BR102014028989A2 - PROCESS FOR RECYCLING THROUGH SEPARATION OF THE CONSTITUENTS OF ALUMINIZED AND PLASTICATED CARTONED PACKAGING - Google Patents

Abstract

process for recycling by separating the constituents of aluminized and plasticized carton packs, refers to the process patent for recycling and waste utilization, particularly that of plasticized, aluminized and non-carton packs, by means of extraction and separation of main components present in them for waste utilization avoiding environmental pollution, recycling of waste constituents; and recovering the constituents; plastic, aluminum and paper in their original form, bringing the advantages of obtaining reusable quality polymer, obtaining insulated aluminum, making use of low-cost, readily available solvent, energy-efficient pulp, to be reapplied in the production of carton paper, for box manufacturing, incorporated as part of a mechanical pulp load or even for clarification, to have lower processing and investment costs and to be less cost-effective.

Description

"PROCESS FOR RECYCLING THROUGH SEPARATION OF ALUMINIZED AND PLASTICATED CARTON PACKAGING" [01] This patent refers to a process for recycling and the recovery of waste, particularly plasticized, aluminized and non-cartoned packaging, by method extraction and separation of the main components present in them for waste utilization avoiding environmental pollution, recycling of waste constituents; and recovering the constituents; plastic, aluminum and paper in their original form, having advantages of obtaining reusable quality polymer, obtaining insulated aluminum which can be melted and purified by conventional processes such as recycling aluminum cans and other scrap metal, or if it prefers to be used as a raw material for the production of aluminum derivatives such as salts, organoaluminium, or even aluminum pigment, to make use of low cost, low energy consuming solvent in the market, the pulp may to be reapplied in the production of carton paper, for box manufacturing, incorporated as part of a mechanical pulp load or even for clarification, to have lower processing and investment costs and to be less cost-effective.

[02] As is well known by the technical means linked to the recycling industry for waste recovery, particularly packaging, the technologies employed to date make the recovery of cellulose pulp from carton, plasticized and aluminized packaging, which It is intended for paper making. However, the composite aluminum / polymer process waste is simply ground and used for making parts through the injection process to produce artifacts such as broom handles, thermal pressing in the manufacture of corrugated tiles among others. Thus, not isolating the aluminum component does not exploit its high value as a raw material. Also known are processes which make use of pyrolysis for further generation of energy, thus leading to the production of liquid and / or gaseous fuels. However, although this process produces fuels, it requires a large amount of energy, energy is provided by burning part of the waste itself, since the pyrolysis process involves extremely endothermic reaction.

[03] It is important to note that, in terms of packaging, it is actually a paper / aluminum / polymer sandwich, where the latter polymeric component has a softening point of 125 ° C and a pouring point of 190 ° C and almost entirely made of polymer, which contains in its composition a compatibilizer that promotes better adhesion of low density polyethylene to aluminum. Typically, functionalized polyolefins such as ethylene and acrylic or methacrylic acid copolymer are employed for such function. These compounds in return will contribute to improving the compatibility of the recovered material with other thermoplastics such as polypropylene and polyethylene terephthalate (PET) as well as polyamides such as nylon®, thereby making future reuse of the recovered material more flexible.

[04] Searching national and international patent banks we find the following disclosures: [05] Spanish patent PI 2383208 "Procedures for the recycling of aluminum-containing composite materials" reveals a technique that recovers pulp by mechanical breakdown of the packaging and the waste is then conducted for aluminum recovery.

[06] However, in this process polyethylene is destroyed and converted to paraffins and gases. Said process makes use of plasma to conduct the operation which, besides leading to the loss of the polymer requires for its operation the consumption of a high amount of energy, since to operate the plasma requires temperatures of the order of 15,000. ° C, besides the need to operate in an inert atmosphere, which means high cost.

[07] Several patents employ solvents for the recovery of carton packaging plastics: Brazilian patent PI 0202303-2 "Multilayer film separation process used for packaging" using various solvents such as tetrahydrofuran, xylene, toluene, tetrachloride carbon, organic acids, water, acetone and chloroform; Chinese Patent CN 1554691 ”Method for Separating Aluminum into Sheets and Plastics in Aluminized Plastic Packaging Waste Films” makes use of solvents such as tetraline, tetrahydrofuran in addition to the incorporation of glacial acetic acid, which transforms aluminum into a salt ; and Korean patent KR 20010016352, discloses a process which promotes the reaction of aluminum in the presence of alcohols, such as methanol, ethanol, propanol or butanol, associated with chloride salts such as mercury, calcium, magnesium aluminum, potassium chloride. or even hydrochloric acid.

[08] These processes use highly toxic and carcinogenic solvents and reagents, and have a great potential for polymer degradation associated or not, to compounds that react with aluminum, turning it into a salt, leading not only high reagent consumption, but also not allowing full recovery of aluminum in its original metallic form.

[09] Other patents disclose other separation methods, such as Brazilian patent PI0006641-9 “Surfactant solution used in the recycling process of plastics for cleaning and aluminum separation”, which employs a surfactant and formic acid for film removal. However, the presence of an acid under the mentioned operating conditions also leads to the consumption of part of the aluminum present in the residue.

[010] Other patents also disclose processes that remove aluminum by chemical reaction, usually employing strong bases or acids: [011] Brazilian patent PI 0706115-3 "Multilayer packaging recycling", which utilizes a sodium hydroxide solution thereof. US Patent 5127958 "Removing Metal Roofs from Polymeric Substrates".

[012] Chinese patent CN 102532592 "Aluminum-plastic separation agents and corresponding preparation method" in turn employs 5 to 50% acid associated with an unspecified 25 to 50% organic solvent. Similarly, Japanese Patent JP 20040327047 discloses separation of polymers by density difference in glycol solution, however, also attacks Aluminum with sodium hydroxide.

It is important to highlight that in these processes where acids or bases are used, these reagents are consumed, which increases the cost of the process, but also when consuming all or part of aluminum, there are economic losses resulting in lower value-added products. .

US Patent 7,598,297, to cover other possible processes, comprehensively describes every possible range of solvents as well as the use of a strong base such as sodium or potassium hydroxide. Similarly over a wide temperature spectrum. However, in its claim it specifically uses xylene only, and operates at different temperatures so that it can selectively remove the different naturally occurring polymers in said packages, however using a strong base undoubtedly leads to the consumption of aluminum.

European patent EP 0568791 discloses a cast of any and all solvents of different natures as petroleum derivatives (aliphatic, naphthenic aromatics), halogenated compounds and mixtures thereof, as well as a wide temperature range of 40 to 500 ° C, similarly trying to get exclusivity from any process. However, by proceeding with the process of separating the constituents using the packages in their composite form, paper, aluminum and polymer, certainly, beyond this wide range, it certainly leads to a high consumption of process solvent. Said process also explores, among other application forms, the conduction of the solution containing the different polymers dissolved in the different solvents listed in a thermal cracking process operated in the range of 650 - 1200 0 C and pressures of 0.1-0, 3. MPa.

[016] The processes disclosed in the prior art present the following problems, which the present process solved: [017] 1. Some current processes do not recover all constituents in their highest added value form. The process of the present invention recovers all reusable constituents;

[018] 2. Some processes consume a lot of energy in melting aluminum and polymer mixtures, including decomposing the polymer. The process of the present invention separates with solvent only;

[019] 3. Some processes require complex and expensive operations for polymer separation from aluminum. The process of the present invention separates only with solvent, leading the process by operations that involve low investment and low cost of raw material; and [020] 4. Some processes use toxic solvents that are difficult to separate and recycle in their use. The process of the present invention utilizes commercially abundant, non-toxic, low-energy, fully recycled, low-energy solvents.

[021] Processes disclosed in the prior art have the following drawbacks, disadvantages and limitations: [022] (a) Some current processes do not recover all constituents in their highest added value form;

(023) (b) Some current processes for the recovery of aluminum-bound polymer consume other inputs which, in addition to not being recovered for the process, generate low commercial value product;

(024) (c) In some processes, the aluminum is not separated from the polymer, so that the two components are employed, mixed together, thus proceeding with aluminum, a high added value component, in the condition of isolated compound, only enter as loading on products made from said mixture;

[025] d) Certain processes insulate aluminum, but do so by consuming a great deal of energy, using very high temperatures, which leads to the cracking of the polymer that is destroyed and made into a mixture of waxes and volatile compounds of value. lower aggregate than polymer, still requires operation in the presence of inert atmosphere, which certainly contributes to cost increase;

[026] e) Use of expensive and toxic solvents;

[027] (f) high processing and investment costs; and [028] g) Greater value for money.

[029] “PROCESS FOR RECYCLING THROUGH SEPARATION OF CARTRIDGE, ALUMINIZED AND PLASTICATED PACKAGING has been developed to overcome the drawbacks, disadvantages and limitations of current processes through solvent-based method for polymer dissolution in extraction and separation the main components present in them for waste utilization avoiding environmental pollution, recycling of waste constituents; and recovering the constituents in their original form for reuse as plastic, aluminum and paper.

[030] The process of the present patent has the following advantages over current processes: [031] a) The developed process obtains reusable quality polymer for making artifacts and films, which can be made with said recovered product and can therefore be used in its raw form as it was removed from the process, or even be mixed with another virgin or recovered polymer, in the composition of blends which may further receive fillers, dyes or other additives;

(B) Aluminum isolated from the process may be conducted in a melting and purification process, as in conventional processes for recycling aluminum cans and other scrap metal, and may thus be used as a raw material either in the production of alloys, blades, inorganic compounds such as salts, aluminates, or even organic derivatives such as alkylaluminum;

C) The invention makes use of a commercially available, low-cost solvent, as it is not a synthesis compound, being a distilled fraction of petroleum;

(034) (d) By using a solvent which is a narrow-range boiling fraction petroleum fraction and not being incorporated into the product at the end of the process, the recovery of the product is complete as it fully resumes at the beginning of the process. The distillation may be conducted in simple equipment requiring no fractional distillation;

[035] e) Solvent characteristics: low boiling temperature, low specific heat and low evaporation enthalpy are significant in energy consumption as only a small fraction is evaporated and almost all of the solvent is evaporated. It is recycled without distillation, which greatly reduces energy consumption because it does so by filtration;

F) The process of the invention recovers the polymer maintaining its physical and chemical characteristics including the compatibilizer, which favors the future application of the recovered polymeric residue in the formulation of blends with other thermoplastics;

(037) (g) Cellulose pulp may be reapplied in the production of cartonboard paper, incorporated as part of a mechanical pulp load or even for clarification;

[038] (h) lower processing and investment costs; and [039] (i) lower cost / benefit ratio.

[040] The process of the present invention was based on the inventor's knowledge and experience in his previous research and development work with paraffin and polymer compound blocks applied as a radiation barrier (moderators) and later in the development of explosive compositions. , specifically emulsions type.

[041] Research has begun to address the need to recycle packaging waste to recover the polymer / aluminum waste polymer from a mechanical process, which employs hydrapulper to recover paper pulp from aluminized packaging waste.

[042] The initial objective was to remove aluminum by dissolving, etching, to produce aluminum salts for use in wastewater treatment. The process was also adjusted to obtain aluminates, sulfates and aluminum chloride. The resulting polymer from acid or base digestion after washing would then be taken for recycling. However, by evaluating the price of these salts, and comparing the flexibility of use of aluminum in its (reduced) metallic state, it was decided to evaluate the possibility of removal of the metal without being brought to its oxidized state.

Based on knowledge of the properties of the polymer with respect to its structure and similarity to solid paraffins, polymer solubilization assays in solid paraffin were initiated in the following sequence: [044] In a Becker beaker containing 100 g of solid paraffin, after melting and having raised the temperature to 100 ° C, 20 g of aluminum / polymer containing films were incorporated. The temperature was raised to about 125 ° C. Stirred with a glass stick for five minutes. The entire contents were transferred to another Becker beaker by passing the molten paraffin through a metal sieve. After cooling the sieve contents, it was washed with cold carbon tetrachloride. Knowing that this solubilizes the paraffin cold, but the polymer only if heated, it can be seen that the paraffin removed the polymer adhered to aluminum, a fact proven by tearing the resulting film, which broke without stretching a plastic film different from the behavior of tear of the composite film.

Another finding was that the resulting paraffin / polymer mixture solidified at a lower temperature when subjected to heating compared to a blank paraffin-only test.

In view of this, a possible way of separating the paraffin from the polymer was considered. A problem was difficult to solve, as it would not be possible to think of distillation or fractional solubilization, since it was a mixture of high molecular weights. It was then set off to employ directly carbon tetrachloride. However, due to its high cost and high toxicity characteristics, its use was discontinued.

[047] Other chlorides were then researched but the problems cited by the former were also repeated.

[048] In the next step studies were made with aromatic, chlorinated and non-chlorinated, naphthenic solvents, as well as esters of alcohols, acetyls of amyl, methyl, butyl, and others.

[049] In parallel the removals of aluminum linked to polypropylene, PET and PVC present in different packages such as medicine blister packs, refreshment powder packs, cookie packets, candy and chips were also tested. For all these products positive results were achieved for some of the solvents tested. Some of these solvents were studied with more criteria considering the aspect of health risks as well as their accessibility and cost.

[050] However, the main focus remained on cartoned aluminized packaging. In this sense, the tests with the other residues were interrupted and the tests with the last ones continued.

In view of the difficulty of separation when paraffin was used, it was decided to evaluate the use of kerosene, since it is of paraffin structure similar to the solid paraffin employed. The results obtained using the same mass ratios were positive. Dissolution occurred in less than 5 minutes. The next problem then arose, removing all solvent from the polymer. The solvent would probably have in its composition high molecular weight paraffin compounds in small quantities, which required the polymer to be brought to elevated temperature for effective removal of that residual component. Considering also the size of the kerosene and paraffin chain, strong interactions would be present, factors that make the separation difficult.

[052] It was then set off for precipitation separation. The cooled polymer / kerosene solution was presented as a paste. This paste was then incorporated into the same volume of ethanol under stirring. The precipitated polymer was then filtered, subjected to successive ethanol washes. Drying was obtained and precipitated polymer was obtained.

The resulting solvent mixture was distilled off to separate ethanol from kerosene. Considering the difficulties in the distillation elimination of residual kerosene in the precipitated polymer, we proceeded to use a solvent with the same characteristics as the kerosene, but with a lower boiling point.

Commercial hexane was then used because it is a more volatile solvent and dissolved in a flask coupled with a reflux condenser. The same solvent / residue ratio was employed. Five minutes was sufficient for dissolution to occur.

In another experiment petroleum ether was employed, distillation range of 60 ° C. Dissolution difficulty was observed, since unlike the commercial hexane employed in the previous test, the temperature reached in the latter was not sufficient to lead to dissolution. .

[056] In a later experiment, compared to the previous experiment, the same amounts of solvent / residue were placed in a steel tank, which was then closed and placed under heating in hot water. When the water bath reached boiling temperature, the tank under heating was removed and allowed to cool. When the reactor was opened, as its contents were still slightly heated, much of the solvent vaporized from the tank, resulting in a polymer sponge. The experiment was then reproduced under pressure to operate at the polymer softening temperature. Upon dissolution, the solvent was removed gradually, keeping the environment of the dissolver heated at the same pressure and temperature, obtaining, after cooling, solid polymer.

[057] Therefore, after several tests it was concluded that the most suitable solvent for the isolation and separation of polymer from the aluminized and plasticized carton packs are the low and medium boiling alkanes, therefore of lower molecular weight. because they more easily interact with the large polymer chain and favor, due to the reduced chain size, rapid interaction and consequent polymer dissolution, since, due to their short chain length, it easily diffuses between the polymer chains. Moreover, since the linear solvent structure is similar to the polymer, it does not interfere with its breakdown, with only Van der Walls breaking forces.

[058] The reason why normal paraffin hydrocarbons (straight chain alkanes) have been chosen is because these compounds are less toxic than aromatic or even naphthenic, also minimizing the risk of polymer degradation (ie due to structural similarity) as well as for their easy elimination by evaporation and / or distillation).

[059] Experiments have shown the feasibility of using paraffinic hydrocarbon solvent boiling below 120 ° C, preferably from 60 to 100 ° C, operation is well below polymer flow temperature which is approximately 190 ° C Thus, it is observed that it operates at a temperature close to softening, about 125 ° C, without having to operate at such high pressures. The ease of dissolution and consequent flexibility of its elimination when the return to atmospheric pressure leads to a better final quality of the recovered polymer. To circumvent the dissolution temperature problem, which falling below the polymer softening temperature was operated with increased pressure thus reaching the ideal process temperature which is the polymer softening temperature.

As for the separation of the solvent, as the boiling point was below the softening temperature of the polymer, when the solution left the dissolver part of the solvent evaporated, but before removing the aluminum, it was of course added after removal. of the solution containing most of the polymer, new solvent (distillate) that washed the aluminum. This still heated solvent was used as the first solvent of the next batch, thus optimizing the solvent recovery process.

The solution containing the polymer, after partial concentration due to partial evaporation of the solvent, whose vapors were conducted to the condenser, was then carried to the later step.

Finally, the last sequence of experiments was evaluated filtration technique. Ultrafiltration (emulsions, bacteria, fats and macromolecules) is known to have an operating pressure range of 1 to 10 bar, with pore membranes ranging from 0.001 to 0.1. The average molecular weight of the polymer is ~ 200000 Da , this technique could be promising, in addition to the possibility of rational use of energy, for example.Use of the gases served from a boiler, leaving the chimney with temperature around 250 ° C, which could be carried to the tower or evaporation and drying of the polymer, and if the melting of the aluminum were performed, when cooling the ingots the air of the exchanger would leave with initial temperature of 650 ° C and final could be in the range of 125 ° C, thus making adequate energy use.

The pressure filtration of an 11% dissolved polymer solution was initially tested under pressure using filter paper on a porous ceramic plate and it was observed that solvent migrated by capillary and the more concentrated polymer was retained on the paper.

[064] In another assay the solution was subjected to room cooling and subsequent filtration on paper, applying light pressure manually with syringe-shaped equipment and it was observed that the solvent was easily separated. Afterwards the paper-wrapped wet cake was pressed using a press, the cake formed with very little solvent. Thus it was evident that the separation process can be efficiently improved, thereby saving energy by filtering the solution hot and subsequently subjecting the cake to compression on the filtering surface. Although filter paper is employed, the cake is easily detached from the cake and the crumbled material may be subjected to final drying with complete elimination of residual solvent, with or without pre-washing.

The minimum time required for dissolution of the polymer associated with the aluminum film of the Tetra Pack® packages was also verified, for this the residue of these packages with the already removed cellulose was submitted to kerosene solubilization and kept at 100 ° C. Using tweezers, pieces of film measuring approximately 30mm x 30mm were immersed in the heated solvent and proceeding with slight movement were removed after different time intervals: 2, 4, 6, 8, 10, up to 20 seconds. Each individual piece, immediately after emergence of the heated kerosene, was then immersed in another Becker glass containing cold petroleum ether.

A procedure that aimed to rinse, that is, to remove the residual solution that possibly involved the films and also facilitate the subsequent elimination at low temperature. To verify the efficiency of the dissolution process, each piece of sample was subjected to tearing. It is observed that the Aluminum / polymer film being subjected to this static procedure presents itself as a cracked aluminum film still adhered to an extended polymer film. As a result of the tests, it can be observed that even those pieces kept only for two seconds immersed in the solvent showed removal of the polymer, a fact verified by its fragility against the tear. Given this it can be stated that the time required for solubilization of the polymer is extremely short. This is due to the large area of film, associated with their reduced thickness. However, to ensure that all polymer is removed it is convenient to keep the material submerged for a longer time, especially to ensure the dissolution of thicker layers present, as in the case gluing regions where film overlap occurs. . It is also important that the lids are removed at the disintegration stage of the enclosures, as if present at the dissolution stage, they will require a much longer heating time. However, if not removed, they will accompany the aluminum and should be mechanically removed from the mixture aluminum foil and caps via sieving or screening. Agitation is also of fundamental importance to favor the diffusion of the solvent and also to facilitate the disintegration of the residues, which, due to the previous process, are kneaded and aggregated.

[066] Briefly the new process brings the following novelties: [067] 1. Use of polymer dissolution with a solvent of the low and medium boiling alkane family, therefore of lower molecular weight, preferably paraffinic point hydrocarbons. boiling less than 100 ° C, preferably from 60 to 120 ° C. Exemplary in this new process kerosene may be employed, but operating at only 100 ° C, well below its boiling temperature, and well below its boiling point. glow, having low flammability advantage at this temperature. Following cold removal of the residual kerozene by washing with low boiling hydrocarbon which will eventually be easily eliminated. These hydrocarbons easily interact with the large polymer chain, favoring, due to reduced chain size, rapid interaction and consequent polymer dissolution, since, due to their short chain length, they easily enter and diffuse between the polymer chain, and being of a similar structure, it hardly interferes with its breaking, with only Van der Walls breaking forces;

[068] 2. Operation at temperatures well below the polymer melt temperature which is approximately 190 ° C, thus operating at a temperature close to softening which is about 125 ° C and no operation is required. under pressure. This new feature also has the advantage, in subsequent operation, easy elimination and consequent recovery of the solvent employed when subjected to atmospheric pressure;

[069] 3. Separation of Polymer Aluminum from Polymer / Aluminum rich residue by dissolving the polymer in recirculating solvent, with polymer concentration in the solution during its residence time;

[070] 4. Separation of polymer and solvent from concentrated polymer rich solution to obtain reusable polymer and recycled solvent in the process itself;

[071] 5. For the disposal of the dissolving solvent residue in aluminum, the scrubbing solvent chosen from low boiling hydrocarbons in their preferred form is the hydrocarbon fraction in the distillation range of commercial hexane, or petroleum ether. or alternatively ethanol 96 GL.

[072] 6. Process requires reduced dissolution time, therefore its operation is feasible continuously, which leads to the reduction of the size of the dissolutors, which can be performed either through conveyor threads, solvent-immersed conveyor belts, pumping. , associated with filtration, whether with cooling or not, if ultrafiltration is adopted, devices such as extruders whose liner wall is the filter element, or any assembly arrangement that can perform unitary operations continuously or even the combination of continuous operations with batch operations;

[073] 7. Energy optimization of the process, if the entire recovery chain is contemplated, whether it is separation of the paper, polymer and aluminum pulp, making the heat recovery between the process phases, for example gas utilization Processes such as a boiler (outlet) ~ 250 ° C for the polymer drying tower or mat after washing solvent evaporation. If aluminum melting were to be conducted, the cooling of the ingots could be carried out in a chamber whose hot cooling gases would recover heat from aluminum and could be conducted either to heat part of the solvents or even to be used for drying in general. either from the composite films after cellulose elimination, prior to entering the solubilization process, drying the spray polymer after washing solvent elimination. This is indeed feasible, since we would have hot gases with an initial temperature of 650 ° C and final could be in the range of 105 0 C;

[074] 8. Optionally solvent separation from the polymer may take place by batch distillation process, where the addition of new solvent (distillate) prior to the removal of aluminum from the dissolver, leading to the washing of aluminum, thereby removing solubilized polymer residue adhered to it. Its subsequent use as the first solvent for the next batch not only provides effective consumption of the solvent itself but also leads to greater and more efficient polymer recovery;

[075] 9. Obtaining the recovered polymer without the need for melt reprocessing to avoid longer reflow processing time;

[076] 10. Alternative solvent-forming polymer film formation through a steam-heated roller tower process, said film being or not being comminuted immediately after its formation;

[077] 11. Alternative polymer isolation contained in solution by injection of pre-concentrated solution, rotating disc and a spray dryer chamber; and Obtaining the precipitated polymer by incorporating a second solvent.

[079] For a better understanding of the present patent the following figures are attached: [080] FIGURE 1, which shows the block diagram of the process and equipment in step A of separating the cellulose from the aluminized and carton packs of the present patent.

[081] FIGURE 2, showing the block diagram of the process and equipment in their preferred form in step B of aluminum separation and isolation and of the polymer rich polymer composition contained in the aluminum / polymer mixture.

FIGURE 3, showing the block diagram of the first alternative process and equipment of aluminum separation and isolation step B.a and the polymer rich polymer composition contained in the aluminum / polymer mixture.

FIGURE 4, showing the process and equipment block diagram of the second alternative of the aluminum separation and isolation step B.a and the polymer-rich polymer composition contained in the aluminum / polymer mixture.

FIGURE 5, showing the process and equipment block diagram of the alternative of step B.d of separating the polymer from the concentrated polymer rich solution.

[085] FIGURE 6, showing the block diagram of the alternative process of performing all step B of the aluminum separation and isolation process and of the polymer rich polymer composition contained in the aluminum / polymer mixture.

[086] FIGURE 7, showing the block diagram of the process in step C in option C, of obtaining crushed polymer [087] FIGURE 8., showing the block diagram of the process in step C in option C.2 , for obtaining polymer in the form of pellets in Evaporator.

FIGURE 9, which shows the block diagram of the process in step C.3 of obtaining polymer in the form of vapor column pellets.

[089] FIGURE 10, showing the block diagram of the process in step C in option C.4, of obtaining expanded powdered polymer.

[090] FIGURE 11 showing the block diagram of the process in step C in option C.5 of obtaining polymer as a dry precipitate.

[091] For a better understanding of the process, we have established the following chain and equipment identifications: [092] ECAP - Carton, Aluminum and Plasticized Packaging [093] RME - Mechanical Shredder [094] RTS - Dirty Flaps [095] TLR - Tank Scrubber [096] CP - Perforated Baskets [097] FRS - Dust Removal Filter Set [098] SRF - Filter Set Retained Dirt [099] ARE - Recovered Water [0100] RTL - Clean Scrap [0101 ] DHP - Hidrapulper Breaker Breakdown [0102] CCF - Fixed Cylindrical Basket [0103] RPA - Polymer / Aluminum Rich Polymeric Waste [0104] PC - Pulp Pulp [0105] TTR - Tilted Rotary Drum [0106] HC - Hydrocyclones [0107] ΤΕΤ - Treadmill Conveyor [0108] AFIC - Cellulose Free Filtered Water [0109] SEC-Dryer [0110] CES - Dry Cellulose [0111] MP - Paper Machine [0112] FPA - Sheets of Paper [0113] BR - Whitener [0114] CEB - Cellulite Bleached Bone [0115] SOLV - Recovered Dissolving Solvent [0116] CAI - Inclined Rail [0117] CTL - Conveyor Belt [0118] FSPC - Concentrated Polymer Rich Solution Filter [0119] BSPC - Concentrated Polymer Solution Pump [0120] SPC - Concentrated Polymer Rich Solution [0121] FAIP - Polymer and solvent impregnated aluminum sheets [0122] CAV - Vacuum Chamber [0123] FAIS - Solvent impregnated aluminum sheets [0124] SL - Solvent Washer [ 0125] SEI - Lower Dryer [0126] COS - Solvent Condenser [0127] FA - Aluminum Sheets [0128] SOLVQ - Hot Recovered Dissolving Solvent [0129] SU - Ultrafiltration Separation [0130] PFP-Polymer in Paste Form [0131] FPL - Washing Press Filter [0132] MDS - Solvent Blend [0133] PPU - Wet Polymer Powder [0134] DSS- Single Solvent Distiller [0135] SEPO - Polymer Dryer [0136] SLR - Washing Solvent Recovered [0137] PPS - Polymer Powder Dry Dry [0138] CTL - Conveyor Belt [0139] DSPC - Solution Filter [0140] BSPC - Solution Recirculation Pump [0141] EH - Hildebrand Extractor [0142] RSTC Solution Cooling Heat Exchanger [0143] FFP - Press Filter [0144] AQS - Solvent Heater [0145] PFP - Paste Polymer [0146] TQD - Dissolution Tank [0147] CR - Reflux Condenser [0148] TSF- Siphon Term [0149] TS - Solvent Tank [0150] FL - Line Filter [0151] TCS - Solvent Condensing Tank [0152] TSD - Diluted Solution Tank [0153] SV - Vacuum System [0154] NPP - Nitrogen for Purge [0155] FIA - Aluminum Film [0156] CRS - Backflow Condenser [0157] SR - Resulting Solution [0158] VAS - Saturated Water Vapor [0159] CD1 - Condenser 1 [0160] CD2 - Condenser 2 [0161] TO - Tower or Horizontal Belt [0162] RM - Metal Rolls [0163] VA - Water Vapor [0164] TRIT - Crusher [0165] EN - Crushed Polymer [0166] SCRS Recovery System, Condenser / Separator [0167] TELS - Solvent Disposal Tank [0168] SEX - Exhaust System [0169] FUS - Spindle [0170] PP - Pellet Polymer [0171] COL - Column Distillation [0172] LG - Rotary Blade [0173] DR - Rotary Disc [0174] CSD - Spray Dryer Chamber [0175] PEP - Expanded Powder Product [0176] TPP - Precipitation Tank [0177] FIL - Polymer Filter [ 0178] TA - Water Tank [0179] PPS - Dry Precipitated Polymer [0180] TDE - Decanting Tower [0181] COND - Condenser [0182] DES A - Ethanol Distiller [0183] DESH - Dissolving Solvent Distiller [0184 ] AER - Recovered Ethanol [0185] The manufacturing process of the present invention is carried out in the following steps:. Separation of cellulose from cartoned, aluminized and plasticized packaging (ECAP), as follows: [a] Shredding of packaging to obtain shredded dirty shreds (RTS);

Washing the dirty flaps (RTS) with vigorous shaking with room temperature water and filtering the flaps, separating the dirty water, which after recirculation in closed system undergoes filtration and removal of dirt (SRF), resuming the reclaimed water (ARE) for new use in washing and clean flaps (RTL) with clean polymer / aluminum rich polymer composition are removed and taken to the disintegration step;

[0189] Ac Shear breakdown (RTL) resulting in paper pulp that as agitation disaggregates and cellulose fibers with a size and density lower than the resulting residue, further aided by the vortex formed by the agitation, pass through where it loses speed resulting in virtually cellulose-free concentrated polymer / aluminum rich polymer (RPA) residue which is directed to the drying step Ad and the pulp slurry (PC) that passes to the outside of the screen decant and is removed from the process and directed to step Ae;

[0190] Ad Waste polymer / aluminum rich polymeric composition (RPA) undergoes drying process conducted with mildly overheated water vapor, or saturated water vapor, or heated air or flue gases (waste gases). ) and once dried, the polymer / aluminum rich polymeric composition (RPA) residue proceeds to the separation and isolation of aluminum and polymer in step B;

Filtration of the pulp pulp (PC) suspension, where the pulp pulp (PC) is drained and directed to step Af and the filtrate, which is cellulose free filtered water (AFIC), returns to step Ac, constantly recirculating and feeding the breakdown; and [0192] A.f Cellulose pulp (PC) undergoes partial drying to dry cellulose (CES) or direct targeting for production of paper sheets (FPA) or bleached cellulose (CEB).

[0193] The process of step A of separating cellulose from cartoned, aluminized and plasticized (ECAP) packages is performed using the following equipment in the following sequence: [0194] EAa Mechanical shredder (RME) shredding to obtain dirty shreds (RTS) proceeding to step EAb;

[0195] E.A.b Flush Wash Tank (TLR) filtration wash with agitation, where the already ground waste is placed in perforated (CP) baskets and these are introduced into the tank (TLR) with water; the flaps are vigorously agitated with spears that direct jets of pressurized water tangentially to the center of the basket causing high flap agitation; water carrying the dirt is permeated through the basket screen (CP), and when recirculating in a closed system passes through a set of dirt removal filters (FRS) separating the return water (ARE) to the tank through said lances with the dirt retained in the filter set (SRF) being discarded and the basket (CP) containing the clean flaps (RTL) being removed and forwarded to step EAc;

[0196] EAC Clean flap breakdown (RTL) in hydrapulper-type breaker (DHP) consisting of a perforated or screened fixed cylindrical basket (CCF) located within a larger diameter propeller and knife-propelled cylindrical tank on a fixed base above the basket (CCF) with spindle and propellant within said basket, by agitation and disintegration, cellulose fibers of a size and density lower than the resulting residue, further aided by the vortex formed by agitation, pass through the screen ; As the diameter of the basket is much smaller than the diameter of the disintegrator, the pulp passing the screen loses speed and no longer suffers the effect of the vortex inside the basket, resulting in concentrated polymer / aluminum rich polymer (RPA) composition residue. practically free of cellulose which is released from the bottom of the basket (CCF) through an angled valve located at the bottom and the pulp (PC) when exiting the field of action of the propeler, is outside the screen, decant and is removed through the tank bottom valve and is directed to step EAe;

[0197] EAd Drying the polymer / aluminum rich polymeric composition (RPA) residue in an inclined rotating tilt drum (TTR) with mildly overheated water vapor, or by saturated water vapor, or heated air or exhaust gases. combustion (waste gas) in which the heating fluid is injected from the inside of the screened rotary cylinder (TTR) along its axis; once dried, the polymer / aluminum rich polymeric composition (RPA) residue proceeds to the removal of the polymer rich polymeric composition in step B;

[0198] EAe Pulp pulp (PC) filtration by directing it to a hydrocyclone (HC) assembly and then to a conveyor belt conveyor (TET), interlocked with pressing belts where the pulp (PC) is drained and directed to step EAf and the filtrate, which is cellulose-free filtered water (AFIC), returns to step EAc recirculating and constantly feeding into the breaker (DHP); and [0199] EAf Drying the pulp pulp (PC) in conventional dryer (SEC) obtaining dry pulp (CES) or directing to receive new amount of water, being dispersed and fed in paper machine (MP) for production of sheets of paper. paper (FPA) or for bleaching (BR) to obtain bleached pulp (CEB).

B. Step B: Separation and isolation of aluminum and polymer contained in the residue, polymer / aluminum rich polymer composition (RPA), as follows: [0201] Ba Dissolution of the residue polymer / aluminum rich polymer composition ( RPA) in a dissolving solvent (SOLV) of the low to medium boiling alkane family (60 to 250 ° C) associated with agitation or movement operating at a temperature of 90 to 125 ° C (in its preferred form with kerosene at 100 ° C) or alternatively operating at 90 ° C with hexane) at atmospheric pressure, with concentration of polymer in solution during residence time from 2 seconds, with drainage of concentrated polymer-rich solution (SPC) which is directed to step Bd and separating the solvent and polymer impregnated aluminum sheets (FAIP);

Washing Dissolvent Solvent Impregnated Aluminum Foils (FAIP) and Concomitant Draining to Take Concentrated Polymer Rich Solution (SPC) that is directed to step Bd and separating solvent impregnated aluminum sheets ( FAIS);

Washing aluminum foil (FAIS) with solvent washer (SL) chosen from low boiling hydrocarbons (petroleum ether) or 96 GL ethanol, with drainage to remove concentrated polymer rich solution (SPC) to step Bd and with final aluminum foil (FA) separation by drying and evaporation and subsequent solvent condensation, which resumes as the hot recovered dissolving solvent (SOLVQ) for the dissolution process, step Ba;

[0204] Bd Separation of polymer from concentrated polymer rich solution (SPC) by hot pressure filtration from 1.0 to 10 bar, with pulp-like polymer (PFP) routing for press filtration, step Be and hot recovered dissolution solvent (SOLVQ) for further dissolution operation, step Ba;

B.e. Paste filtration (PFP) by wash pressing, where most of the hot recovered dissolving solvent residual (SOLVQ) is exhausted and returns to the step Ba dissolution process and the resulting cake, with the characteristic of a crumbly wet powder is washed with low volume washer solvent (SL), chosen from low boiling hydrocarbons or 96 GL ethanol which will remove all the solvent impregnated in the paste, obtaining solvent mixture (MDS) and wet polymer powder (PPU); and Separation of the small volume solvent mixture (MDS) by distillation with return of the hot recovered dissolution solvent (SOLVQ) from the distillation bottom for further dissolution, step Ba, the recovered washer solvent (SLR) from the top of the Distillation resumes for new washing and the wet polymer powder (PPU) is dried and the final product is obtained dry polymer powder (PPS) and the residual solvent vapors are condensed and the hot recovered dissolving solvent (SOLVQ) returns to new dissolution step Ba

[0207] The process of step B of aluminum polymer separation in its preferred form is performed using the following equipment in the following sequence: [0208] EBa Dissolution of the polymer / aluminum rich polymeric composition (RPA) residue in endowed equipment of an inclined rail (CAI) in the shape of curved edge ladders, where the residue (RPA) is fed at the top and in the course through the rail, the whirling and complete dissolution of the polymer occurs and at the end of the rail the aluminum suspension in polymer solution falls onto a screened conveyor belt (CTL) where the initially drained solution recirculates through the Concentrated Polymer Rich Solution Pump (BSPC) and the Concentrated Polymer Rich Solution Filter (FSPC) and at the end draining the rich solution. concentrated polymer (SPC) which is directed to step EBd and separating the solvent and polymer impregnated aluminum sheets (FAIP);

E.B.b. Washing the impregnated aluminum foil (FAIP) following the conveyor belt (CTL) with dissolving solvent spray (SOLV) and concomitantly draining the concentrated polymer rich solution (SPC) initially by gravity and then vacuuming through a chamber vacuum (CAV) which is directed to step EBd and separating solvent impregnated aluminum sheets (FAIS);

[0210] EBc Washing aluminum foil (FAIS) following conveyor belt (CTL) with solvent washer spray (SL) with concentrated polymer-rich solution (SPC) drainage initially by gravity and then vacuum through vacuum chamber (CAV) which is directed to step EBd and separating the aluminum foils (FA) which are dried in lower drier (SEI) heated by low pressure saturated steam and the impregnated solvent is separated by evaporation and subsequent condensation on solvent condenser (COS), which resumes as the hot recovered dissolution solvent (SOLVQ) for the respective dissolution processes, step EBa;

[0211] E.B.d. Separation of the polymer solvent from the concentrated polymer-rich solution (SPC) by hot ultrafiltration under pressure of 2 to 10 bar using polymer-directed ceramic (PFP) ultrafiltration (SU) separator. for pressing filtration, step EBe and hot recovered dissolving solvent (SOLVQ) for further step dissolving step EBa;

[0212] E.B.e. Paste filtration (PFP) which proceeds for subsequent wash press filter (FPL) filter filtration, where most of the hot recovered dissolving solvent residual (SOLVQ) is exhausted and returns to the step EBa dissolution process and The resulting cake, with a crumbly powder characteristic, is washed with low volume washer solvent (SL), which removes all the solvent impregnated in the paste, obtaining separately small volume of solvent mixture (MDS) and wet polymer powder (PPU). ; and [0213] EBf Separation of small volume solvent mixture (MDS) by distillation in single solvent distiller (DSS) with return of hot recovered dissolving solvent (SOLVQ) from distiller bottom (DSS) for further dissolution, step EBa , the scrubber solvent (SLR) from the top of the distiller (DSS) resumes for new washing and the wet polymer powder (PPU) is dried in a polymer drier (SEPO) and the final polymer dry powder (PPS) product is obtained. and residual solvent vapors are condensed in solvent condenser (COS) and hot recovered dissolving solvent (SOLVQ) resumes for further dissolution, step EBa

[0214] Carrying out the process of aluminum polymer separation steps Ba in its first alternative is done using the following equipment in the following sequence: [0215] EBa1 Immersion of the residue polymer-rich polymer composition (RPA) in a conveyor belt dissolving solvent (SOLV) on a conveyor belt (CTL), stirred by movement of recirculating solvent jets through solution filter (FSPC) and solution recirculation pump (BSPC) with concentration of polymer in solution during its residence time, with drainage through the screen, by gravity of the concentrated polymer rich solution (SPC) with the solvent and polymer impregnated aluminum sheets (FAIP) emerging from the solution are retained and insulated on the screened belt (CTL).

Alternatively, performing the process of aluminum polymer separation steps Ba in its second alternative is done using the following equipment in the following sequence: [0217] EBa.2 Dissolution of the residue with polymer / aluminum rich polymer composition (RPA) ) with a Hildebrand (EH) type dissolution solvent (SOLV), with gravity drainage of the concentrated polymer rich solution (SPC) leaving the solvent and polymer impregnated aluminum sheets (FAIP) emerging from the solution.

[0218] The process of polymer separation steps Bd in their alternate form is performed using the following equipment in the following sequence: [0219] EBdl Polymer solvent separation is achieved by cooling the solution to 60 and 70 ° C in heat exchanger (RSTC) and press filter filtration (FFP) at pressures up to 1.5 bar, with the hot recovered dissolving solvent (SOLVQ) at a temperature of about 65 to 70 ° C and reheating in the heater solvent (AQS) at 100 ° C and is then reused for further dissolution, step Ba and the slurry polymer (PFP) for press filtration, step Be

Alternatively the completion of the complete aluminum polymer separation process is carried out through steps EB and EC using the following equipment and in the following process sequence: [0221] B. Step B: Obtaining Aluminum Film (FIA) separated from the polymer rich polymer solution (SPC) employing boiling point solvent in the process operating temperature range.

[0222] EBA Positioning the polymer rich aluminum / polymeric composition (RPA) residue contained in a perforated basket (CP) within a dissolution tank (TQD) so that in its position within the vessel does not touch the bottom of the even, being supported by wall supports and then the tank is closed; The tank (TQD) has two separate heating systems, both powered by saturated steam: the first system consists of a heat siphon (TSF) (so that it can operate with a large volume of solvent (boiling point in the temperature range process) in which the basket is fully immersed during the dissolution step); and the second with a steam jacket at the bottom of the tank (so that it can operate with a small volume of solvent in which the basket is fully immersed, ie above the solvent level during the aluminum wash step, operating as a soxhlet ); It is connected to a reflux condenser (CR) which has temperature and pressure and water flow control in the reflux condenser (which controls the heating steam supply as well as the reflux condenser feed water flow). and allows to control the circulation of the term siphon and the pressure inside the dissolver); and has a bottom valve (for transferring the solution to the solvent concentrator tank (TCS));

[0223] EBB Transfer of the solvent (from boiling point in the process operating temperature range) of the solvent tank (SOLV) from the solvent tank (TS) to the dissolution tank (TQD) until it masks aluminum residue / polymer rich composition. (RPA) contained in the basket (CP) and dissolution of the polymer-rich polymer composition is started by feeding water into the term siphon (TSF) connected to the dissolution tank (TQD) and heating and vaporization occurs. of the solvent within the tube bundle, which, as a result, displaces a liquid column responsible for the upward displacement of the liquid solvent and its circulation through the flaps of the polymer / aluminum-rich polymer composition residue returning to the bottom and feeding the tube bundle ( creating efficient recirculation, which favors dissolution), circulation is maintained for 5 to 15 minutes when partial evaporation occurs. the solvent which is condensed in the Reflux Condenser (CR) returning to the Tank and at the end the concentrated polymer rich polymer (SPC) solution is drained through the bottom valve and through the line filter (FL) into the concentration concentrator tank. (TCS) and proceeds to the EBF step (the high temperature of the solution during filtration makes this operation easier, as it significantly reduces its viscosity and due to the solvent ratio employed, after cooling presents as a consistent paste) ;

[0224] EBC Solvent is again transferred from the solvent tank (TS) to the dissolution tank (TQD) below the basket bottom (CP) and washing is started and water vapor is now fed. in the dissolution tank jacket, heating of the solvent contained in the bottom of the vessel, and rising of the vapors, passing through the basket, following to the reflux condenser (CR), operation is maintained at the pressure corresponding to the dissolution temperature and the Condensed solvent at a temperature just below the saturation temperature percolates through the contents of the basket and which upon contact with the rising stream of vapors absorbs heat and so that when heated down over the flaps, they wash away the residual composition solution. polymer-rich polymeric material that still surrounds the aluminum, and said solution is then transferred to the space below the basket base for complete and continuous washing of the aluminum and finally, with the aid of internal pressure, the diluted polymer rich polymer composition (SPD) solution is transferred through the tank side valve (TQD) to the dilute solution tank (TSD) containing its own reflux condenser, positioned above the tank (TQD) which will feed a new filler of polymer / aluminum rich polymeric composition residue, complemented by new or recovered solvent;

[0225] EBD Once all liquid solvent has been transferred from the dissolution tank (TQD), after washing and the bottom outlet of the dissolution tank (TQD) is closed, the vacuum is initially proceeded through the vacuum system (SV). which directs the steam to the reflux condenser (CR) and from it to the atmosphere and the steam tank is kept warm in the jacket and following a residual vapor purge operation contained in the dissolution tank which is entrained by a heated purge nitrogen (NPP) stream to reflux condenser (CR) and from this to the atmosphere;

[0226] EBE Then the dissolution tank (TQD) is opened, the basket (CP) is removed and after removal of the polymer-rich polymer composition-free aluminum film (FIA) pieces, it is taken back to step EAb and the recovered aluminum is directed for processing in a casting and casting or other step;

EBF The concentrated polymer rich polymer composition (SPC) solution contained in the solvent concentrator tank (TCS) is heated to distill part of the solvent and the vapors are fed to the transferring reflux condenser (CRS). the hot recovered dissolution solvent (SOLVQ) into the solvent stock tank (TES) that feeds the dissolution tank (TQD) to give the resulting solution (SR) containing higher viscosity polymer rich polymer composition and can then be shipped for step EBG or for steps Cla, C.2.a, C.3.a C.4.a or C.5.a; and [0228] EBG The resulting solution (SR) containing the higher viscosity polymer rich polymer composition from which the solvent has been partially removed is subjected to saturated water vapor (VAS) dragging, which is performed at the temperature near the temperature. softening of the polymer rich polymeric composition and employing saturated direct steam in this operation (resulting in the most intense and efficient solvent removal, as vapor enthalpy is elevated in this condition) and indirect steam with injected vapor temperature at tank shell (TCS) kept close to that of the injected saturated vapor (Since the vessel is kept in this operation at atmospheric pressure and the operating temperature is greater than the boiling temperature of the solvent, almost all of it is eliminated); water and solvent) from this operation goes to a condenser, where the condensed water is drained and the solvent vapors m at the top of this first condenser (CD1), it passes to a second condenser (CD2) where solvent condensation occurs, following, still hot, to the solvent stock tank (TES) which feeds the solvent dissolution tank (TQD) hot recovered dissolution (SOLVQ) (storage of the still heated solvent means energy saving in the process); This step has its solvent elimination control adjusted for different recovery processes of the polymer rich polymer solution (SPC) as regards its final form; in the form of film, powder or pellets.

[0229] C. Step C: Obtaining Polymer for Reuse: [0230] EC 1 In the form of shredded film [0231] ECla The resulting solution (SR) containing the highest viscosity polymer rich composition is fed into a Tower or Belt. Horizontal (TO) at a slightly lower temperature than the extraction due to pressure reduction or at the same temperature if the same extraction pressure is maintained through holes between Teflon-coated metal rollers (RM) operating as calender and are heated entirely with water vapor (VA) (in this operation a thin polymer film is formed which favors high contact area, allowing effective removal of solvent), the film when moving is kept in contact with a current saturated vapor, which ensures complete elimination of the solvent;

[0232] E.C.l.b The solvent proceeds to the recovery system, condenser / water separator (SCRS), where the solvent (SOLVQ) and water (WATER) are recovered separately; and [0233] E.C.l.c The produced film taken at the bottom of the Tower or at the end of the Belt may then be conveyed to a Crusher (TRIT) to obtain crushed polymer (PT).

[0234] C.2 In the form of evaporator pellets [0235] EC2.a The resulting solution (SR) containing higher viscosity polymer rich polymer composition is kept in the solvent elimination tank (TELS) and is made by maintaining The temperature in the polymer softening range is achieved, which is achieved by keeping the vessel pressure under control to prevent mass expansion, so that solvent elimination (SOLVQ) is effected in an exhaust system (SEX). ), until its complete exhaustion (as the temperature is kept in the softening range of the polymer it can be extruded directly below the tank); and [0236] EC2.b At the bottom of the tank is a helical spindle (FUS) or gear pump that extrudes molten mass through the orifice, from which the noodle-shaped fillets are cooled and cut into small shapes. pellets (PP);

[0237] C.3 In the form of vapor column pellets [0238] EC3.a The resulting solution (SR) containing higher viscosity polymer rich polymer composition from which part of the solvent has been removed is fed by a pump. positive displacement (for example, through a screw or gear pump), which leads the viscous mass through holes installed in the top of a Column (COL), in which overheated steam rises against the holes just below them , the noodle-shaped fillets are immediately cut by a disk-shaped rotating blade (LG); The small pellets fall through the steam stream, during the fall they are cooled through the second stage of the column with saturated steam jets at a temperature of 100 ° C and collected in a hopper then onto a conveyor where they are cooled with water; and [0239] E.C.3.b Solvent / water vapors flow to recovery system, condenser / water separator (SCRS), solvent collection (SOLVQ) and water (WATER).

[0240] C.4 In the form of expanded powder [0241] EC4.a The resulting solution (SR) containing higher viscosity polymer rich polymer composition is still injected hot and under pressure through orifice or rotary disc (DR) interconnected to a parallel saturated vapor stream (VAS) in a cyclone-shaped spray dryer (CSD) chamber, where the expanded powder product stream falls through the lower cyclone opening; and [0242] E.C.4.b The gaseous stream flows to the recovery system, condenser / water separator (SCRS) for solvent collection (SOLVQ) and water (WATER).

[0243] C.5 In the form of a precipitate [0244] EC5.a The resulting solution (SR) containing higher viscosity polymer rich polymer composition is cooled and precipitated in Ethanol (AE) under stirring and indirect cooling in Precipitation (TPP);

[0245] E.C.5.b The precipitated polymer is filtered off (FIL), separating the obtained powder, then transferred to a Water Tank (RT) where solvents will be removed;

[0246] EC5.CO solvent is removed using direct water vapor (VA) heating, entrained solvent vapors are directed to a Condenser (COND) and then to a Decantation Tank (TDE) to proceed. the separation of the immiscible phase and the supernatant solvent;

[0247] EC5.d The aqueous phase is subjected to distillation to recover the recovered ethanol (AER) dissolved in distillator (DESA), and the organic phase, which contains the greatest amount of dissolving solvent, is further distilled off ( DESH), recovering from this mixture, the dissolving solvent (SOLVQ) and also some partitioned ethanol in equilibrium with the phase equilibrium dissolving solvent; and [0248] E.C.5.e The resulting polymer is filtered, filtered (FIL), and dried in a conventional drier (SEC) to obtain the dry precipitated polymer (PPS).

In the case of packaging made only of paperless aluminized polymer films containing polypropylene and polyethylene, the same procedures as for steps B and C (post pulp extraction) are followed, ie recovery of polymer / aluminum residue as in previous case is similar with the only difference being the operating temperature. If conducted up to 100 ° C, only polyethylene dissolves and polypropylene is insoluble. In this condition, the solution is filtered hot and the undissolved solid components, polypropylene and aluminum are conducted after washing with petroleum ether and subsequently with ethanol, dispersed in a liquid to a low shredder crushing system. , kind of blind blender. Said liquid may be, for example ethanol. In this condition, the aluminum will be crushed leaving the PP larger, thus allowing easy separation by sieve filtration.

[0250] The process can still be optimized with regard to energy if it contemplates the entire recovery chain, whether it is separation of paper, polymer and aluminum pulp, making heat recovery between all process phases, eg utilization of boiler gases (Chimney) output ~ 250 ° C to the polymer drying tower or conveyor after washing solvent evaporation. If aluminum melting were conducted, the cooling of the ingots could be performed in a chamber whose hot cooling gases would recover heat from aluminum and could be conducted either to heat part of the solvents or even to be used for general drying. either from the composite films after cellulose elimination, prior to entering the solubilization process, drying the spray polymer after washing solvent elimination. This is indeed feasible as we would have hot gases with an initial temperature of 650 ° C and an end temperature of 105 ° C.

Claims (16)

1. “PROCESS FOR RECYCLING THROUGH SEPARATION OF THE CONSTITUENTS OF ALUMINIZED AND PLASTICATED CARTON PACKAGING”, characterized by the following sequence: A. Separation of cellulose from carton, aluminized and plasticized packaging (ECAP), as follows: A. Shredding of packaging obtaining shredded dirty shreds (RTS); Ab Washing dirty flaps (RTS) with vigorous shaking with room temperature water and filtering the flaps, separating the dirty water, which after recirculation in closed system undergoes filtration and removal of dirt (SRF), recovering the recovered water ( ARE) for further use in washing and the clean flaps (RTL) with clean polymer / aluminum rich polymeric composition are removed and taken to the disintegration step; Ac Shear breakdown (RTL) resulting from paper pulp that as the agitation occurs disaggregates and the cellulose fibers with size and density lower than the resulting residue, further aided by the vortex formed by the agitation, pass through a screen where loses velocity resulting in practically cellulose-free concentrated polymer / aluminum (RPA) rich polymeric composition residue that is directed to the drying step Ad and the pulp slurry (PC) that passes to the outside of the screen, decants and is removed from the process and directed to step Ae; Ad The polymer / aluminum rich polymeric composition (RPA) residue undergoes a drying process conducted with mildly overheated water vapor, or saturated water vapor, or heated air or flue gas and once dried, polymer / aluminum rich polymeric composition (RPA) residue proceeds for separation and isolation of aluminum and polymer in step B; Filtration of the pulp pulp (PC) suspension, where the pulp pulp (PC) is drained and directed to step Af and the filtrate, which is cellulose free filtered water (AFIC), returns to step Ac, recirculating and constantly nourishing the breakdown; and A. f Cellulose pulp (PC) undergoes partial drying to dry cellulose (CES) or direct direction for production of paper sheets (FPA) or bleached cellulose (CEB); and B. Step B: Separation and isolation of aluminum and polymer contained in the residue, polymer / aluminum rich polymer composition (RPA), with the following sequence: Ba Dissolution of the residue polymer / aluminum rich polymer composition (RPA) in a solvent of the low to medium boiling alkane family (SOLV) associated with agitation or movement at a temperature of 90 to 125 ° C at atmospheric pressure, with concentration of the polymer in the solution during its residence time from 2 seconds, draining the concentrated polymer rich solution (SPC) which is directed to step Bd and separating the solvent and polymer impregnated aluminum sheets (FAIP); Bb Washing Dissolvent Solvent Impregnated Aluminum Sheets (FAIP) and Concomitant Draining to Take Concentrated Polymer Rich Solution (SPC) that is directed to Step Bd and Separating Solvent Impregnated Aluminum Sheets (FAIS) ; Washing aluminum foil (FAIS) with scrubbing solvent (SL) chosen from low boiling hydrocarbons, with drainage to remove concentrated polymer rich solution (SPC) for step Bd and with final separation of aluminum foil ( FA) by drying and evaporation and subsequent condensation of the solvent, which resumes as the hot recovered dissolving solvent (SOLVQ) for the dissolving process, step Ba; Bd Separation of the polymer from the concentrated polymer-rich solution (SPC) by hot pressure filtration from 1.0 to 10 bar, with slurry polymer (PFP) routing for press filtration, step B and solvent hot recovered dissolution (SOLVQ) for further dissolution operation, step Ba; B.e. Paste filtration (PFP) by wash pressing, where most of the hot recovered dissolving solvent residual (SOLVQ) is exhausted and returns to the step Ba dissolution process and the resulting cake, with the characteristic of a crumbly wet powder is washed with low volume washer solvent (SL), chosen from low boiling hydrocarbons or 96 GL ethanol which will remove all the solvent impregnated in the paste, obtaining solvent mixture (MDS) and wet polymer powder (PPU); and Bf Separation of small volume solvent mixture (MDS) by distillation with return of hot recovered dissolution solvent (SOLVQ) from distillation bottom for further dissolution, step Ba, recovered scrubbing solvent (SLR) from top of distillation returns to rinsing and the wet polymer powder (PPU) is dried and the final product dry polymer powder (PPS) is obtained and the residual solvent vapors are condensed and the hot recovered dissolving solvent (SOLVQ) is resumed for further dissolution, step Ba 2. "PROCESS FOR RECYCLING THROUGH SEPARATION OF THE CONSTITUENTS OF ALUMINIZED CARD PACKAGED PACKAGING" according to claim 1, characterized in that the dissolving solvent (SOLV) is preferably boiling paraffin hydrocarbons in the range from 60 to 250 ° C. 3. The process for recycling by separating the constituents of aluminum and plasticized carton packs according to claims 1 and 2, characterized in that the dissolving solvent (SOLV) is kerozene. 4. The process for recycling by separating the constituents of aluminum and plasticized carton packs according to claims 1 and 2, characterized in that the dissolving solvent (SOLV) is alternatively hexane. 5. The process for recycling by separating the constituents of aluminum and plasticized carton packs according to claim 1, characterized in that dissolution takes place at temperatures of 90 to 110 ° C, well below the flowable temperature of the polymer at temperatures close to polymer softening. 6. The process for recycling by separating the constituents of aluminum and plasticized carton packs according to claim 1, characterized in that the scrubbing solvent (SL) is preferably petroleum ether. 7. Recycling process by separating the constituents of aluminum and plasticized carton packs according to Claim 1, characterized in that the washer solvent (SL) is alternatively ethanol 96 GL. Recycling process by separating the constituents of aluminum and plasticized carton packs according to claim 1, characterized in that the process of step B of aluminum polymer separation in its preferred form is carried out using the following equipment: EBa Dissolution of the residue Polymer / aluminum-rich polymeric composition (RPA) on equipment with a curved-edged stairway inclined rail (CAI), where the waste (RPA) is fed at the top and in the course. through the chute occurs the whirling and complete dissolution of the polymer and at the end of the chute the aluminum suspension in polymer solution falls on a conveyor belt (CTL) where the initially drained solution recirculates through the Concentrated Polymer Rich Solution Pump (BSPC). ) and the Concentrated Polymer Rich Solution Filter (FSPC) and at the end draining the concentrated polymer rich solution (SPC) which is directed to step E.B.d and separating the solvent and polymer impregnated aluminum sheets (FAIP); E.B.b. Washing the impregnated aluminum foil (FAIP) following the conveyor belt (CTL) with dissolving solvent spray (SOLV) and concomitantly draining the concentrated polymer rich solution (SPC) initially by gravity and then vacuuming through a chamber vacuum (CAV) which is directed to step EBd and separating solvent impregnated aluminum sheets (FAIS); EBc Washing aluminum foil (FAIS) following conveyor belt (CTL) with solvent washer spray (SL) with concentrated polymer-rich solution (SPC) draining initially by gravity and then vacuuming through a vacuum chamber (CAV) which is directed to step EBd and separating the aluminum foil (FA) which is dried in lower dryer (SEI) heated by low pressure saturated steam and the impregnated solvent is separated by evaporation and subsequent condensation in solvent condenser. (COS), which resumes as the hot recovered dissolution solvent (SOLVQ) for the respective dissolution processes, step EBa; E.B.d. Separation of the polymer solvent from the concentrated polymer rich solution (SPC) by hot ultrafiltration under pressure of 2 to 10 bars using ultrafiltration separator (SU) with slurry polymer (PFP) routing to pressing filtration, step EBe and hot recovered dissolving solvent (SOLVQ) for further step dissolving step EBa; E.B.e. Paste filtration (PFP) which proceeds for subsequent wash press filter (FPL) filter filtration, where most of the hot recovered dissolving solvent residual (SOLVQ) is exhausted and returns to the step EBa dissolution process and The resulting cake, with a crumbly powder characteristic, is washed with low volume washer solvent (SL), which removes all the solvent impregnated in the paste, obtaining separately small volume of solvent mixture (MDS) and wet polymer powder (PPU). ; and EBf Separation of the small volume of solvent mixture (MDS) by distillation in single solvent distiller (DSS) with return of hot recovered dissolving solvent (SOLVQ) from distiller bottom (DSS) for further dissolution, step EBa, solvent The Top Distiller (DSS) Recovered Washer (SLR) resumes for rewashing and the Wet Polymer Powder (PPU) is dried in a Polymer Dryer (SEPO) and the final polymer dry product (PPS) and vapors are obtained. of residual solvent are condensed in solvent condenser (COS) and hot recovered dissolving solvent (SOLVQ) resumes for further dissolution, step EBa 9. "Process for recycling through separation of the constituents of aluminum and plasticized carton packs" according to Claim 1, characterized in that the process of step Ba of aluminum polymer separation in its first alternative is carried out using the following: equipment in the following sequence: EBa Immersion of the polymer / aluminum-rich polymeric composition (RPA) residue in a conveyor belt (CTL) dissolving solvent (SOLV) with recirculating solvent jet stirring through solution filter (FSPC) and water pump lower solution recirculation (BSPC) with polymer concentration in the solution during its residence time, with drainage through the screen, by gravity of the concentrated polymer rich solution (SPC) leaving the solvent and polymer impregnated aluminum sheets (FAIP) at emerging from the solution are retained and isolated over the screened belt (CTL). 10. A process for recycling by separating the constituents of aluminum and plasticized carton packs according to claim 1, wherein the process of step Ba of polymer separation of aluminum in its second alternative is carried out using the following: equipment in the following sequence: EBa.2 Dissolution of the polymer / aluminum rich polymer (RPA) residue with a Hildebrand (EH) type dissolution solvent (SOL) with gravity drainage of the concentrated polymer rich solution (SPC) ) leaving the polymer and solvent impregnated aluminum sheets (FAIP) emerging from the solution. A process for recycling by separating the constituents of aluminum and plasticized carton packs according to claim 1, wherein the process of step Bd of aluminum polymer separation in its alternative form is carried out using the following: EBdl Polymer solvent separation is achieved by cooling the solution to 60 and 70 ° C in a heat exchanger (RSTC) and by press filter filtration (FFP) at pressures up to 1.5 bar with the hot recovered dissolving solvent (SOLVQ) at a temperature of about 65 to 70 ° C and undergoing reheating in the solvent heater (AQS) to 100 ° C and continuing to be reused in further dissolving operation, step Ba and the polymer in the Paste (PFP) for pressing filtration, step Be Alternatively the completion of the complete process of aluminum polymer separation step B is done using the following equipment in the following sequence: 12. "PROCESS FOR RECYCLING THROUGH SEPARATION OF THE CONSTITUENTS OF ALUMINIZED CARD PACKAGED PACKAGING", characterized in that the complete process of separation of polymer from aluminum in its alternative form is carried out, through the steps EB and EC using the following equipment in the following sequence : B. Step B: Obtaining Aluminum Film (FIA) Separated from Polymer Rich Polymer Solution (SPC): EB .A Positioning Polymer / Aluminum Rich Polymer Composition (RPA) Residue and Contained in Perforated Basket (CP) inside a dissolution tank (TQD) so that in its position inside the vessel does not touch the end of the vessel, it is supported by wall supports and then the tank is closed; The tank (TQD) has two separate heating systems, both fed with saturated steam: the first system consists of a term siphon (TSF) (so that it can operate with a large volume of solvent in which the basket is fully immersed when of the dissolution stage); and the second with a steam jacket at the end of the tank; is connected to a reflux condenser (CR) that has temperature and pressure control and water flow in the condenser; and has an end valve; EBB Dissolve solvent (SOLV) in the range 90 to 100 ° C from solvent tank (TS) to dissolution tank (TQD) to cover aluminum residue / polymer-rich polymer composition (RPA) contained in the basket (CP ) and dissolution of the polymer-rich polymer composition is started by feeding water into the term siphon (TSF) connected to the dissolution tank (TQD), and heating and vaporization of the solvent within the tube bundle occurs. as a result, it displaces a liquid column responsible for the upward displacement of the liquid solvent and its circulation through the flaps of the polymer / aluminum-rich polymeric composition residue returning to the bottom and feeding the tube bundle; circulation is maintained for 5 to 15 minutes when partial evaporation of the solvent which is condensed in the Reflux Condenser (CR) occurs, returning to the tank and at the end the polymeric solution is drained concentrated polymer (SPC) through the bottom valve and through the line filter (FL) to the solvent concentrator tank (TCS) and proceeds to step E.B.F; EBC The solvent is again transferred from the solvent tank (TS) to the dissolution tank (TQD) below the basket bottom (CP) and washing is started and water vapor is now fed into the jacket. dissolution tank, heating of the solvent contained in the bottom of the vessel, and rising of the vapors, passing through the basket, following to the reflux condenser (CR), operation is maintained at the pressure corresponding to the dissolution temperature and the condensed solvent in the temperature just below the saturation temperature percolates through the contents of the basket and which upon contact with the rising stream of vapors absorbs heat and so that when heated down over the flaps they wash away the residual of solution rich in polymeric composition. polymers that still surround the aluminum, and said solution is then transferred to the space below the base of the basket, obtaining complete and continuous washing of the aluminum and finally then, with the aid of internal pressure, the diluted polymer rich polymeric composition (SPD) solution is transferred through the tank side valve (TQD) to the dilute solution tank (TSD) containing its own reflux condenser, positioned above the tank (TQD) which will feed a new filler of polymer / aluminum rich polymeric composition residue, complemented by new or recovered solvent; EBD Once all liquid solvent from the dissolution tank (TQD) is transferred, after washing and the bottom outlet of the dissolution tank (TQD) is closed, the vacuum is initially proceeded through a vacuum system (SV) directing the vapor to the reflux condenser (CR) and from it to the atmosphere and the steam tank is heated in the jacket and following a residual vapors purge operation contained in the dissolution tank which are entrained by a stream of nitrogen heated purge (NPP) to reflux condenser (CR) and thereto into the atmosphere; EBE Then the dissolution tank (TQD) is opened, the basket (CP) is removed and after removal of the polymer-rich polymer composition-free aluminum film (FA) pieces, it returns to step EAb and the recovered aluminum is directed for processing in a casting and casting machine or other step; EBF The concentrated polymer rich polymer (SPC) solution in the solvent concentrator tank (TCS) is heated to distill part of the solvent and the vapors are fed to the reflux condenser (CRS) which transfers the solvent from hot recovered dissolution (SOLVQ) into the solvent stock tank (TES) that feeds the dissolution tank (TQD) to give the resulting solution (SR) containing the higher viscosity polymer rich composition and can then be sent to step EBG or for steps Cla, C.2.a, C.3.a C.4.a or C.5.a; and EBG The resulting solution (SR) containing the higher viscosity polymer-rich polymer composition from which the solvent was partially removed is subjected to saturated water vapor (VAS) dragging, which is performed at the temperature near the softening temperature of the solvent. polymer rich composition and using this operation saturated direct steam and indirect steam with tank jacket injected steam temperature (TCS) maintained close to that of the injected saturated steam, the vapor stream from this operation flows to a condenser, where the condensed water is drained and the solvent vapors come out on top of this first condenser (CD1), it goes to a second condenser (CD2) where the solvent condensation occurs, following, still hot, to the solvent stock tank (TES) that feeds the dissolution tank (TQD) with hot recovered dissolving solvent (SOLVQ) (storage of the still heated solvent means economical energy in the process); This step has its solvent elimination control adjusted for different recovery processes of the polymer rich polymer solution (SPC) as regards its final form; in the form of film, powder or pellets; and C. Step C: Obtaining Polymer for Reuse: EC 1 In the form of ECla shredded film The resulting solution (SR) containing higher viscosity polymer rich polymer composition is fed into a Tower or Horizontal Belt (TO) at a temperature slightly lower than that of extraction due to pressure reduction or at the same temperature if the same extraction pressure is maintained through holes between Teflon-coated metal rollers (RM) operating as a calender and which are heated entirely with water vapor ( VA), the moving film is kept in contact with a saturated vapor stream, which guarantees total solvent elimination; E.C.l.b The solvent proceeds to the recovery system, condenser / water separator (SCRS), where solvent (SOLVQ) and water (WATER) are recovered separately; and E.C.l.c The produced film taken at the bottom of the Tower or at the end of the Belt may then be conveyed to a Crusher (TRIT) to obtain crushed polymer (PT). 13. "PROCESS FOR RECYCLING THROUGH SEPARATION OF ALUMINIZED AND PLASTICATED CARTON PACKAGING CONSTITUENTS" according to Claim 11, characterized in that the process of step EC is carried out in its first alternative form using the following equipment in the following sequence: C .2 In the form of pellets in EC2.a evaporator The resulting solution (SR) containing higher viscosity polymer rich polymer composition is maintained in the solvent elimination tank (TELS) and is maintained by maintaining the temperature in the range of softening of the polymer, which is achieved by keeping the vessel pressure under control in order to prevent mass expansion, so that solvent removal (SOLVQ) is carried out in an exhaust system (SEX) until it is completely exhausted ( as the temperature is kept in the softening range of the polymer it can be extruded directly below the tank); and EC2.b At the bottom of the tank is a helical spindle (FUS) or gear pump that extrudes molten mass through the orifice, from which the noodle-shaped fillets are cooled and cut into small pellets (PP). ). 14. "PROCESS FOR RECYCLING THROUGH SEPARATION OF THE CONSTITUENTS OF ALUMINIZED AND PLASTICATED CARTON PACKAGING" according to claim 11, characterized in that the process of step EC is carried out in its second alternative form using the following equipment in the following sequence: C .3 In the form of an EC3 vapor column pellet. The resulting solution (SR) containing the higher viscosity polymer rich polymer composition from which part of the solvent has been removed is fed by a positive displacement pump which leads to viscous mass through holes installed at the top of a Column (COL), in which overheated steam rises against the holes just below them, the noodle-shaped fillets are immediately cut by a rotating blade (LG) disco; the small pellets fall through the steam stream, during the fall they are cooled through the second stage of the column with saturated steam jets at a temperature of 100 ° C and collected in a hopper then onto a mat where they are cooled with water; and E.C.3.b Solvent / water vapors flow into the recovery system, condenser / water separator (SCRS), solvent collection (SOLVQ) and water (WATER). 15. PROCESS FOR RECYCLING THROUGH SEPARATION OF ALUMINIZED AND PLASTICATED CARTON PACKAGING CONSTITUENTS ”according to Claim 11, characterized in that the process of step EC in its third alternative form is carried out using the following equipment in the following sequence: C .4 In the form of an expanded powder EC4.a The resulting solution (SR) containing higher viscosity polymer rich polymeric composition is further injected under hot and pressure pressure through orifice or rotary disc (DR) in a parallel stream of vapor. saturated (VAS) in a cyclone-shaped spray dryer (CSD) chamber, where the expanded powder product stream falls through the lower cyclone opening; and E.C.4.b The gaseous stream flows to the recovery system, condenser / water separator (SCRS) for solvent collection (SOLVQ) and water (WATER). 16. "PROCESS FOR RECYCLING THROUGH THE SEPARATION OF THE CONSTITUENTS OF ALUMINIZED AND PLASTICATED CARTON PACKAGING" according to claim 11, characterized in that the process of step EC in its fourth alternative form is carried out using the following equipment in the following sequence: C .5 In precipitate form EC5.a The resulting solution (SR) containing higher viscosity polymer rich polymer composition is cooled and precipitated in Ethanol (AE) under agitation and indirectly cooled in Precipitation Tank (TPP); E.C.5.b The precipitated polymer is filtered off (FIL), separating the obtained powder, then transferred to a Water Tank (RT) where solvents will be removed; EC5.CO solvent is removed using direct water vapor (VA) heating, entrained solvent vapors are directed to a Condenser (COND) and then to a Decantation Tank (TDE) to separate the immiscible phase and the supernatant Solvent; EC5.d The aqueous phase is subjected to distillation for recovery of recovered ethanol (AER) dissolved in distillate (DESA), and the organic phase, which contains the greatest amount of dissolving solvent, is further distilled into distillate (DESH), recovering from this mixture the dissolving solvent (SOLVQ) and also some partitioned ethanol in equilibrium with the phase equilibrium dissolving solvent; and E.C.5.e. The resulting polymer is filtered, filtered (FIL), and dried in a conventional drier (SEC), obtaining the dry precipitated polymer (PPS).