169310 A US70169310 A US 70169310A US 2010230518 A1 US2010230518 A1 US 2010230518A1
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- feedstock
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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
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M10/00—Secondary cells; Manufacture thereof
- H01M10/54—Reclaiming serviceable parts of waste accumulators
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M6/00—Primary cells; Manufacture thereof
- H01M6/52—Reclaiming serviceable parts of waste cells or batteries, e.g. recycling
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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
- B03B2009/066—General arrangement of separating plant, e.g. flow sheets specially adapted for refuse the refuse being batteries
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- 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/52—Mechanical processing of waste for the recovery of materials, e.g. crushing, shredding, separation or disassembly
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- 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/84—Recycling of batteries or fuel cells
Definitions
- the present invention relates to a system and process for recycling sealed cell batteries.
- a known method for recycling alkaline batteries involves mechanically removing the casing from the battery cell and then using chemical processes to separate the solid materials of the cell.
- Major solid components of the cells are carbon, zinc, potassium, and manganese.
- chemical separation processes There are several problems with chemical separation processes. Firstly, the component materials involved are of low value while chemical processing is expensive. Also, additional waste streams are created with the chemical processes. In view of these drawbacks, this recycling method has not found widespread use.
- This invention seeks to overcome drawbacks of known sealed cell battery recycling processes.
- the batteries are shredded to form a shredded feedstock.
- the shredded feedstock is heated above ambient temperature and rolled to form a dried material.
- the dried material is screen separating into a coarse fraction and a powder fraction and the powder fraction is output.
- a system for recycling sealed cell batteries comprises an oven with a first conveyor extending into the oven.
- a rotatable tunnel extends within the oven from an output of the first conveyor.
- the tunnel has a spiral vane depending from its inner surface which extends along a length of the tunnel.
- a second conveyor is positioned below an output of the rotatable tunnel.
- FIG. 1 is a schematic diagram of a system for battery recycling in accordance with this invention
- FIG. 2 is a partially cut-away perspective view of a portion of the system of FIG. 1 ,
- FIG. 3 is a schematic diagram of another system for battery recycling in accordance with this invention.
- FIG. 4 is a schematic diagram of a portion of another system for battery recycling in accordance with this invention.
- a battery is a series of battery cells.
- a 9 V battery is a true battery
- AAA through D size batteries are cells.
- the term battery is used to mean either true batteries or cells.
- the central core of an alkaline cylindrical button cell is the anode which is a dispersion of zinc oxide powder in a gel containing a potassium hydroxide electrolyte.
- This core is surrounded by a separator which is a non-woven layer of cellulose (paper) or a synthetic polymer (plastic).
- a separator which is a non-woven layer of cellulose (paper) or a synthetic polymer (plastic).
- an annular cathode which is a compressed paste of manganese dioxide with carbon (graphite) powder to increase conductivity.
- the anode, separator, and cathode are sealed in a drawn steel casing.
- a system 10 for recycling sealed cell alkaline batteries has a pre-shredder 12 for pre-shredding the feedstock in order to rupture their sealed steel casings.
- the batteries may be further shredded in secondary shredder 14 , which may be a granulator, and are then conveyed downstream by conveyor 16 .
- the conveyor which may be a chain conveyor or a belt conveyor with flights, assists in breaking up the feedstock into a more uniform material feed stream.
- oven conveyor 20 has an input belt conveyor 22 with an overlying blade 24 .
- the input belt conveyor dispenses to an upstream screw tunnel 26 .
- the upstream screw tunnel has a spiral vane depending from its inner surface that extends along the length of the tunnel.
- the upstream screw tunnel 26 in turn dispenses to a middle belt conveyor 28 with an overlying blade 30 .
- the middle belt conveyor dispenses to a downstream screw tunnel 32 having a similar configuration as the upstream screw tunnel.
- the downstream screw tunnel dispenses to an output belt conveyor 34 .
- the output belt conveyor has an overlying blade 36 .
- An oven 40 surrounds all but the upstream end of the input belt conveyor and downstream end of the output belt conveyor.
- Feedstock traveling on the input belt conveyor 22 is levelled by blade 34 .
- the material then drops into upstream screw tunnel 26 .
- This screw tunnel rotates to roll the feedstock and feed it downstream.
- the feedstock drops to the middle belt conveyor 28 where it is levelled—by blade 30 —and conveyed into downstream screw tunnel 32 .
- the downstream screw tunnel rotates to roll the feedstock and convey it to output belt conveyor 34 , where the feedstock is levelled by blade 36 and then dispensed from the oven conveyor.
- the feedstock By conveying and rolling the feedstock at elevated temperatures in the oven conveyor, the feedstock is dried and evaporation of mercury in the feedstock is promoted.
- each of the air uptakes feed to a cyclone 46 , with air uptakes 13 and 15 feeding to the cyclone through a particulate filter 37 .
- a vacuum source 44 draws air through the cyclone 46 to a scrubber 48 before the air leaves the system 10 .
- the cyclone swirls the moving air to drop out any powder or other solids entrained by the moving air.
- the scrubber sequesters vapours in the moving air which, with the alkaline battery feedstock, will be mercury vapours.
- the scrubber may be a venturi scrubber with a pH control system that ensures the solubility of vapours.
- a venturi scrubber With a venturi scrubber, the scrubber itself acts as the vacuum source.
- Filter 37 traps any paper and light plastics drawn off by air intakes 13 and 15 so that the scrubber is not obstructed by this material and so that any fire that develops in the scrubber is not fed by this paper and plastics.
- mercury has a boiling point of about 357° C., it is nevertheless volatile even at room temperature and therefore off gases at the various air uptakes as well as off gassing strongly in the oven conveyor.
- Feedstock leaving the oven conveyor passes to a sieve 50 which may be a shaker table with a mesh size #30. This separates a coarser fraction of the feedstock from a finer fraction.
- the mesh size is such that the finer fraction which drops through the sieve is a zinc oxide, manganese dioxide, and potassium hydroxide powder. This powder is recovered as a finished product of the process.
- the coarser fraction which comprise the shredded steel casing along with brass, cellulose (paper), graphite (carbon), and plastic, collectively known as fluff, pass to a magnetic separator 52 , which may be a magnetic wheel.
- the separated steel (magnetic component) is immersed in a first water bath 54 .
- Water from the bath 54 drains through a wash screen 56 . Any remaining powder will pass through the screen and therefore remain in the water. Larger solids, namely the separated steel, are blocked by the screen and are washed off the screen to recover the steel as a second finished product of the process.
- the water which passes through the screen 56 passes on to filter press 60 .
- the fluff (non-magnetic component) which is separated by the magnetic separator is immersed in a second water bath 62 .
- Water from the bath 62 drains through a wash screen 64 . Any remaining powder in the water will pass through the screen with the water. Larger solids, namely the fluff, are blocked by the screen and are washed off the screen.
- This fluff passes to a tumbler dryer 66 where it is dried and then to a specific gravity separator 68 .
- the specific gravity separator separates the ferrous component of the fluff (graphite and brass) from the nonferrous component (paper and plastic). These two output streams are finished products of the process.
- the water which passes through screen 64 passes on to filter press 60 .
- the water passing to the filter press from screens 56 and 64 passes through the membranes of the filter press such that any powder which had been in the water is recovered as a wet powder.
- This wet powder is fed back to the conveyor 16 in the system 10 .
- the water, which at this stage is normally caustic, then passes to a holding tank (not shown) wherein its pH is adjusted so that it may be reused in the water baths.
- the recovered powder of zinc oxide, manganese dioxide, and potassium hydroxide may be used in fertilizer provided its mercury content has been sufficiently reduced.
- a powder with a mercury content of less than 75 ppm is suitable for use in fertilizer.
- mercury concentrations down to undetectable levels may be achieved.
- the recovered steel may be used in the steel industry.
- the recovered paper and plastic from the fluff may be burned for energy (e.g., in oven 40 ).
- alkaline batteries may also be used for any of zinc carbon, zinc chloride, and manganese batteries.
- the composition of the recovered powder will vary somewhat depending upon the type of battery which forms the feedstock. However, for all of these types of battery, the recovered powder may be used in fertilizer.
- the time during which the feedstock remains in the oven conveyor and the temperature of this conveyor are determined based on characteristics of the feedstock and desired properties of the powder output from the system. More specifically, a customer of the powder may specify a required dryness and mercury content for the powder. Characteristics of the feedstock which impact the required heating time and temperature are the size of the battery cells, the age of the cells (newer batteries need to be run slower at higher temperatures), mercury content, and the type of battery. Regardless of customer requirements, the feedstock must at least be sufficiently dry so that it separates at the screen separator 50 .
- the temperature of the oven can be varied as required, typically, a temperature of between 300° F. and 800° F. is sufficient where the feedstock remains in the oven conveyor for 1 to 5 minutes.
- the speed through the oven conveyor may be 26 ft/min and the temperature may be set at 800° F.
- the mesh size of the screen separator can be varied as required provided it is sufficiently small to separate the powder fraction of the feedstock. However, a #30 mesh size is suitable where the powder is to be used in the fertilizer industry and also allows the powder to pelletize well.
- System 100 for use with a feedstock of nickel metal hydride batteries is identical to system 10 of FIG. 1 , and like parts have been given like reference numerals, except as follows.
- System 100 includes a tumbler dryer 76 at the output of the first wash screen 56 which feeds to a specific gravity separator 78 .
- the anode is nickel oxyhydroxide and the cathode is most commonly a lanthanoid mixture with nickel, cobalt, manganese, and/or aluminum.
- Some cathodes may include other metals, such as iron or chromium.
- the electrolyte is most commonly potassium hydroxide.
- the processing of nickel metal hydride batteries in system 100 proceeds identically to the processing of alkaline batteries in system 10 of FIG. 1 except as follows.
- Vapours generated from drying the feedstock are water and volatile organic compounds (VOCs).
- the speed of the oven conveyor is adjusted so that the feedstock dries sufficiently through the oven conveyor at the chosen oven temperature.
- the scrubber (which may be a venturi scrubber as used in the system 10 of FIG. 1 ) sequesters the vapours from the drying process.
- the powder component which passes through the sieve comprises nickel oxyhydroxide powder, cobalt oxide, and lanthanoids.
- sieve 50 may have a #30 mesh size.
- the recovered powder may be used in the coatings industry for pigmentation or the powder may be used in the stainless steel industry.
- the solid component which does not pass through the sieve, contains nickel plated steel and fluff.
- the nickel plated steel forms the magnetic component which is separated from the fluff by the magnetic wheel 52 .
- the nickel plated steel of this magnetic component typically encapsulates some of the fluff as a consequence of the upstream shredding process. This encapsulated fluff remains with the magnetic component leaving the magnetic wheel.
- the magnetic component is directed through bath 54 to the first wash screen 56 .
- the solid component leaving the wash screen passes to tumbler dryer 76 where it is dried.
- the dried solid component then inputs specific gravity separator 78 to separate nonferrous fluff residues from the nickel plated steel.
- the nickel plated steel is a finished product that may be used in the steel industry.
- System 100 may be modified to operate with a feedstock of lithium button cells, namely lithium ion batteries —which are rechargeable—or lithium polymer batteries.
- the anode is a lithium metal or lithium compound.
- the cathode is, most commonly, manganese dioxide and the electrolyte is, most commonly, lithium perchlorate in propylene carbonate and dimethoxyethane.
- FIG. 4 illustrates a portion of a system 1000 for use with lithium button cells.
- System 1000 is identical to system 100 of FIG. 2 except as follows.
- the scrubber 48 outputs to a water atomizer 84 and the atomizer outputs to a tank 86 . These modifications are employed because of the highly combustible nature of lithium compounds and the VOCs in the batteries.
- the powder which drops out is mostly lithium cobalt oxide (but can vary depending on the chemical composition of the lithium ion battery).
- This powder can be used in the coatings industry.
- a mesh size #30 is suitable to limit contamination of this powder.
- the magnetic component separated by the magnetic wheel includes stainless steel and magnetic alloys as well as any copper that is trapped by the stainless steel and magnetic alloys.
- the specific gravity separator 78 FIG. 3 ) separates out non-ferrous fluff encapsulated with this magnetic component and also separates the stainless steel, magnetic alloys, and copper from each other.
- the oven conveyor is run at a low speed and high temperature (to promote evaporation of mercury), with system 1000 run with lithium batteries, the oven conveyor is run at a mid speed and temperature (to avoid combustion), and when the system 100 is run with nickel metal hydride batteries, the oven conveyor is run at high speeds and temperatures.
- blowers could be used for this purpose.
- filter 37 may be omitted when running system 10 .
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Abstract
In a method of recycling sealed batteries, the batteries are shredded to form a shredded feedstock. The shredded feedstock is heated above ambient temperature and rolled to form a dried material. The dried material is screen separating into a coarse fraction and a powder fraction and the powder fraction is output. A system for recycling sealed cell batteries comprises an oven with a first conveyor extending into the oven. A rotatable tunnel extends within the oven from an output of the first conveyor. The tunnel has a spiral vane depending from its inner surface which extends along a length of the tunnel. A second conveyor is positioned below an output of the rotatable tunnel.
Description
- This application claims priority from U.S. Provisional Application No. 61/160,058 filed on Mar. 13, 2009.
- The present invention relates to a system and process for recycling sealed cell batteries.
- Ninety-five percent of portable batteries are household batteries. The vast majority of these are sealed cell alkaline batteries. Once spent, most of these batteries are simply discarded and find their way to landfill sites.
- A known method for recycling alkaline batteries involves mechanically removing the casing from the battery cell and then using chemical processes to separate the solid materials of the cell. Major solid components of the cells are carbon, zinc, potassium, and manganese. There are several problems with chemical separation processes. Firstly, the component materials involved are of low value while chemical processing is expensive. Also, additional waste streams are created with the chemical processes. In view of these drawbacks, this recycling method has not found widespread use.
- This invention seeks to overcome drawbacks of known sealed cell battery recycling processes.
- In a method of recycling sealed batteries, the batteries are shredded to form a shredded feedstock. The shredded feedstock is heated above ambient temperature and rolled to form a dried material. The dried material is screen separating into a coarse fraction and a powder fraction and the powder fraction is output.
- A system for recycling sealed cell batteries comprises an oven with a first conveyor extending into the oven. A rotatable tunnel extends within the oven from an output of the first conveyor. The tunnel has a spiral vane depending from its inner surface which extends along a length of the tunnel. A second conveyor is positioned below an output of the rotatable tunnel.
- Other features and advantages will be apparent from the following description in conjunction with the drawings.
- In the figures which illustrate an example embodiment of the invention,
-
FIG. 1 is a schematic diagram of a system for battery recycling in accordance with this invention, -
FIG. 2 is a partially cut-away perspective view of a portion of the system ofFIG. 1 , -
FIG. 3 is a schematic diagram of another system for battery recycling in accordance with this invention, and -
FIG. 4 is a schematic diagram of a portion of another system for battery recycling in accordance with this invention. - Technically, a battery is a series of battery cells. Thus, a 9 V battery is a true battery, whereas AAA through D size batteries are cells. In this specification, the term battery is used to mean either true batteries or cells.
- The central core of an alkaline cylindrical button cell is the anode which is a dispersion of zinc oxide powder in a gel containing a potassium hydroxide electrolyte. This core is surrounded by a separator which is a non-woven layer of cellulose (paper) or a synthetic polymer (plastic). Surrounding the separator is an annular cathode which is a compressed paste of manganese dioxide with carbon (graphite) powder to increase conductivity. The anode, separator, and cathode are sealed in a drawn steel casing. Although some alkaline batteries are mercury-free, many spent alkaline batteries contain mercury, with an average overall concentration of 100 ppm.
- Turning to
FIG. 1 , asystem 10 for recycling sealed cell alkaline batteries has a pre-shredder 12 for pre-shredding the feedstock in order to rupture their sealed steel casings. Next the batteries may be further shredded insecondary shredder 14, which may be a granulator, and are then conveyed downstream byconveyor 16. The conveyor, which may be a chain conveyor or a belt conveyor with flights, assists in breaking up the feedstock into a more uniform material feed stream. - From the
conveyor 16, the feedstock passes to anoven conveyor 20. Theoven conveyor 20 is detailed inFIG. 2 . Turning toFIG. 2 ,oven conveyor 20 has aninput belt conveyor 22 with anoverlying blade 24. The input belt conveyor dispenses to anupstream screw tunnel 26. The upstream screw tunnel has a spiral vane depending from its inner surface that extends along the length of the tunnel. Theupstream screw tunnel 26 in turn dispenses to amiddle belt conveyor 28 with anoverlying blade 30. The middle belt conveyor dispenses to adownstream screw tunnel 32 having a similar configuration as the upstream screw tunnel. The downstream screw tunnel dispenses to anoutput belt conveyor 34. The output belt conveyor has anoverlying blade 36. Anoven 40 surrounds all but the upstream end of the input belt conveyor and downstream end of the output belt conveyor. - Feedstock traveling on the
input belt conveyor 22 is levelled byblade 34. The material then drops intoupstream screw tunnel 26. This screw tunnel rotates to roll the feedstock and feed it downstream. At the downstream end of the upstream screw tunnel, the feedstock drops to themiddle belt conveyor 28 where it is levelled—byblade 30—and conveyed intodownstream screw tunnel 32. The downstream screw tunnel rotates to roll the feedstock and convey it to outputbelt conveyor 34, where the feedstock is levelled byblade 36 and then dispensed from the oven conveyor. - By conveying and rolling the feedstock at elevated temperatures in the oven conveyor, the feedstock is dried and evaporation of mercury in the feedstock is promoted.
- Returning to
FIG. 1 , there areair uptakes shredder 14,oven 20 and asieve 50, respectively. Each of the air uptakes feed to acyclone 46, withair uptakes particulate filter 37. Avacuum source 44 draws air through thecyclone 46 to ascrubber 48 before the air leaves thesystem 10. The cyclone swirls the moving air to drop out any powder or other solids entrained by the moving air. The scrubber sequesters vapours in the moving air which, with the alkaline battery feedstock, will be mercury vapours. The scrubber may be a venturi scrubber with a pH control system that ensures the solubility of vapours. With a venturi scrubber, the scrubber itself acts as the vacuum source. Filter 37 traps any paper and light plastics drawn off byair intakes - While mercury has a boiling point of about 357° C., it is nevertheless volatile even at room temperature and therefore off gases at the various air uptakes as well as off gassing strongly in the oven conveyor.
- Feedstock leaving the oven conveyor passes to a
sieve 50 which may be a shaker table with amesh size # 30. This separates a coarser fraction of the feedstock from a finer fraction. The mesh size is such that the finer fraction which drops through the sieve is a zinc oxide, manganese dioxide, and potassium hydroxide powder. This powder is recovered as a finished product of the process. - The coarser fraction, which comprise the shredded steel casing along with brass, cellulose (paper), graphite (carbon), and plastic, collectively known as fluff, pass to a
magnetic separator 52, which may be a magnetic wheel. - The separated steel (magnetic component) is immersed in a
first water bath 54. Water from thebath 54 drains through awash screen 56. Any remaining powder will pass through the screen and therefore remain in the water. Larger solids, namely the separated steel, are blocked by the screen and are washed off the screen to recover the steel as a second finished product of the process. - The water which passes through the
screen 56 passes on tofilter press 60. - The fluff (non-magnetic component) which is separated by the magnetic separator is immersed in a
second water bath 62. Water from thebath 62 drains through awash screen 64. Any remaining powder in the water will pass through the screen with the water. Larger solids, namely the fluff, are blocked by the screen and are washed off the screen. This fluff passes to atumbler dryer 66 where it is dried and then to aspecific gravity separator 68. The specific gravity separator separates the ferrous component of the fluff (graphite and brass) from the nonferrous component (paper and plastic). These two output streams are finished products of the process. - The water which passes through
screen 64 passes on tofilter press 60. - The water passing to the filter press from
screens conveyor 16 in thesystem 10. The water, which at this stage is normally caustic, then passes to a holding tank (not shown) wherein its pH is adjusted so that it may be reused in the water baths. - The recovered powder of zinc oxide, manganese dioxide, and potassium hydroxide may be used in fertilizer provided its mercury content has been sufficiently reduced. In this regard, typically, a powder with a mercury content of less than 75 ppm is suitable for use in fertilizer. With the subject system, mercury concentrations down to undetectable levels may be achieved.
- The recovered steel may be used in the steel industry. The recovered paper and plastic from the fluff may be burned for energy (e.g., in oven 40).
- The same process described for alkaline batteries may also be used for any of zinc carbon, zinc chloride, and manganese batteries. The composition of the recovered powder will vary somewhat depending upon the type of battery which forms the feedstock. However, for all of these types of battery, the recovered powder may be used in fertilizer.
- The time during which the feedstock remains in the oven conveyor and the temperature of this conveyor are determined based on characteristics of the feedstock and desired properties of the powder output from the system. More specifically, a customer of the powder may specify a required dryness and mercury content for the powder. Characteristics of the feedstock which impact the required heating time and temperature are the size of the battery cells, the age of the cells (newer batteries need to be run slower at higher temperatures), mercury content, and the type of battery. Regardless of customer requirements, the feedstock must at least be sufficiently dry so that it separates at the
screen separator 50. - While the temperature of the oven can be varied as required, typically, a temperature of between 300° F. and 800° F. is sufficient where the feedstock remains in the oven conveyor for 1 to 5 minutes.
- For example, for a mixed feedstock of alkaline, zinc carbon, zinc chloride, and manganese batteries and a 26 ft long oven conveyor, the speed through the oven conveyor may be 26 ft/min and the temperature may be set at 800° F.
- The mesh size of the screen separator can be varied as required provided it is sufficiently small to separate the powder fraction of the feedstock. However, a #30 mesh size is suitable where the powder is to be used in the fertilizer industry and also allows the powder to pelletize well.
- The described system may be modified for use with nickel metal hydride sealed cell batteries. More specifically, turning to
FIG. 3 ,system 100 for use with a feedstock of nickel metal hydride batteries is identical tosystem 10 ofFIG. 1 , and like parts have been given like reference numerals, except as follows.System 100 includes atumbler dryer 76 at the output of thefirst wash screen 56 which feeds to aspecific gravity separator 78. - With nickel metal hydride batteries, the anode is nickel oxyhydroxide and the cathode is most commonly a lanthanoid mixture with nickel, cobalt, manganese, and/or aluminum. Some cathodes may include other metals, such as iron or chromium. The electrolyte is most commonly potassium hydroxide.
- The processing of nickel metal hydride batteries in
system 100 proceeds identically to the processing of alkaline batteries insystem 10 ofFIG. 1 except as follows. Vapours generated from drying the feedstock are water and volatile organic compounds (VOCs). The speed of the oven conveyor is adjusted so that the feedstock dries sufficiently through the oven conveyor at the chosen oven temperature. The scrubber (which may be a venturi scrubber as used in thesystem 10 ofFIG. 1 ) sequesters the vapours from the drying process. - When the feedstock leaves the oven conveyor and reaches the sieve, the powder component which passes through the sieve comprises nickel oxyhydroxide powder, cobalt oxide, and lanthanoids. As when operating with alkaline batteries, sieve 50 may have a #30 mesh size. The recovered powder may be used in the coatings industry for pigmentation or the powder may be used in the stainless steel industry.
- The solid component, which does not pass through the sieve, contains nickel plated steel and fluff. The nickel plated steel forms the magnetic component which is separated from the fluff by the
magnetic wheel 52. However, the nickel plated steel of this magnetic component typically encapsulates some of the fluff as a consequence of the upstream shredding process. This encapsulated fluff remains with the magnetic component leaving the magnetic wheel. The magnetic component is directed throughbath 54 to thefirst wash screen 56. The solid component leaving the wash screen passes totumbler dryer 76 where it is dried. The dried solid component then inputsspecific gravity separator 78 to separate nonferrous fluff residues from the nickel plated steel. The nickel plated steel is a finished product that may be used in the steel industry. -
System 100 may be modified to operate with a feedstock of lithium button cells, namely lithium ion batteries —which are rechargeable—or lithium polymer batteries. With a lithium battery, the anode is a lithium metal or lithium compound. The cathode is, most commonly, manganese dioxide and the electrolyte is, most commonly, lithium perchlorate in propylene carbonate and dimethoxyethane. -
FIG. 4 illustrates a portion of asystem 1000 for use with lithium button cells.System 1000 is identical tosystem 100 ofFIG. 2 except as follows. Thescrubber 48 outputs to awater atomizer 84 and the atomizer outputs to atank 86. These modifications are employed because of the highly combustible nature of lithium compounds and the VOCs in the batteries. - In this modified system, when the lithium ion batteries are shredded and conveyed by the conveyor, lithium compounds, which gas off at any of the air pick up points pass to the scrubber where they are sequestered. Any lithium compounds or VOCs which escape the scrubber are condensed by the atomized water from the
atomizer 84 and the condensed lithium compounds and VOCs pass to thewater tank 86. The pH of the water in the atomizer and the tank is controlled with, for example, the addition of sodium hydroxide to a concentration of 50%, to ensure the gas remains condensed in the water. Any paper drawn off is trapped byfilter 37 before it reaches the scrubber so that it will not obstruct the scrubber. Because of the risk of combustion with lithium ion battery feedstock, the temperature in the oven conveyor is maintained below the combustion temperature of paper (454° F.). - With lithium button cells, at the sieve, the powder which drops out is mostly lithium cobalt oxide (but can vary depending on the chemical composition of the lithium ion battery). This powder can be used in the coatings industry. As before, a
mesh size # 30 is suitable to limit contamination of this powder. - The magnetic component separated by the magnetic wheel includes stainless steel and magnetic alloys as well as any copper that is trapped by the stainless steel and magnetic alloys. The specific gravity separator 78 (
FIG. 3 ) separates out non-ferrous fluff encapsulated with this magnetic component and also separates the stainless steel, magnetic alloys, and copper from each other. - In general, with
system 10 run with alkaline batteries, the oven conveyor is run at a low speed and high temperature (to promote evaporation of mercury), withsystem 1000 run with lithium batteries, the oven conveyor is run at a mid speed and temperature (to avoid combustion), and when thesystem 100 is run with nickel metal hydride batteries, the oven conveyor is run at high speeds and temperatures. - While three different systems have been described, they may be combined in a single system and components of that system switched in or out, or on or off, as appropriate, to adapt the system to the different kinds of feedstock.
- Rather than providing a vacuum source to draw vapours into the scrubber, blowers could be used for this purpose.
- There is a minimal amount of paper and light plastics released with the shredding of alkaline batteries. Accordingly, optionally, filter 37 may be omitted when running
system 10. - Other modifications will be apparent to those skilled in the art and, therefore, the invention is defined in the claims.
Claims (20)
1. A method of recycling sealed batteries, comprising:
shredding said batteries to form a shredded feedstock;
heating said shredded feedstock above ambient temperature while rolling said shredded feedstock to form a dried material;
screen separating said dried material into a coarse fraction and a powder fraction; and
outputting said powder fraction.
2. The method of claim 1 wherein said batteries are alkaline batteries containing mercury, said heating comprises heating said shredded feedstock above ambient temperature and below the boiling point of mercury, said heating while rolling evaporates a portion of said mercury from said feedstock, and wherein said powder fraction comprises zinc oxide, manganese dioxide, and potassium hydroxide.
3. The method of claim 2 further comprising drawing air through said shredded material during said heating and rolling to draw off mercury vapour from said shredded feedstock.
4. The method of claim 3 further comprising sequestering said mercury in a scrubber.
5. The method of any one of claim 1 to claim 4 further comprising swirling said air drawn from said shredded material to drop out any particulates from said air and returning said particulates to said shredded material.
6. The method of any one of claim 1 to claim 5 further comprising magnetically separating said coarse fraction into a magnetic component and a non-magnetic component.
7. The method of claim 6 further comprising immersing said magnetic component in a first water bath and passing water from said first water bath through a screen to separate magnetic solids, and outputting said magnetic solids.
8. The method of claim 7 further comprising separating said magnetic solids based on their specific gravity prior to said outputting said magnetic solids and wherein said outputting said magnetic solids comprises outputting separated constituents of said magnetic solids.
9. The method of claim 7 or claim 8 further comprising immersing said non-magnetic component in a second water bath and passing water from said second water bath through a screen to separate fluff, and outputting said fluff.
10. The method of claim 9 further comprising separating said fluff based on specific gravity of constituents of said fluff prior to said outputting said fluff and wherein said outputting said fluff comprises outputting separated constituents of said fluff.
11. The method of claim 9 or claim 10 further comprising using at least a portion of said fluff as a combustible in said heating step.
12. The method of any one of claim 9 to claim 11 further comprising combining water from said first water bath and said second water bath as a water component and filtering said water component to recover a powder component.
13. The method of claim 12 further comprising adding said powder component to said shredded material.
14. A method of recycling sealed batteries containing mercury, comprising:
shredding said batteries to form a shredded feedstock;
heating said shredded feedstock above ambient temperature and below the boiling point of mercury while rolling said shredded feedstock to evaporate a portion of said mercury from said feedstock to form a mercury reduced dried material;
screen separating said dried material into a coarse fraction and a powder fraction; and
outputting said powder fraction.
15. A system for recycling sealed cell batteries, comprising:
an oven;
a first conveyor extending into said oven;
a rotatable tunnel with a spiral vane depending from an inner surface of said tunnel extending along a length of said tunnel, said rotatable tunnel disposed within said oven and extending from an output of said first conveyor;
a second conveyor below an output of said rotatable tunnel.
16. The system of claim 15 further comprising a sieve downstream of an output of said second conveyor.
17. The system of claim 15 or claim 16 further comprising a shredder upstream of an input of said first conveyor.
18. The system of any one of claim 15 to claim 17 further comprising a leveller associated with said first conveyor.
19. The system of any one of claim 15 to claim 18 further comprising a cyclone and a scrubber above said oven, and means for moving air upwardly through said oven, said cyclone and said scrubber.
20. The system of claim 19 further comprising at least one particulate filter between said oven and said scrubber.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
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US12/701,693 US20100230518A1 (en) | 2009-03-13 | 2010-02-08 | System and process for battery recycling |
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US16005809P | 2009-03-13 | 2009-03-13 | |
US12/701,693 US20100230518A1 (en) | 2009-03-13 | 2010-02-08 | System and process for battery recycling |
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US20100230518A1 true US20100230518A1 (en) | 2010-09-16 |
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US12/923,957 Active US8210456B2 (en) | 2009-03-13 | 2010-10-18 | Battery recycling |
US13/473,682 Abandoned US20120227589A1 (en) | 2009-03-13 | 2012-05-17 | Battery recycling |
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US12/923,957 Active US8210456B2 (en) | 2009-03-13 | 2010-10-18 | Battery recycling |
US13/473,682 Abandoned US20120227589A1 (en) | 2009-03-13 | 2012-05-17 | Battery recycling |
Country Status (4)
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US (3) | US20100230518A1 (en) |
EP (1) | EP2406843B1 (en) |
CA (2) | CA2778136C (en) |
WO (1) | WO2010102377A1 (en) |
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Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
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Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
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Family Cites Families (24)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US1587623A (en) * | 1925-03-02 | 1926-06-08 | Max E Zuckerman | Process of reclaiming the constituents of lead battery plates |
US3456886A (en) * | 1964-11-19 | 1969-07-22 | Tonolli & C Spa A | Process for the separation of the active material from the remaining material constituting storage batteries |
US3614003A (en) * | 1964-11-19 | 1971-10-19 | Tonolli & C Spa A | Apparatus for selectively crushing of storage batteries and separating the component materials |
DE1224935B (en) * | 1964-12-09 | 1966-09-15 | Stolberger Zink Ag | Process and system for the processing of lead-containing batteries |
LU50208A1 (en) * | 1965-01-15 | 1966-03-07 | ||
US3393876A (en) * | 1966-11-21 | 1968-07-23 | Bunker Hill Company | Recovery of lead from waste storage batteries |
DE2104130C3 (en) * | 1971-01-29 | 1975-07-03 | Kloeckner-Humboldt-Deutz Ag, 5000 Koeln | Process for processing accumulator scrap |
US3892563A (en) * | 1973-05-14 | 1975-07-01 | Point Albert E | Method and apparatus for separating the constituents of lead-acid storage batteries |
DE3022665A1 (en) * | 1980-06-18 | 1982-01-21 | Hazemag Dr. E. Andreas GmbH & Co, 4400 Münster | METHOD FOR RECOVERY OF LEAD AND LEAD CONNECTIONS FROM LEAD ACCUMULATORS TO BE SCRAPPED |
US4612711A (en) * | 1983-06-30 | 1986-09-23 | Phillips Petroleum Company | Apparatus and method for drying particulate material |
DE3614242A1 (en) * | 1986-04-26 | 1987-10-29 | Metallgesellschaft Ag | METHOD FOR WORKING OUT SMALL BATTERIES |
DE3709967A1 (en) * | 1987-03-26 | 1988-10-06 | Metallgesellschaft Ag | METHOD FOR RECOVERING SMALL BATTERIES |
DE4020227A1 (en) * | 1990-06-26 | 1992-01-02 | Celi Antonio Maria Dipl Ing | METHOD AND DEVICE FOR PROCESSING USED DEVICE BATTERIES |
DE4224884A1 (en) * | 1992-07-28 | 1994-02-03 | Batenus Gmbh & Co Kg | Process for the recovery of raw materials from pre-sorted, used goods, in particular from used electrochemical batteries and accumulators |
CH684225A5 (en) * | 1992-09-02 | 1994-07-29 | Inter Recycling Ag | A process for disposing of nickel-cadmium or nickel-hydride cells. |
US5707015A (en) * | 1994-02-09 | 1998-01-13 | Guthrie; Rhett Bob | Process for recovery of the constituent materials from lead acid batteries |
US5632863A (en) * | 1994-11-22 | 1997-05-27 | Meador; W. R. | Battery pyrolysis process |
US6686086B1 (en) * | 2000-06-30 | 2004-02-03 | Secor International Inc. | Battery reclamation system |
CA2391865C (en) * | 2000-09-13 | 2011-04-19 | Francois Cardarelli | A method for recycling spent lithium metal polymer rechargeable batteries and related materials |
US6833100B2 (en) * | 2001-06-01 | 2004-12-21 | Liberty Engineering Company | Mogul machine for manufacturing starch molded products such as candy and apparatus and starch level adjuster and method for reducing starch loss in same |
EP1333522A1 (en) * | 2002-02-01 | 2003-08-06 | Batrec Industrie AG | Method of and apparatus for storage and handling of objects comprising alkali metals, such as alkali metal containing batteries |
KR100898076B1 (en) * | 2007-08-29 | 2009-05-18 | 주식회사 반디신소재 | Recycling apparatus for used Zinc-Carbon and Alkaline batteries and method thereof |
US8034150B2 (en) * | 2007-10-12 | 2011-10-11 | Metal Conversion Technologies, Llc | Process and system for material reclamation and recycling |
US8475564B2 (en) * | 2009-02-10 | 2013-07-02 | Peter Valente | Biomass dryer/burner system |
-
2009
- 2009-11-03 CA CA2778136A patent/CA2778136C/en active Active
- 2009-11-03 EP EP09841288.5A patent/EP2406843B1/en not_active Not-in-force
- 2009-11-03 CA CA2730320A patent/CA2730320C/en active Active
- 2009-11-03 WO PCT/CA2009/001583 patent/WO2010102377A1/en active Application Filing
-
2010
- 2010-02-08 US US12/701,693 patent/US20100230518A1/en not_active Abandoned
- 2010-10-18 US US12/923,957 patent/US8210456B2/en active Active
-
2012
- 2012-05-17 US US13/473,682 patent/US20120227589A1/en not_active Abandoned
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Also Published As
Publication number | Publication date |
---|---|
CA2730320C (en) | 2012-09-11 |
EP2406843A4 (en) | 2013-05-29 |
US20120227589A1 (en) | 2012-09-13 |
EP2406843B1 (en) | 2015-08-19 |
CA2730320A1 (en) | 2010-09-16 |
US20110031336A1 (en) | 2011-02-10 |
CA2778136C (en) | 2013-04-09 |
EP2406843A1 (en) | 2012-01-18 |
WO2010102377A1 (en) | 2010-09-16 |
CA2778136A1 (en) | 2010-09-16 |
US8210456B2 (en) | 2012-07-03 |
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