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US20010006606A1 - Aluminium base alloy of scrap metal and casting alloy produced from this - Google Patents

Aluminium base alloy of scrap metal and casting alloy produced from this Download PDF

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Publication number
US20010006606A1
US20010006606A1 US09/741,469 US74146900A US2001006606A1 US 20010006606 A1 US20010006606 A1 US 20010006606A1 US 74146900 A US74146900 A US 74146900A US 2001006606 A1 US2001006606 A1 US 2001006606A1
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US
United States
Prior art keywords
aluminium base
aluminium
casting
pyrolysis
production
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Abandoned
Application number
US09/741,469
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English (en)
Inventor
Hubert Koch
Horst Schramm
Peter Krug
Gerhard Ost
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Aluminium Rheinfelden GmbH
Original Assignee
Aluminium Rheinfelden GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Aluminium Rheinfelden GmbH filed Critical Aluminium Rheinfelden GmbH
Assigned to ALUMINIUM RHEINFELDEN GMBH reassignment ALUMINIUM RHEINFELDEN GMBH ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: KOCH, HUBERT, KRUG, PETER, OST, GERHARD, SCHRAMM, HORST
Publication of US20010006606A1 publication Critical patent/US20010006606A1/en
Priority to US10/375,596 priority Critical patent/US20030129077A1/en
Abandoned legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B21/00—Obtaining aluminium
    • C22B21/0084—Obtaining aluminium melting and handling molten aluminium
    • C22B21/0092—Remelting scrap, skimmings or any secondary source aluminium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B21—MECHANICAL METAL-WORKING WITHOUT ESSENTIALLY REMOVING MATERIAL; PUNCHING METAL
    • B21J—FORGING; HAMMERING; PRESSING METAL; RIVETING; FORGE FURNACES
    • B21J5/00—Methods for forging, hammering, or pressing; Special equipment or accessories therefor
    • B21J5/004—Thixotropic process, i.e. forging at semi-solid state
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B21/00—Obtaining aluminium
    • C22B21/0038—Obtaining aluminium by other processes
    • C22B21/0069—Obtaining aluminium by other processes from scrap, skimmings or any secondary source aluminium, e.g. recovery of alloy constituents
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22C—ALLOYS
    • C22C21/00—Alloys based on aluminium
    • C22C21/06—Alloys based on aluminium with magnesium as the next major constituent
    • C22C21/08—Alloys based on aluminium with magnesium as the next major constituent with silicon
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • the invention concerns an aluminium base alloy for production of casting alloys with magnesium as the most essential alloy element.
  • the scope of the invention also includes a process for production of the aluminium base alloy, casting alloys produced from the aluminium base alloy and a process for their production.
  • DE-C-1483229 discloses AlMgSi alloys made from secondary aluminium alloys or secondary metals for production of cylinder heads.
  • EP-A-0779371 and EP-A-0780481 disclose a process for preparation of aluminium-containing waste for recovery of aluminium from this waste.
  • the essential core of this known process is the recovery of aluminium from materials contaminated with organic components, in particular from foodstuff and animal feed packing, in the form of printed and/or painted aluminium waste or aluminium/plastic compound material waste.
  • the invention is based on the task of preparing a low cost aluminium base alloy for production of casting alloys.
  • Casting alloys made from the aluminium base alloy are suitable amongst others for production of heat-resistant and/or corrosion-resistant parts in engine areas.
  • the task according to the invention is solved by an aluminium base alloy which contains at least 50% scrap metal on a primary aluminium base and as the remainder primary aluminium and/or scrap metal on a secondary aluminium base of known composition.
  • the aluminium base alloy can be “diluted” with primary aluminium.
  • the scrap composition for production of an aluminium base alloy with a low content of undesirable accompanying elements is preselected accordingly before production of the scrap metal.
  • the aluminium base alloy can in principle contain, as well as the scrap metal on a primary aluminium base, also a certain proportion of scrap metal on a secondary aluminium base, but in this case the composition of the scrap metal should be known so that the quantity of undesirable accompanying elements introduced into the aluminium base alloy is not too great.
  • the proportion of primary alloys is at least 80% and ideally 100% of the scrap metal used.
  • Suitable scrap metal on a primary aluminium base is mainly recycling metal obtained from foodstuff and animal feed packaging.
  • magnesium can also be added up to a total content of 3.0 to 5.0 w. % and silicon up to a total content of 1.5 to 3.0 w. %.
  • Further additional alloy elements are 0.5 to 1.2 w. % manganese and/or 0.5 to 1.2 w. % copper and max 0.2 w. % titanium, max 0.4 w. % cobalt, max 0.4 w. % cerium and max 1.2 w. % zirconium.
  • the casting alloys produced from primary aluminium alloys according to the invention achieve a higher elongation, which can be up to 6%, in relation to the casting alloys produced from secondary aluminium alloys according to the state of the art.
  • a process particularly suited for production of the aluminium base alloy according to the invention is characterised in that materials on a primary aluminium base contaminated with organic compounds are prepared separately according to their thermal value and their aluminium content, combined in measured quantities to achieve a nominal value, the organic compounds carbonised by pyrolysis with formation of pyrolysis gas and pyrolysis coke, the pyrolysis coke separated off, the materials pretreated in this way are where applicable bright annealed, and where applicable sorted to separate out foil constituents, and then melted.
  • aluminium compound substances are suitably reduced to a unit size and after pyrolysis at least the iron parts are separated out.
  • the separately prepared materials are combined to set the nominal value by way of a computer-controlled metering system, where in addition to the thermal value and the aluminium content of the materials, further parameters of the materials prepared can be taken into account, in particular their moisture, apparent density and grain size.
  • the composition of the aluminium base alloy can be set within certain limits i.e. the process allows in a simple manner the production of different aluminium base alloys for different applications.
  • Tables 1 to 3 show as examples three mixtures of different scrap metals. The typical compositions of the individual scrap metals relate to 100% aluminium alloy. The tables also contain typical further compositions of aluminium base alloys produced from the three scrap mixtures.
  • DSD material is combined packaging material provided by the system Duales System GmbH
  • IGORA material is combined packing material produced by the Swiss collection point IGORA
  • composition of the aluminium base alloy cannot be determined theoretically from the compositions of the individual scrap metals of a mixture because packaging waste in particular contains a lot of plastic and adhering foreign substances such as foodstuff residue, and therefore the aluminium proportion in this scrap material is considerably less than with practically pure metal scrap such as for example cans or bottle tops.
  • the scab-reducing addition of beryllium can take place in substantially lower quantities than without the addition of vanadium.
  • a content of more than 3.5 w. % magnesium it is sufficient to add 10 to 50 ppm beryllium, preferably 10 to 35 ppm beryllium. If the content of magnesium in the melt is less than 3.5 w. %, less than 25 ppm beryllium is required to achieve a high scabbing resistance. For lower requirements for the scabbing tendency, the beryllium addition can even be omitted.
  • the preferred area of application of the casting alloys produced from the aluminium base alloy according to the invention is the production of heat-resistant and/or corrosion-resistant parts in the engine area, in particular engine blocks, cylinder heads and oil sumps, by means of sand casting, chilled casting, diecasting, thixocasting or thixoforging.
  • FIG. 1 a diagram of the main structure of a recycling plant
  • FIG. 2 a basic flow diagram of the plant in FIG. 1;
  • FIG. 3 a block circuit diagram of the plant in FIG. 1;
  • FIG. 4 a process flow diagram of the plant in FIG. 1;
  • FIGS. 5 - 7 enlarged sections of FIG. 3.
  • a plant for recovery of aluminium from aluminium scrap contaminated with organic compounds according to FIGS. 1 to 7 has the three operating units:
  • the material preparation BE 1 includes the material delivery, storage until charging and mechanical preparation and retention (buffering) of prepared material for the decoating plant BE 2 .
  • Materials to be processed in the plant are usually delivered by road or rail.
  • the incoming materials are weighed.
  • the nature, provenance and quantity of the materials supplied are recorded and documented.
  • a reception test may be performed depending on the material type.
  • the material preparation BE 1 in principle serves for preparation of two fundamentally different material types:
  • Aluminium compound substances S 2 are reduced to a unit size, for example 30 ⁇ 40 mm, and the ferrous metals removed.
  • Materials used here are therefore e.g. DSD (Duales System GmbH) material, painted plates and metal goods, painted extrusion profiles, painted tubes and aerosol cans, flexible packs of aluminium combined with plastic or paper, used aluminium cans, cooling radiator scrap, pipes, fins, cuttings, offset panels, cables stripped with grease, bottle caps, number plates, road signs and window profiles.
  • Aluminium compound substances S 2 are intermediate-stored in the case of immediately processing in a preparation room before coarse size reduction.
  • the aluminium compound substances S 2 for coarse size reduction are supplied by way of a delivery conveyor 10 and a subsequent further delivery conveyor 14 into a slow-running cutter 16 .
  • the first delivery conveyor 10 is supplied by way of a delivery shaft 12 by means of a forklift truck 18 . It is also possible to supply the cutter 16 directly using the forklift truck 18 .
  • the coarsely reduced material falls from the rotor shears 16 onto a belt conveyor 20 which also has a delivery well 22 for optimum delivery of batch material.
  • a magnetic separator 24 Arranged above the belt conveyor 20 is a magnetic separator 24 with separating aid. At this point the coarse iron constituents S 3 are removed from the material flow.
  • the belt conveyor 20 is fitted with an integral strong field magnetic roller or magnetic drum 26 .
  • iron constituents S 3 including stainless steel are removed.
  • the iron constituents S 3 can be separated first after pyrolysis.
  • the preferred aluminium compound substances S 2 are transferred by a steep belt conveyor 28 and distribution conveyor 30 into one of for example five buffer containers 32 a - e each with a capacity of for example 40 m 3 .
  • the buffer containers 32 are designed closed i.e. with encapsulated input and output and venting to an extraction system.
  • the material stored is output as required by way of metering conveyors 34 a - e onto a belt conveyor 36 ; this passes the material to the distribution conveyor 38 for the decoating plant BE 2 .
  • the aluminium compound substances S 2 prepared after separation of the iron constituents S 3 to the steep belt conveyor 28 can for example be divided further in a cross-flow separator 29 according to the aluminium content or thermal value H u .
  • the various fractions with different aluminium content or different thermal value H u are then intermediate-stored separately in the buffer containers 32 .
  • Aluminium chips S 1 are taken by wheel loader from chip boxes in the supplier room and deposited by way of a delivery shaft 40 into a delivery conveyor 42 to a sieve 44 .
  • the sieve 44 separates the coarse and fine chippings.
  • the fine chippings travel by way of a belt conveyor 46 and a subsequent further belt conveyor 48 , with an overhead magnetic separator 50 to separate the iron constituents S 3 , into a buffer container 52 with for example a capacity of 20 m 3 .
  • the material flow can pass through a metal detector 31 for detection and subsequent separation of undesirable non-ferrous metals.
  • the material flow can pass through metal detector 31 for detection and subsequent separation of undesirable non-ferrous metals.
  • the fine chippings are passed from the buffer container 52 by way of a metering conveyor 56 onto the belt conveyor 58 and thus reach the preparation line of the aluminium compound substances on the distribution conveyor 38 for the decoating system BE 2 .
  • the material from the compound and chip lines first reaches a buffer container or material store 60 in which the material is moistened where applicable. From here it reaches the input system of a pyrolysis drum 70 .
  • a pyrolysis delivery head can spray water, water vapour and/or an inert gas, e.g. CO 2 .
  • extraction air is collected in order to prevent a diffuse release of emissions of foreign particles such as dust.
  • the individual extraction air flows are combined and passed by way of a cyclone separator 62 and subsequent fan 64 to a combustion chamber 78 for afterburning. Solids separated out in the cyclone separator 64 are discharged into a container 68 by way of a cellular wheel sluice 66 and for example charged into the delivery well 22 .
  • the decoating plant BE 2 consists of the pyrolysis drum, a bright annealing machine, a foil separator, a pyrolysis gas combustion and a flue gas cleaning system with quench, heat exchanger, two-stage washer etc.
  • the material is supplied from the material preparation BE 1 by way of the material delivery 60 and a sluice system consisting of two sealed pushers 72 , 74 to the pyrolysis drum 70 , which has a length L of approximately 25 m.
  • a reduced pressure is applied to the sluice system.
  • inert gas e.g. CO 2 is flushed into this room and the gas between the two pushers 72 , 74 is simultaneously extracted by means of a fan 76 and passed to the heating jacket exhaust gas S 8 from the combustion chamber 78 .
  • the sealed pushers 72 , 74 are designed to be tightly closed.
  • the material is added to the pyrolysis drum 70 in cycles by way of this pusher system. To avoid undesirable air ingress into the drum, in each case only one of the two pushers can be opened, which is guaranteed by means of an end position monitoring.
  • a further seal is applied by way of the material presentation by way of the first double pusher 72 , between the two sealed pushers 72 , 74 , and in an inlet screw 80 which can be liquid-cooled.
  • the pyrolysis process takes place at around 550° C. Because of the conditions of temperature and holding time conditions, it is guaranteed that on reaching the pyrolysis discharge head after around 50 minutes, the material is completely pyrolysed. Extensive degasification of the materials takes place in the pyrolysis drum 70 .
  • the energy required for the pyrolysis process is supplied by way of a heating jacket 82 surrounding the pyrolysis drum 70 .
  • the heating jacket 82 is refractory-lined and designed without burners; the necessary hot gas S 8 is supplied from outside the combustion chamber 70 to the heating jacket 82 and there evenly distributed along the pyrolysis drum wall. After flowing through the heating jacket 82 , the hot gas S 8 , cooled to around 580° C. is guided by means of the fan in the heating jacket 84 of the pyrolysis gas lines 86 and then returned to the combustion chamber 78 . It is returned to the combustion chamber 78 with a view to a closed circuit design and consequent emission reduction.
  • the heating jacket 82 consists of a boiler plate construction with refractory lining. To avoid the emission of hot gas between the heating jacket 82 and the rotary passage through the pyrolysis drum 70 , cable seals are installed. Sealing occurs by mutually overlapping casting segments which are pressed against the rotating sealing surface of the rotary furnace by means of a surrounding cable over locking clamping pins. Because of the pressure conditions in the heating jacket 82 , i.e. the slight pressure reduction, the fan arrangement on the suction side also prevents, by design, the emission of hot gas to the environment.
  • the pyrolysis drum 70 is driven on the output side by way of a crown gear by means of a hydraulic drive, the drum also has an auxiliary drive.
  • the drum rotation speed is for example 5 rotations per minute and can be varied.
  • the pyrolysis drum 70 is sealed on the input and output sides by means of a rotating mechanical seal and CO 2 barrier gas supply.
  • the pyrolysis gas and the solids are separated at the pyrolysis discharge head.
  • the pyrolysis gas is extracted under pressure control.
  • the pressure control and subsequent pyrolysis gas line 86 are designed redundant for operating security.
  • the pyrolysis drum 70 projects with its end part 71 by a dimension a into an outlet housing 88 .
  • This end part 71 is designed as a sieve for separating the solids discharged from the pyrolysis drum 70 into a sieved fine fraction and a coarse fraction emerging from the open end part 71 .
  • the position of the sieve 90 which is designed as an adjustable flap, can be used to set the fraction size of discharge material allocated to the two sluice systems.
  • the pyrolysis coke R 1 is cooled in a water-cooled cooling screw 96 with double casing and indirect cooling. From the screw the cooled coke falls into a cellular wheel sluice 98 ; this discharges into a transport container 100 . The heat is dissipated through a cooling water circuit to which the quench water circuit is also connected, by way of a total of three cooling towers 102 a - c.
  • composition of the pyrolysis coke allows a quantitative use in the production of carbon products e.g. anodes for aluminium electrolysis.
  • the sealed pushers 104 , 106 are in each case designed to be tightly sealed.
  • the material is output in cycles by way of these pushers.
  • To avoid undesirable air ingress into the pyrolysis drum 70 in each case only one of the two pushers can be opened, which is guaranteed by means of an end position monitoring.
  • the material is discharged from the sluice system onto a sieve 108 on which the free pyrolysis coke R 1 remaining in material flow is discharged separately as sieve passage (fine goods) from the aluminium fraction by way of a cellular wheel sluice 110 into the cooling screw 96 ; as described above this empties by way of a cellular wheel sluice 98 into the transport container 100 .
  • the pyrolysis coke can for example be used in production of carbon anodes for electrolysis for aluminium production.
  • the hot aluminium main flow containing the pyrolysis coke R 1 is supplied by way of a hot goods conveyor 112 and a cellular wheel sluice 114 to a bright annealing device 116 .
  • this bright annealing device 116 the pyrolysis coke residue is burnt in a targeted fashion on an oscillating bed through which flows oxygen-regulated hot gas.
  • a proportion of melt furnace extraction gas S 19 is used as a hot gas, to which air is added depending on the oxygen content, on the extraction gas side of the annealing device 116 .
  • the hot gas is supplied by way of a hot gas fan 118 .
  • the resulting flue gases are supplied to the combustion chamber 78 .
  • Ash R 3 which is contaminated with aluminium particles, is separated from the aluminium main flow as sieve passage from the bright annealing device 116 and ejected by way of a cellular wheel sluice 128 into a collection container 130 .
  • the annealed material i.e. bright aluminium
  • the annealed material is discharged from the bright annealing device 116 as sieve residue by way of a cellular wheel sluice and then output, by means of two hot goods conveyors 122 , 124 connected in succession to the foil separator, into a buffer container 126 .
  • the material is supplied to a sieve 134 by way of a constant conveyor 132 .
  • foil is removed from the material flow by air separation, and subsequently precipitated from the separated air in a hot gas cyclone 136 and discharged by way of a cellular wheel sluice 138 into a collection container 140 .
  • the hot gas leaves the hot gas cyclone 136 by way of a hot gas fan 137 .
  • the separated foil residue can be passed to separate recycling.
  • the heavy goods from the air separation i.e. the remaining aluminium fraction
  • a hot goods conveyor 144 by way of a cellular wheel sluice 142 .
  • This opens into an alternating flap 146 which divides the material flow, i.e. bright aluminium S 13 , into two lines.
  • One part is output directly to the buffer container 148 , the other part reaches a further buffer container 154 by way of two hot goods conveyors 150 , 152 connected in succession.
  • Both buffer containers or silos 148 , 154 supply an attached melting plant BE 3 by means of constant conveyors 156 , 158 .
  • the pyrolysis gas S 7 is taken from the pyrolysis drum 70 by way of a redundant pressure control on the outlet housing 88 .
  • the extraction quantity of gas depends on the pressure inside the drum.
  • the separated pyrolysis gas is transported in the shortest route by means of the, also redundant, double jacket heated pyrolysis gas line 86 to the combustion chamber 78 .
  • the heating jacket 84 of the pyrolysis gas line 86 here receives the heating jacket exhaust gas from the pyrolysis drum 70 .
  • the combustion chamber 78 is a lined, high temperature-resistant combustion chamber (burner muffle) into which the pyrolysis gas is discharged by way of a ring line protected against backfire.
  • the combustion air is supplied, stepped at various levels, to achieve combustion as low in NO x as possible.
  • the oxygen content and temperature in the combustion chamber 78 are monitored and recorded. A combustion chamber temperature of 1200° C. is maintained and an oxygen content above 6% ensured in principle.
  • the combustion chamber geometry ensures a minimum flue gas holding time of 2 seconds. In plant start-up and shut-down mode, the combustion chamber is operated with natural gas.
  • the combustion chamber extraction gas where not used as a part-flow for the pyrolysis drum heating (S 8 ), is passed to the quench 160 .
  • the combustion chamber extraction gas used for heating is returned to the combustion chamber 78 .
  • the flue gas S 9 is shock-cooled to below 150° C. This prevents the reformation of polychlorinated p-dibenzodioxine and dibenzofurane (PCDD/PCDF) (prevention of de-novo synthesis).
  • PCDD/PCDF polychlorinated p-dibenzodioxine and dibenzofurane
  • the shock-cooling is achieved by spraying a very large quantity of water into the gas flow. This is recirculated by the quench sump pump or water circulation pump 162 , evaporation losses are constantly replaced under level control in the quench sump.
  • the heat extracted from the gas flow by way of the recirculated water is passed by way of a heat exchanger 164 to a second water circuit and output to the environment by way of the total of three cooling towers 102 a - c.
  • the quench 160 is fitted with an emergency spraying system; on failure of water circulation pump 162 water can still be sprayed into the quench 160 by way of an additional emergency water pump 163 . On power failure this system remains in operation by way of the emergency power supply.
  • the cooled extraction gas S 10 first reaches a droplet separator 166 and then a two-stage gas washer 168 a,b. Liquid occurring at the droplet separator 166 is recirculated in the quench circuit.
  • the hot extraction gas emerging from the combustion chamber 78 can be supplied alternatively for energy use.
  • the extraction gas After emerging from the combustion chamber 78 , the extraction gas enters a boiler with a cooling spiral.
  • the cooled extraction gas is passed for cleaning.
  • the water vapour, heated for example to 400° C. in the cooling spiral, is then passed at a pressure of 38 bar for example to a generator to generate power.
  • sodium lye S 17 As a washing fluid additive in the gas washer, sodium lye S 17 is used; the supply is pH-controlled and takes place by way of a sodium lye metering pump 170 in the sump or washing lye container 170 of the two washer stages. In addition, level-controlled fresh water is added. Slurry water with washer slurry (R 2 ) is continuously centrifuged out from the washer circuit and quench water circuit, and supplied by means of the washer sump pumps 172 , 174 to an evaporation system designed as a thin layer vaporiser 176 . The washing circuits of the two washer stages are operated by redundant circulation pumps 178 , 180 (stage 1 ) and 182 , 184 (stage 2 ).
  • the washed exhaust gas S 11 leaves the flue gas cleaning system at a temperature of around 85° C., saturated with water vapour. To achieve better extraction of the exhaust gas it is therefore raised to a temperature of approximately 105-110° C. by the supply of hot melt gases and then discharged by means of a redundantly designed exhaust gas fan by way of a chimney 189 into the free air flow.
  • salts such as oxides (R 2 ) remain. These can be used, where applicable after recipe correction, as melt salts in the melt plant BE 3 .
  • the melt plant BE 3 is a twin-chamber system (open well) and consists of an open charging chamber 190 , 192 with vortex system, a pump 194 , 196 , an open hearth furnace as a heating chamber, and a conduit system.
  • liquid metal is transported by a pump by way of a conduit into a specially designed charging chamber 190 , 192 , and there given a rotary movement, creating a vortex.
  • the metal flow returns to the open hearth furnace 198 , 200 .
  • the enthalpy applied in the melting process is compensated by gas heating.
  • natural gas air burners 202 , 204 are used.
  • Oxides and salts from the melting process remain on the bath surface as metal-rich scabs.
  • the scab is moved from the open hearth furnace 198 , 200 in a rhythm determined by operation.
  • the melted liquid aluminium is supplied in batches to the foundry, either with liquid metal crucibles 206 , 208 and transport trolleys, or cast to size by way of a casting device 210 , 212 .
  • the melt power of the system is designed for example so that in total max 5 t/h can be melted (2.5 t/h per melt device); this output is achieved only if material with few organic adhesions is pyrolysed. On average around 3.4 t/h are melted.
  • the metal produced is characterised and processed according to its alloy composition.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Manufacturing & Machinery (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Processing Of Solid Wastes (AREA)
  • Cylinder Crankcases Of Internal Combustion Engines (AREA)
  • Disintegrating Or Milling (AREA)
US09/741,469 1999-12-24 2000-12-19 Aluminium base alloy of scrap metal and casting alloy produced from this Abandoned US20010006606A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US10/375,596 US20030129077A1 (en) 1999-12-24 2003-02-27 Aluminium base alloy of scrap metal and casting alloy produced from this

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP19990811210 EP1111077A1 (de) 1999-12-24 1999-12-24 Aluminiumbasislegierung aus Schrottmetall und daraus hergestellte Gusslegierung
EP99811210.6 1999-12-24

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US (2) US20010006606A1 (de)
EP (1) EP1111077A1 (de)
JP (1) JP2001254128A (de)
BR (1) BR0006375A (de)
CA (1) CA2329561A1 (de)
MX (1) MXPA00012836A (de)
NO (1) NO20006644L (de)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1479786A1 (de) * 2003-05-20 2004-11-24 Corus Aluminium N.V. Schmiedealumniumlegierung
CN109072357A (zh) * 2016-02-29 2018-12-21 爱励轧制产品德国有限责任公司 包含轧制铝合金的热交换器

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US7648561B2 (en) * 2005-11-22 2010-01-19 Tsl Engenharia, Manutencao E Preservacao Ambiental Ltda. Process and apparatus for use in recycling composite materials
JP2008077862A (ja) 2006-09-19 2008-04-03 Alps Electric Co Ltd 調光回路
AU2007260796B2 (en) * 2007-01-09 2010-09-02 Tsl Engenharia, Manutencao E Preservacao Ambiental Ltda. Process and apparatus for use in recycling composite materials
FR2917818B1 (fr) * 2007-06-21 2009-09-25 Solios Environnement Sa Procede d'optimisation de la commande d'un centre de traitement des fumees d'un four a feu tournant de cuisson de blocs carbones
JP5435258B2 (ja) * 2009-03-06 2014-03-05 アイシン精機株式会社 金属材料製造用ブリケット及びその製造方法
DE102010007531B4 (de) * 2010-02-11 2014-11-27 Audi Ag Verfahren zum Herstellen eines Karosseriebauteils
US8226019B2 (en) 2011-10-15 2012-07-24 Dean Andersen Trust Systems for isotropic quantization sorting of automobile shredder residue to enhance recovery of recyclable resources
US9132432B2 (en) 2011-10-15 2015-09-15 Dean Andersen Trust Isotropic quantization sorting systems of automobile shredder residue to enhance recovery of recyclable materials
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US20030129077A1 (en) 2003-07-10
NO20006644D0 (no) 2000-12-22
BR0006375A (pt) 2001-07-24
EP1111077A1 (de) 2001-06-27

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