Classifications

• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
  • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
  • C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
  • C01B3/08—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents with metals
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
  • C01F7/00—Compounds of aluminium
  • C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
  • C01F7/04—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom
  • C01F7/14—Aluminium oxide or hydroxide from alkali metal aluminates
  • C01F7/141—Aluminium oxide or hydroxide from alkali metal aluminates from aqueous aluminate solutions by neutralisation with an acidic agent
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
  • C01F7/00—Compounds of aluminium
  • C01F7/68—Aluminium compounds containing sulfur
  • C01F7/74—Sulfates
  • C01F7/741—Preparation from elemental aluminium or elemental aluminium containing materials, e.g. foil or dross
• • 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
  • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
  • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
  • Y02E60/30—Hydrogen technology
  • Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis

Definitions

• the invention relates to a method of recycling waste aluminum packaging into chemical compounds, particularly into aluminum sulfate, and a device for carrying out this method.
• Aluminum removed from waste is processed in other areas of human activity, particularly in the production of pure iriorganic elements or compounds.
• One of these compounds is the aluminum salt of sulfuric acid, more specifically aluminum sulfate.
• Aluminum sulfate is formed by a chemical reaction with sulfuric acid, in which it is allowed to dissolve. Sulfuric acid should not be too concentrated, otherwise passivating layers are created on the surface of the aluminum that prevent further dissolution of aluminum in sulfuric acid unless other ambient conditions are changed, such as pressure, temperature, or the presence of a reaction catalyst.
• the subject of the invention is a method for the production of aluminum sulfate, particularly from aluminum contained in waste.
• the waste is sorted, ground to fine particles, washed, dried, and subject to high temperatures as waste pulp until the occurrence of pyrolytic separation of the other substances, such as residues of organic products and colors.
• the aluminum- containing ash is then mixed with sulfuric acid at a reaction temperature ranging from 80° to 100° C.
• the aluminum reacts with the acid, forming a solution containing aluminum sulfate which is subsequently separated from the solution.
• Patent document CZ 231280 presents a method for manufacturing aluminum sulfate from pure aluminum in which sulfuric acid, in a concentration of 35% to 65% and a temperature ranging from 40° to 110° C, is sprinkled into an atmosphere of inert gas.
• the disadvantage of this solution lies in the fact that the aluminum used comes directly from production and could be used as material in other areas of human activity, and therefore the cost of thus produced aluminum sulfate is too high.
• the device comprises a preparation area for waste aluminum where aluminum is separated, shredded, and stored, further comprising a reactor in which the chemical conversion of waste aluminum occurs, a gas circuit for replacing the explosive mixture of air and hydrogen in the device with pure hydrogen and for the removal of the produced hydrogen from the reactor, a water circuit for supplying the hydrogen washing device with water for diluting the chemicals, a heat circuit for the removal of heat from the reactor and for heating the water in the water circuit
• a reactor in which the chemical conversion of waste aluminum occurs
• a gas circuit for replacing the explosive mixture of air and hydrogen in the device with pure hydrogen and for the removal of the produced hydrogen from the reactor
• a water circuit for supplying the hydrogen washing device with water for diluting the chemicals
• a heat circuit for the removal of heat from the reactor and for heating the water in the water circuit
• the objective of the invention is to provide a method for recycling waste aluminum and a device for carrying out this method in which the waste aluminum is shredded into small iparticles and is mixed with sulfuric acid at elevated temperatures, which would be ienvironmen tally friendly, which would not release hazardous substances into the atmosphere, which would primarily process secondary waste aluminum, which would produce pure aluminum sulfate, and which could be universally applied to other products.
• waste aluminum is initially shredded into particles sized from 1 mm to 10 mm, and then at elevated temperatures it reacts with sulfuric acid to produce hydrogen and aluminum sulfate.
• the essence of the invention consists in that the waste aluminum, after shredded, is washed in a liquid comprising an aqueous caustic solution in a concentration ranging from 0.2% to 15% by weight to remove impurities and greases from the waste aluminum, then rinsed with water, then a washing liquid is used containing impurities and partially dissolved neutralized waste aluminum to neutralize with neutralization acid, thus forming water containing impurities and salts of neutralization acid, and finally the water is separated from the impurities and salts of the neutralization acid, wherein the diluted caustic solution used is at least one caustic solution from the group NaOH and OH, and the neutralizing acid used is at least one acid from the group H 2 S0 4> HN0 3 , and H 3 P0 4 .
• Waste aluminum is dirty; it is usually still printed or glued, and it needs to be cleaned.
• a caustic solution such as a corrosive is very effective on organic residues and inorganic types of impurities (colors, labels, packaging). Since this is a corrosive, the caustic solution from the washing liquid should be neutralized by acid while taking advantage of the fact that the neutralization produces salt and water, which can be further processed.
• the concentration of the caustic solution is limited because a higher concentration of caustic solution in the water no longer increases the desired effect of cleaning the waste aluminum, so therefore a further increase in the concentration would be uneconomic.
• the caustic solution used to create the corrosive solution is at least one caustic solution from the group NaOH and KOH, and the neutralizing acid used is at least one acid from the group H2SO4, HNO3 and 3 ⁇ 4P0 4 .
• the neutralizing salts of these input substances are in demand in industry and are used in other applications of the chemical industry.
• the water created by the neutralization of the washing of the liquid after separation of the impurities is used for rinsing the waste aluminum or for preparing the washing of the liquid, wherein after reaching a concentration of salts in the salt-containing water a neutralizing acid of the amount of 25 g 1 to 50 g/1, then 30% to 50% of the total volume of water is pumped out to the separation of the neutralization salts, and the remaining 50% to 70% of water is diluted with pure water to 100% of the original volume.
• the use of one and the same water is ecological while at the same time the concentration of salts is increased, which subsequently separate. It is more economical to separate a salt a single time in a higher concentration than it is to perform a continuous separation of salts.
• the salts of the neutralizing acid are separated in the liquid or solid phase. Other separation is carried out for each of the salts according to its technological difficulty.
• the hydrogen formed from the reaction of waste aluminum, and. sulfuric acid is used for heating chemicals, waste aluminum, and water. Hydrogen is a good source of heat during incineration and is also very clean because only water vapor is released during its combustion.
• Part of the invention is also a device for carrying out a method according to the invention.
• the device for recycling waste aluminum through a reaction of aluminum shredded to a particle size from 1 mm to 10 mm with sulfuric acid to produce hydrogen and aluminum sulfate includes a waste aluminimi preparation area for purifying waste aluminum, for slrredding it into small particles, and for storing it. It further comprises a reactor for mixing the waste aluminum with sulfuric acid, for its reaction, and for its heating. Further, the device includes a gas circuit for distributing hydrogen throughout the device, a water circuit for distributing new or used water in the device, a thermal circuit for the production and distribution of heat, and a chemical preparation area for the preparation and separation of chemicals.
• the essence of the invention consists in that part of the waste aluminum preparation area includes at least one washing tank for filling the washing liquid which is adapted for the .neutralization of the used washing liquid, and/or at least one neutralizing tank adapted fcr the retention and neutralization of the used washing liquid from the washing tank.
• the cleaned aluminum is removed from the washing liquid and the used washing liquid, which is corrosive, must be safely neutralized. This can be done directly in the washing tank, or the used washing liquid can be pumped into the neutralizing tank, while another batch of aluminum waste is already prepared in the washing tank.
• the washing tank and neutralization tank form a single body.
• the used washing liquid does not need to laboriously pumped; the neutralization is carried out immediately after washing the waste aluminum.
• the neutralizing tank is connected through the water circuit to the waste aluminum preparatory area or to the chemical preparatory area.
• the water circuit transports water formed by the neutralization back to a new cycle of use, or to the separation of salts of the neutralizing acids.
• the reactor is connected with a gas circuit, which is connected to the thermal circuit, which includes a combustion chamber for the production of heat.
• the consumption of the produced hydrogen allows for the thermal self-sufficiency of the entire device.
• the advantages of the present invention consist in the processing of waste aluminum, in the sustainable approach to the environment, in the economic use of the input materials, in the possibility of producing several different products with the same resources, and in energy self-sufficiency.
• FIG. I schematically illustrates the part of the water circuit with the modification of operating ;:and cold water
• Fig. 2 schematically illustrates the part of the chemical preparation area with reservoirs tor additional ingredients
• Fig. 3 schematically illustrates the chemical preparation area with reservoirs for input chemicals
• Fig. A schematically illustrates the waste aluminum preparation area
• Fig. 5 schematically illustrates the sequence of means for loading the dose of aluminum into the reactor
• Fig. 6 schematically illustrates the reactor and sequence of the means of the first filtration
• Fig. 7 schematically illustrates the sequence of means for filtering the product from the reactor
• Fig. 8 schematically illustrates the part of the water circuit with filtration of waste solutions
• Fig. 9 schematically illustrates the part of the water circuit with means for managing hot water and steam
• Fig. 10 schematically illustrates the part of the gas circuit with means for removing bad odors
• Fig. 11 schematically illustrates the ⁇ art of the gas circuit with means for separati g the hydrogen
• Fig. 12 schematically illustrates the part of the gas circuit with means for distributing hydrogen and part of the thermal circuit.
• a device 107 for recycling waste aluminum 100 through a reaction of alumimun shredded into particles sized from 1 mm to 10 mm with sulfuric acid comprising the following operational units.
• Another operational aggregate is the reactor 1, in which the prepared waste aluminum is mixed with sulfuric acid and where the mixture is heated and reacts.
• a gas circuit 106 which serves for the exhaust of released odors and for processing the released hydrogen.
• Also included in the device 107 is a water circuit 97 which distributes new water or processes used water, and a thermal circuit 108 for the production and distribution of heat throughout the entire device 107.
• the device 107 also includes a chemical preparation area 99, in which the input chemicals are prepared and the products are separated.
• Fig. 1 schematically illustrates the treatment of the operational and cold water which is part of the water circuit 97.
• Water is fed from an operational water main 95 under a pressure of 3.5 bar at 10° C in an amount of about 40 m 3 /day into a device 33 for treating water which is equipped with an ion exchanger with a capacity of 10 m 3 /h.
• the ionic waste 96 is disassociated from the water in the device 33 and the treated water is led under pressure from the water main into a pure water reservoir 34 with a volume of 20 m 3 while maintaining a water temperature of 10° C.
• the water is pumped into a reservoir 8 of a concentrated solution of aluminum sulfate, and the water from the reservoir 34 is pumped by a pump 35 further into a reservoir 36 i ' or cold water.
• the cold water reservoir 36 has a volume of 10 m 3 and the water is retained at a temperature of 10° C.
• a hydrogen cooler 23 and an auger 86 for diatomite To the cold water reservoir 36 there are connected a hydrogen cooler 23 and an auger 86 for diatomite.
• an integrated cooling auger connected to the cooling compressor 32, and also connected to the reservoir 36 there is a pump 37 for the distribution of cold water to the odor trap 58.
• tank 30 for emergency, chemical, and operational water with a volume of 15 m 3 with a pH reduced to 0.5 and a water temperature of 40° C.
• a pump 38 which directs the operating water to the reactor 1 as needed.
• Fig. 2 schematically illustrates the reservoirs 17 and 84 of additional ingredients for the chemical preparation area 99.
• the activated carbon reservoir 17 From the input chemical storage 98, approximately 5 m 3 of material is stored into the activated carbon reservoir 17. From the reservoir 17, the activated carbon is transported by an auger 85 into a mixing tank 4 for the preparation of a filtration mixture, into a neutralizing tank 65, and to the reactor 1.
• the diatomite reservoir 84 has a volume of 10 m 3 , and is connected to the auger 86, which also removes the diatomite into the mixing tank 4 for the filtration mixture, into the neutralizing tank 65, and into the reactor 1.
• Fig. 3 schematically illustrates the reservoirs 61, 62, 87, and 88 of the chemical preparation area 99.
• potassium hydroxide at a concentration of 50% into a total volume of 25 m 3 , the temperature of which is 40° C, is supplied into the reservoir 61.
• a pump 63 To the output of the reservoir 61 there is connected a pump 63, which moves 50% of the KOH into a washing liquid reservoir 51.
• Fig. 3 depicts a reservoir 62 for sulfuric acid with a capacity of 25 m 3 .
• the H 2 S0 4 is, after the storage, diluted to a concentration of 50% at a temperature of 40° C. From the reservoir 62 the H2SO4 is moved by a pump 64 to the reactor 1.
• the next depicted reservoir 87 is designed for the detention of nitric acid.
• the concentration of nitric acid is 65%
• the volume of the reservoir is 25 m 3
• the temperature of the retained substance is 40° C.
• the nitric acid is moved to the neutralization tank 65.
• the last depicted reservoir 88 is designed for phosphoric acid at a concentration of 85% and a capacity of 25 m 3 .
• the 3 ⁇ 4 ⁇ 0 4 which is stored at 40° C, is moved from the reservoir 88 through a pump 90 to the neutralizing tank 65.
• Fig. 4 schematically illustrates the shredding and degreasing of the raw waste aluminum in the aluminum waste preparation area 102.
• Raw waste aluminum scrap 100 including aluminum from municipal waste, is stored in a concrete tub 40 that has a volume of 100 m 3 , and is sunk below ground level and covered. From the concrete tub 40 the raw waste aluminum is transported by a conveyor 41 to the shredder 42 which shreds the raw waste aluminum into particles with an average size of 5 mm. From the shredder 42 the shredded raw waste aluminum is accumulated by the conveyor 43 into a washing tank 44 with a wash basket that has a volume of 10 m 3 .
• the washing liquid is led at a temperature of 20° C, with a pH value of 14, at a concentration of 2% KOH which was pumped in from the pump 63.
• the washing liquid reservoir 51 there is also fed relatively pure water from the tank 76.
• the washing liquid washes the raw shredded waste aluminum and is then, together with the dissolved impurities, pumped by pump 60 to a neutralizing tank 65.
• the washing basket is transported across a roller 45 to the rinsing tank 46, into which water is fed from a reservoir 36, as well as hot air from the heat exchanger 49, which is moved by a fan 48 drawing ambient air 101 through a filter.
• the heat exchanger 49 is heated by hot water heated to 95° C from the reservoir 50, and the cooled water is returned to the tank 50 from the heat exchanger 49.
• the water from the rinsing tank 46 is pumped by a pump 56 into the emergency and diluting water reservoir 30.
• the cleaned and shredded aluminum is transported to a silo 39.
• the vapor from the water from the rinsing tank 46 is condensed back into water in the heat exchanger 47, from which water is led into the hot water reservoir 50.
• the air from the heat exchanger 47 is led by a vacuum pump 57 to the odor trap 58.
• the heat exchange in the heat exchanger 47 is supported by the cold water from the reservoir 36, which, upon receipt of the released heat, is led into the hot water tank 50.
• Fig. 5 shows a schematic illustration of the dispensing of cleaned aluminum into the reactor 1.
• the aluminum awaits transport to the reactor 1.
• the aluminum is transported by the conveyor 82 to the dispensing device 20 which has a volume of about 1 m 3 .
• the dispensing device 20 the aluminum is kept airtight and the air is rinsed with flushing hydrogen from the mid-pressure reservoir 26 for operating hydrogen into an odor trap 58.
• r rhe dose of aluminum is then transported by the conveyor 83 from the device 20 conveyed into the reactor 1.
• Fig. 6 shows a schematic illustration of the reactor 1 and the individual connected devices.
• the reactor 1 has a volume of 4.5 m 3 and is designed for an operating temperature of 95° C at a pressure of 1.5 bar. It is provided with means for mixing, a cleaning hatch, and includes double heating/cooling housing.
• Into the reactor 1 is conveyed clean shredded aluminum from the dispensing device 20, and 50% sulfuric acid is pumped into the reactor 1 by a pump 64.
• Activated carbon from the reservoir 17 and diatomite from the reservoir 84 are also fed to the reactor 1.
• the reactor 1 is provided with a supply of emergency dilution water from the reservoir 30 for the eventual opouring and neutralizing the contained reactants for safety.
• From the reactor 1 there are discharged gaseous substances that formed during the chemical reactions, such as hydrogen discharged at.a pressure of 1.5 bar into the washing tank 21, or odors that are sent to the odor trap 58.
• the Koeactor ! is emptied through a drain valve 10, from where the reaction mixture is sent to a press filter 2.
• the press filter 2 is supplied with hot water from the reservoir 50 and released gases are drawn from it into the odor traps 58 while filtering the solids 103 from the reaction liquid mixture.
• reaction liquid mixture continues through the discharge valve 11 into the inter-reservoir 3 of the reaction liquid during the intake of air 101, which flushes the remainder of the odors into the trap 58.
• the reacted reaction liquid is pumped by a pump 12 into the mixing tank 4.
• Fig. 7 illustrates a diagram of the filtration of die reaction mixture and the finished product.
• activated carbon and diatomite is fed from reservoirs 17 and 84, whereupon the reaction mixture is stirred at a temperature of 50° C.
• the mixture is pumped by a pump 13 to a BF diatomite filture 5 on an active area of 4 m 2 at a throughput of 2.7 m 3 /h, where the diatomite as a solid component 103 is separated at a temperature of 40° C.
• the solution is pumped by a pump 14 into the pure solution reservoir 6.
• the solution is stored at a temperature of 30° C.
• the pure solution is pumped by a pump 15 into a reservoir 8 of concentrated sulfate with a capacity of 10 m 3 , where it is stirred and heated to a temperature of 60° C.
• the concentrated solution of sulfate is drained by a pump 16 into a reservoir 9 for the finished product, where the sulfate solution is diluted with clean water from the reservoir 34 into the output concentration and the solution is pumped by a pump 18 from the reservoir into distribution 104.
• the reservoir 9 has a capacity of 25 m 3 and the solution temperature is maintained at 20° C.
• Fig. 8 schematically illustrates the filtration of waste solutions in the water circuit 97.
• the neutralizing tank 65 there is pumped the used washing liquid by a pump 60 while further into the neutralizing tank 65 there is dispensed diatomite and activated carbon from reservoirs 17 and 84.
• the pH is neutralized to the value of 7 by the neutralization acid from the reservoir 88 or from the reservoir 89, and the neutralized used washing liquid is stirred at a temperature of 30° C.
• the volume of the tank 65 is 10 m 3 .
• the used washing liquid passes through the tank 65 at a volume of 2 m 3 h.
• the pump 66 drains the mixture of used washing liquid to a BF filter 67 for separating solid components 103 while maintaining the same temperature.
• the BF filter 67 has an active area of 4 m 2 . From the BF filter 67 ; through the pump 68, the pure solution from the washing liquid is pumped into the reservoir 3 ⁇ 469 of pure neutralized solution. From the reservoir 69, the solution is pumped by a pump 70 into the device 71 for reducing water, in which 50% of the water is removed from the total volume of the solution and is returned to the reservoir 76.
• the concentrated solution is drained from the device 71 for reducing water by a pump 72 to a reservoir 73 of salt solution, from where approximately half the total volume is returned by a pump 74 into the reservoir 51 of washing liquid, and the other half is pumped by a pump 75 into the tank 78 for storing sodium sulfate and aluminum sulfate.
• the concentrated solutions are driven by a pump 79 to the evaporator 91 where the remaining water is removed using high temperatures.
• the salts are stored by the conveyor 92 in the storage area 93 or storage area 94 from where they are transferred to distribution 104.
• Fig. 9 schematically illustrates the hot water system.
• water is returned to the reservoir 50.
• water from the steam generator 54, which is supplied by the pump 55.
• the steam generator produces steam 105 at a temperature of 150° C, which is driven into the heat exchanger 53.
• Through the heat exchanger 53 there flows water from the pump 55 into the reservoir 50.
• Hot water is pumped by the pump 55 into the reactor ⁇ to be heated as well as to the other components of the device 107 where the internal temperature must be kept above 10° C, including their pipes.
• FIG. 10 schematically illustrates the trapping of the released gases and odors.
• a vaciium pump 57 which develops a vacuum of about 1.3 kPa, pumps gases from the reactor 1, from the hydrogen washing tank 21, from the hydrogen separator tank 22, and from the hydrogen cooler 23, and blows them into the odor trap 58.
• the odor trap 58 there is also fed water from the reservoir 36 and, through pressure, the other gases from the other tanks and reservoirs.
• used water is pumped by pump 7 into the tank 30 for emergency water.
• the gases leave on their own pressure to the inlet 80 of the chimney 59, from where they escape into the atmosphere. Condensates from the inlet 80 are diverted back into the tank 30.
• Fig. 11 schematically illustrates the washing and drying of hydrogen.
• hydrogen is fed to the hydrogen washing tank 21, in which a pressure of 13 bar and a temperature of 20° to 40° C are maintained. Also into the hydrogen washing tank 21 there is fed water from the reservoir 34.
• the circulation pump 29 is connected, as is a device for treating water 33 for draining the water into the tank 30.
• hydrogen is drained into the separation tank 22, in which hydrogen is separated from water using Raschig rings.
• the pressure is 1 bar and the temperature is 20° C.
• a pump 31 for draining water into the tank 30.
• Hydrogen further continues to a hydrogen cooler 23, where it is supercooled to -20° C using a refrigeration auger connected to a cooling compressor 32. Relatively dry hydrogen leaves the cooler 23.
• the auger of the compressor 32 is defrosted by warm water fed from the reservoir 50, while dissolved water is discharged into the tank 30.
• Fig. 12 schematically illustrates the compression and distribution of hydrogen.
• a low- pressure hydrogen tank 24 there is pumped hydrogen under a pressure of 1 bar, while the temperature in the tank 24 corresponds to the temperature of the surrounding environment.
• the tank 24 there condense the remnants of the water which are discharged into the tank 30.
• Hydrogen is pumped by a compressor 25 into a medium pressure hydrogen tank 26, where the pressure of the stored hydrogen is approximately 10 bars. From here, the hydrogen is pumped into the reactor 1, into the dispensing device 20, and into the combustion chamber 27, from where the formed heat is used for the hot air exchanger 28.
• the heat exchanger 28 heats the water using hot air, or the warm air is removed for heating the building.
• the washing liquid is neutralized in the tank 65 to a pH of 7 by sulfuric acid pumped in by pump 64.
• the neutralized liquid is filtered and the salt solution with water is re-used to produce the washing liquid until the concentration of dissolved salts increases to a value of 30 g/liter.
• the 35% volume of the thus concentrated solution is pumped to the separation of salts, and the remainder is diluted with new water re-used to prepare the washing liquid.
• the rate of return of the resulting salts A1 2 (S0 4 ) 3 per 24 hours is 130 kg
• the rate of return of KSO 4 per 24 hours is 220 kg.
• the hydrogen released from the reaction of sulfuric acid and aluminum is burned in the combustion chamber 27, and the heat released is used through the heat exchanger 28 to heat water, chemicals, and for heating.
• washing liquid in the neutralization tank 65 is neutralized with nitric acid.
• washing liquid in the neutralization tank 65 is neutralized with phosphoric acid.
• a method of recycling waste packaging aluminum into chemical compounds, particularly into aluminum sulfate, and a device for carrying out this method, are designed for the secondary ⁇ processing of used aluminum, the recycling of which is unprofitable using conventional methods.
• drain valve 1 1. drain valve

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• Chemical & Material Sciences (AREA)
• Organic Chemistry (AREA)
• Inorganic Chemistry (AREA)
• Life Sciences & Earth Sciences (AREA)
• Geology (AREA)
• Health & Medical Sciences (AREA)
• Chemical Kinetics & Catalysis (AREA)
• General Health & Medical Sciences (AREA)
• Engineering & Computer Science (AREA)
• Combustion & Propulsion (AREA)
• Processing Of Solid Wastes (AREA)

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• 2013
  • 2013-09-30 CZ CZ2013-749A patent/CZ2013749A3/cs not_active IP Right Cessation
• 2014
  • 2014-09-29 EP EP14795940.7A patent/EP3052434A1/en not_active Withdrawn
  • 2014-09-29 WO PCT/CZ2014/000105 patent/WO2015043557A1/en not_active Ceased

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