EA040731B1 - WASTE RECYCLING METHOD BY SEPARATING ALUMINIZED AND PLASTIC COMPONENTS OF CARDBOARD OR OTHER PACKAGING AND NECESSARY EQUIPMENT - Google Patents

Description

It refers to this patented process for the recycling and disposal of waste, in particular plastic, aluminum, cardboard or other packaging, using a method and equipment to extract and separate the main components present in the package, to recycle waste and prevent environmental pollution, which allows reuse the constituent components of the waste: plastic, aluminum and paper in their original form, resulting in an excellent quality polymer from the waste, insulated aluminum can be obtained by melting and refining in the usual way, i.e. collection of aluminum cans and other pieces of aluminum, or alternatively, this scrap can be used as a raw material for the production of aluminum derivatives such as salts, organic aluminum or even aluminum pigment, an easily digestible and cheap solvent can be brought to the market, with low energy consumption pulp can be re-manufactured into cardboard for making boxes, and it can even be sent to a subsequent clarification process - when recycling waste, the investment in the raw material process is small, and we also get the best price / quality ratio.

To do this, you need to have an idea about the technical means used in the processing industry for waste disposal, in particular, packaging. Technologies currently in use are recovering pulp from cardboard boxes, plastic and aluminum packaging, which is destined for paper making. As for the use of the rest of the packaging, the aluminium/polymer is simply crushed and injection molded into product parts such as hairs on floor brushes, hot pressed into corrugated sheets, and many other products. Thus, bare aluminum is not used as an expensive raw material. Recycling processes are also known that use pyrolysis to further generate electricity, and then we have liquid and / or gaseous fuels at the output. However, this process, which produces fuel, requires a lot of energy, energy is provided by burning part of the waste itself, since a rather strong endothermic reaction occurs during the pyrolysis process.

Speaking of packaging, it is important to note that this is actually a paper/aluminum/polymer sandwich in which the polymer component has a softening point of 125°C and a pour point of 190°C, and consists almost entirely of polymer, which contains in its composition of a compatibilizer, which contributes to better adhesion of low-density polyethylene to aluminum. Functionalized polyolefins such as ethylene copolymer and acrylic or methacrylic acid are commonly used for this function. These compounds, in turn, improve the compatibility of material recovered from 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.

According to queries made in national and international patent databases, the following discoveries have been found.

Spanish patent PI 2383208 Procedures for the processing of materials containing aluminum compounds discloses a process that recovers cellulose by mechanically separating packages and waste, and accordingly leads to the recovery of aluminum.

In this process, polyethylene is destroyed, it turns into paraffin and gases. To carry out this operation, plasma is used, which, in addition to leading to the destruction of the polymer, also requires a large amount of energy for its operation, since working with plasma requires a high temperature of the order of 15000 ° C, as well as the need to work in an inerted atmosphere which means high cost.

Some patents use solvents to recover plastic from cartons: Brazilian patent PI 0202303-2 A method for separating multilayer films intended for packaging uses various solvents, including tetrahydrofuran, xylene, toluene, carbon tetrachloride, organic acids, water, acetone and chloroform; Chinese Patent CN 1554691 A method for separating aluminum sheet and plastic in a film left over from plastic packages containing aluminum uses solvents such as tetrahydrofuran, tetralin, in addition to adding glacial acetic acid, a component that converts aluminum into salt; and Korean Patent KR 20010016352 discloses a process that promotes reaction in the presence of alcohols such as methanol, ethanol, propanol or butanol with salts in the form of chlorides such as mercury chloride, calcium chloride, aluminum chloride, magnesium chloride, potassium chloride, or even hydrochloric acid.

These processes use mostly highly toxic and carcinogenic solvents and reagents, in addition to presenting a great potential for polymer degradation, bound or unbound, they react with aluminum, converting it into a salt, which leads not only to a large the consumption of reagents, but also it does not allow the complete recovery of aluminum in its original metallic form.

Other patents disclose other separation methods, such as Brazilian patent PI0006641-9 A surfactant solution used in the plastics processing process for

- 1 040731 purification and separation of aluminum, which uses a surfactant and formic acid to remove the polymer film, operating in the range from 85°C to 198°C. However, the presence of acid under the conditions described above leads to a partial consumption of the aluminum present in the waste.

Other patents also disclose processes that release aluminum through a chemical reaction, usually using bases or strong acids:

Brazilian patent PI 0706115-3 Processing of multi-layer packaging uses sodium hydroxide solution in the same way as US patent US 5127958 Cleaning of metal surfaces of polymeric substrates.

Chinese patent CN 102532592 Aluminum-plastic separating agents and the corresponding preparation method, in turn, uses 5 to 50% acid with an unidentified organic solvent in an amount of 25 to 50%. In the same way, Japanese patent JP 20040327047 discloses the separation of polymers by density difference in a glycol solution, as well as the attack of aluminum with a sodium hydroxide solution.

It should be noted that in processes that use acids or bases, these reagents are consumed in sufficient quantities, which increases the cost of the process, but in the case of complete or partial consumption of aluminum, there are economic losses that result in a lower cost product.

US Pat. No. 7,598,297, in order to cover other possible processes, comprehensively describes the whole range of solvents, as well as the use of a strong base such as sodium or lead hydroxide. The same is true for a wide temperature range. However, he insists on using only xylene, which works at different temperatures so that the various polymers that occur in said type of packaging can be selectively removed, however, the use of a strong base leads, of course, to the consumption of aluminum.

European patent EP 0568791 discloses maps for any solvent of completely different nature, for example, derivatives of petroleum (aliphatic, aromatic, naphthenic), halogenated compounds and mixtures thereof, and also uses a wide temperature range from 40 to 500 ° C, trying to obtain exclusive rights on any of the processes. However, when carrying out the process of separating the components of the package, using the package in its composite form - paper, aluminum and polymer, of course, in addition to the indicated wide range, this leads to a high consumption of solvent in the process. This method also uses, among other forms of application, bringing a solution containing various polymers dissolved in solvents to a thermal cracking process operating in the range of 650-1200 ° C and a pressure of 0.1 to 0.3 MPa.

The processes mentioned above have the following technical problems, which have been solved with the method currently in use.

1. Some modern processes do not restore all components to their more expensive state. The method currently in use recovers all components in a quality suitable for reuse.

2. Some processes consume a lot of energy in smelting a mixture of aluminum and polymer, also causing the polymer to decompose. The presently used method produces a solvent-only separation.

3. Some processes require a complex and costly operation to separate the aluminum from the polymer. The method currently in use produces a solvent-only separation in operations that involve low investment and low raw material costs.

4. Some processes use toxic solvents that are difficult to use in separation and processing. The method currently used uses inexpensive solvents that are abundant on the market, non-toxic, fully recyclable and low energy consumption.

The processes discussed earlier have the following disadvantages, disadvantages, and limitations:

a) some modern processes do not restore all components to a high level of their cost;

b) during some modern processes for the recovery of a polymer extracted from aluminum, other substances are involved in the process, which, in addition to not helping the recovery in any way, but also give this product a low commercial value;

c) during some processes, there is no separation of aluminum from the polymer, both components are mixed, and aluminum, as an expensive component in an isolated position, is included in the products obtained from the said mixture only as a filler;

e) certain methods release aluminum, but in this way cause it to consume a large amount of energy when using very high temperatures - a condition that leads to the formation of cracks in the polymer, which breaks down and produces a mixture of wax and volatile compounds less than the total cost of the polymer, and also requires carrying out operations in inert atmosphere,

- 2 040731 which, of course, contributes to the increase in cost;

f) use of expensive and toxic solvents;

g) high cost of investment and processing; And

h) high price/quality ratio.

The waste recycling process by separating the aluminized and plastic components of carton or other packaging and the necessary equipment was designed to eliminate all the inconveniences, shortcomings and limitations of today's processes with a method based on the use of a special solvent to dissolve the polymer at the time of extraction and separation of the main components, to reuse waste, preventing environmental pollution, to recycle the constituent components of the waste, and restore the constituent parts to their original form for reuse as plastic, aluminum and paper.

The method according to the present invention has the following advantages over existing methods:

a) using the developed process, we obtain a polymer with a quality suitable for reuse for the manufacture of products and films that can be made with this recovered product and, therefore, it can be used in the form in which it was isolated, or be blended with other pure or recovered polymer, in mixtures to which fillers, colorants or other additives may be added;

b) isolated aluminum can be involved in the process of melting and refining, as in traditional methods of processing aluminum cans and other scrap of this metal, and thus can be used as a raw material for the production of alloys, blades, inorganic compounds such as salts, aluminates , or even organic derivatives such as aluminum alkyl;

c) the invention uses a solvent that is easy to find on the market for a small price, since it is not the result of synthesis, but only a distilled petroleum fraction;

d) since the solvent, which is the petroleum fraction, is used in a small boiling range and cannot become one with the product at the end of the process, the recovery of the product becomes complete after it is fully returned to the beginning of the process. Simple distillation equipment can be used for distillation without the need for fractional distillation;

e) solvent characteristics: low boiling point, low specific heat seem to be of particular importance in relation to energy consumption, since only a small part of it is evaporated, and almost all of the solvent is processed without passing through distillation, and this significantly reduces energy consumption, since this happens through filtering;

e) the method used according to the present invention, restores the polymer, retains its physical and chemical characteristics, including compatibilizer, which facilitates the future use of waste polymer recovered in a mixture with other thermoplastics;

g) pulp can be reused in the production of cardboard, for the manufacture of boxes, can also be used in the clarification process;

h) lower investment and processing costs; And

i) low price/quality ratio.

The present method was based on the knowledge and experience of the inventor in his technical research work and previous developments on blocks consisting of paraffin and polymer used as a barrier against radiation, and then in the development of explosive compositions, in particular of the emulsion type.

Research began to address the need to recycle packaging waste to recover the polymer/aluminum contained in the waste resulting from a mechanical process that uses hydrapulper to recover cellulose from aluminized packaging.

The initial goal was to remove aluminum by dissolving, etching to obtain aluminum salts intended for use in wastewater treatment. The process has also been adjusted to produce aluminates, sulfates and aluminum chloride. The resulting polymer, after its digestion with an acid or base, and then after washing, went for further processing. However, evaluating the cost of such salts, aluminum, and comparing the flexibility in using aluminum in its metallic state (reduced), it was decided to evaluate the possibility of removing it from the metal without oxidizing it.

Based on the knowledge of the properties of the polymer, with respect to their structure and similarity to paraffin waxes, tests began on the solubility of the polymer in paraffin wax in the following sequence:

In a beaker containing 100 g of solid paraffin, subjected to melting and raising the temperature to 100°C, was added 20 g of the film containing aluminum/polymer. The temperature was raised by about

- 3 040731 up to 125°C. Stirred with a glass rod for five minutes. Then the contents of the beaker were poured into another, passing the paraffin through a metal sieve. After cooling, the contents of the sieve were washed with cold carbon tetrachloride. Knowing that cold carbon tetrachloride dissolves the paraffin, but the polymer only dissolves when heated, it can be seen that the paraffin has removed the aluminum bonded polymer. This can be checked by tearing the resulting film, which is torn without stretching, unlike plastic film, which is torn differently.

Another finding is that the wax/polymer mixture solidified at a lower temperature when heated compared to the wax alone test.

Given this, they began to think about a possible way to separate the paraffin from the polymer. A problem was encountered which proved difficult to solve as it was impossible to think of distillation or fractional solubilization because the mixture had a high molecular weight. The next step is the direct use of carbon tetrachloride. However, due to the high cost, as well as its high toxicity, its use was abandoned.

Then other chlorides were investigated, but the same problems recurred.

The next stage was to investigate aromatic solvents, chlorinated and non-chlorinated, naphthenic, as well as alcohol ethers, amyl-, methyl-, butyl acetates, etc.

In parallel, the removal of aluminum bonded to polypropylene, PET and PVC was also tested, present in various packaging such as tablet blister packs, powder packs for future soft drinks, biscuit, candy and chips packs. All of these products have positive results associated with some of the solvents tested. Some solvents have been studied more carefully, taking into account the issue of health risks, availability and their cost.

But the main goal was aluminized cardboard packaging. In this regard, tests with other wastes have been suspended, leaving this type of packaging as a priority and continuing testing.

Due to the difficulty of isolating the paraffin during use, we decided to consider using kerosene, as its structure is similar to that of solid paraffin. The results obtained using the same mass were positive. Dissolution occurred in less than 5 minutes. But there was another problem - how to remove the solvent from the polymer. The solvent should probably contain high molecular weight paraffinic compounds in small amounts, and for this it is necessary to bring the polymer to a higher temperature in order to effectively remove residual component. In addition, given the size of the chain of kerosene and paraffin, the interaction would be quite strong, and this factor prevents separation.

The next step was then separation by precipitation. The polymer/kerosene solution was presented as a mass after cooling. This mass is then introduced in equal volume into ethanol, mixing the components. The precipitated polymer is then filtered by subjecting it to successive washings with ethanol. Then it is subjected to drying and as a result a precipitated polymer is obtained.

The resulting solvent mixture is distilled to separate the kerosene from the ethanol. Given the difficulty in separating residual kerosene from the precipitated polymer by distillation, a solvent with identical characteristics to kerosene but with a lower boiling point was used.

Hexane was used because it is a more volatile solvent, the dissolution was carried out in a flask which was attached to a reflux condenser. The same ratio of solvent/precipitate was used. Dissolution occurred after five minutes.

In another experiment, petroleum ether was used, distillation range from 60°C. Difficulties in dissolution were observed because, unlike the hexane used in the above test, in this experiment the temperature reached an insufficient level for dissolution.

In the subsequent experiment, when compared to the previous experiment, the same amount of solvent/waste was placed in a steel tank, which was then closed and placed in hot water to heat. When the water bath reached the boiling point, the container that had been heated was removed and left to cool. When the tank is opened, since the contents are still slightly hot, most of the solvent evaporates from the tank, resulting in a polymer sponge. The experiment was then run under pressure to take advantage of the softening temperature of the polymer. Dissolution has occurred, the solvent is removed gradually, keeping the dissolver heated, at the same pressure and temperature, and finally, after cooling, a solid polymer is obtained.

Thus, after conducting various experiments, it was concluded that the most suitable solvent for the separation and isolation of polymer from aluminized and plastic cartons is an alkane with a low and medium boiling point, and therefore a lower molecular weight, because it interacts more easily with a large polymer chain, and due to the reduced chain length, provides rapid interaction and subsequent dissolution of the polymer, and due to the short chain length, the solvent easily penetrates between the polymer units. Also, the linear structure of the solvent is similar to the structure of the polymer, and therefore does not affect it, thus

- 4 040731 only the van der Waals forces break.

The reason why it was decided to use normal paraffinic hydrocarbons (straight chain alkanes) is because they are less toxic compounds than aromatics or even naphthenics, minimizing also the risks of polymer degradation (due to structural similarity) and also because of their easily eliminated by evaporation and/or distillation).

Experiments show the possibility of using a solvent of paraffinic hydrocarbons at a boiling point below 120°C, preferably from 60 to 100°C, the process takes place well below the melting point of the polymer, which is about 190°C, and thus it should be noted that the process takes place at a temperature below the softening temperature, about 105°C, but operation at such a high pressure is optional. Ease of dissolution and subsequent flexibility in its recovery when returned to atmospheric pressure results in a better quality of the recovered polymer. To get around the problem of the dissolution temperature, if it is below the softening temperature of the polymer, the pressure can be increased, and then there will be an ideal softening temperature for the process.

With regard to the separation of the solvent, since the boiling point was below the softening point of the polymer, when the solution left the dissolver, some of the solvent evaporated, although another new solvent (distilled) was added before removing the aluminum, which washed out the aluminum. All this was done, of course, after removing the solution containing most of the polymer. This solvent, while still hot, was used as the first solvent for the next batch, this also optimized the solvent recovery process.

The solution containing the polymer, after partial concentration due to the partial evaporation of the solvent, whose vapors were passed through the condenser, enters the next stage.

Finally, as a last experiment, the filtration method was evaluated. It is known that during ultrafiltration (emulsions, bacteria, fats and macromolecules), the working pressure range is from 1 to 10 bar, and the membrane has pores from 0.001 to 0.1 ^μ ™ Since the average molecular weight of the polymer is ~ 200,000 Da, this technique could become promising, for example, together with the possibility of rational use of energy. Use of boiler gases from a chimney at a temperature of about 250°C, such gases that they can be carried into a concentration tower or belt and the polymer can be dried. However, if aluminum fusion were performed, when the ingots were cooled, the air from the heat exchanger would exit at an initial temperature of 650°C, and the final temperature could be about 125°C, thus using energy appropriately.

First, pressure filtration of a solution containing 11% polymer dissolved using filter paper and a porous ceramic plate was tested. It was observed that the solution migrated through the pores and the more concentrated polymer remained on the paper.

In another experimental environment, the solution was cooled at room temperature and then filtered through paper using light hand pressure on the syringe equipment, and the solvent was observed to separate easily. Then the wet cake wrapped in paper was pressed with a press, and the cake began to contain a very small amount of solvent. Thus, it has become apparent that the separation process can be effectively improved, thereby saving energy, by filtering the hot solution and then subjecting the cake to compression on the filter surface. Since filter paper is used, the cake comes off very easily, then it can be crushed and subjected to final drying to completely eliminate residual solvent, with or without pre-washing.

The minimum time required for dissolution of polymer, film, adhered to aluminum film in Tetra Pack® containers was also checked, for which the waste of such packages with the cellulose already removed was subjected to dissolution in kerosene and kept at 100°C. Using tweezers, pieces of film about 30x30 mm in size were immersed in the solvent, warmed up and removed with a slight movement at various time intervals: 2, 4, 6, 8, 10, and up to 20 s. Each individual piece, immediately after being removed from the heated kerosene, was immersed in another flask containing cold petroleum ether. This is a washing procedure, that is, removing the residual solvent in which the films were, as well as facilitating their subsequent removal at low temperature. To test the effectiveness of the dissolution process, each piece was torn apart. It should be noted that the aluminum/polymer film to be subjected to this procedure is stretched, presenting itself as a cracked aluminum film, and still adhered to the stretched polymer film. As a result of the tests carried out, it can be seen that even those pieces that were kept in the solvent for only two seconds showed that it was possible to remove the polymer, and this fact is confirmed by its brittleness at break. Taking this fact into account, it can be said that the time required for the solubilization of the polymer is extremely reduced. This is due to the large area of the film and its reduced thickness. However, to ensure that all polymer is removed, it is better to keep the material immersed in the liquid for a longer time, in particular to allow the thicker layers present to dissolve, for example in the case of box seams where film is applied. It is also important that the lids are removed during the dismantling stage, as if they are involved in the dissolving stage, it will take much longer to heat up. Therefore, if they are not removed, if they are together with aluminum, then they must be removed mechanically from the aluminum foil / polymer mixture and lids, using a sieve or grid. Shaking is also important in diffusing the solvent, as well as in facilitating the disintegration of the waste which, as a result of the process described above, has already been rumpled and collected together.

In short, the new process has the following new features:

1. Dissolution of the polymer using a solvent from the alkane family with medium and low boiling points, and thus lower molecular weight, preferably paraffinic hydrocarbons with a boiling point below 100°C, preferably from 60 to 120°C. Kerosene can illustrate this new process, but it only works at 105°C, i.e. at a temperature well below its boiling point, and well below its combustion temperature, i.e. low flammability at a given temperature is an advantage. Subsequently, in the cold, remove residual kerosene by washing with a hydrocarbon with a low boiling point, and it is easily eliminated completely. These hydrocarbons easily interact with the large polymer chain, aiding, due to their small chain size, rapid interaction and subsequent dissolution of the polymer, since, due to their short chain length, it is easy for hydrocarbons to penetrate and spread between the polymer chain, and since they have a similar structure, they have almost nothing to do with breaking the chain, and only breaking the van der Waals force occurs.

2. Processing at temperatures well below the melt temperature of the polymer, which is about 190°C, thus showing that it runs at a temperature below the softening temperature, which is about 125°C, and pressure work is not necessary. This news also has the advantage, in terms of the subsequent operation, of the easy removal and subsequent recovery of the used solvent during exposure to atmospheric pressure.

3. Separation of aluminum and polymer from polymer/aluminum rich waste by dissolving the polymer in a circulating solvent with the concentration of polymer in solution throughout the residence time.

4. Separation of polymer and solvent from a solution rich in concentrated polymer, resulting in a polymer for reuse and a solvent recycled in the process itself.

5. To eliminate residual solvent in the aluminum solution, use a flushing solvent selected from low boiling point hydrocarbons in the preferred form of a hydrocarbon fraction in the distillation range of hexane or petroleum ether, or alternatively ethanol 96 GL.

6. The process requires a reduced dissolution time and hence the operation can be carried out continuously, resulting in a reduction in the size of the dissolvers and can be done either with a screw conveyor or belt conveyor immersed in solvent, pumping associated with filtration, with or without cooling , in the case of ultrafiltration by equipment such as an extruder whose wall is the filter element, or any assembly assembly that is capable of performing single operations in a continuous mode or even long-term combination operations in batches.

7. The optimization of the process in relation to energy, if we consider the entire recovery chain, will be the separation of paper pulp, aluminum and polymer, recovering heat between process phases, using gases, for example, a boiler or a chimney at a temperature of about 250 ° C for a drying tower or belt, to dry the polymer after the wash solution has evaporated. In the case of aluminum melting, the cooling of the ingot can be carried out in a chamber where the hot gases produced by the cooling would return the heat to the aluminum and could be used either to heat some of the solvents or even to dry the films as a whole after removal from the pulp. , prior to the start of the solubilization process, drying the sprayed polymer after its removal from the solvent in which it was washed. This is indeed feasible, since we would have hot gases at our disposal with an initial temperature of 650°C, and at the end the temperature could be about 105°C.

8. Optionally, separation of the polymeric solvent is done by distillation, in batches, while adding fresh solvent (distilled) before removing the aluminum from the dissolver, washing the aluminum, thereby removing the aluminum polymer residue that has attached to it. Its subsequent use as the first solvent for the next batch, not only ensures the efficient use of the solvent itself, but also results in a larger and more efficient recovery of the polymer.

9. Obtaining an isolated polymer, without the need for remelting, to avoid wasting time on the melting process.

10. Alternative to polymer film formation, with parallel solvent regeneration with

- 6 040731 By means of a process carried out in a tower with a roller heated by steam, this film can be shredded immediately or not immediately after the process of its formation.

11. An alternative to isolating the polymer contained in the solution for spraying the pre-concentrated solution onto the rotary disc and into the spray dryer type chamber; And

12. Obtaining a precipitated polymer by introducing a second solvent.

For a better understanding of the present invention, the following drawings are shown:

fig. 1, which shows a diagram of a continuous process for the processing of aluminized and plastic components of a cardboard or other packaging according to the present invention;

fig. 2, which shows a process diagram for batch recycling of aluminized and plastic components of a carton or other packaging according to the present invention;

fig. 3 which shows a schematic view of a special device for withdrawing aluminum in three operating positions;

fig. 4 which shows a diagram of the process and equipment in step A for depulping aluminized boxes according to the present invention;

fig. 5 which shows a diagram of the process and equipment in its preferred embodiment in step B for separating and isolating the aluminum and polymer composition from the polymer contained in the aluminum/polymer mixture;

fig. 6 which shows a process and equipment diagram of the first alternative step in step B to separate and isolate the aluminum and polymer composition from the polymer contained in the aluminum/polymer mixture;

fig. 7 which shows a process and equipment diagram of the second alternative step in step B for separating and isolating the aluminum and polymer composition from the polymer contained in the aluminum/polymer mixture;

fig. 8, which shows a process and equipment diagram of an alternative for step B, for separating a polymer solution from a solution containing a concentrated polymer;

fig. 9 which shows an alternative process flow diagram for the entire step B to separate and isolate the aluminum and the polymer rich polymer composition contained in the aluminum/polymer mixture; and fig. 10 which shows the process flow for step B, in option B.1, obtaining the polymer as a dry cake.

In order to better understand this process, we have established the following identifiers for connecting concepts and equipment:

A01 - film dispenser

B01 - variable feed device

B01A - continuous feeder

B 02 - slurry tank

С01 - dissolver

D01 - special screen filter

E01 - polymer waste scrubber

F01 - tank for concentrated solution

F02 - diluted solution tank

G10 - special device for aluminum production

G11-piston

G11A - cavity

G12 - casing

G12A - top hole

G12B - bottom hole

H01 - polymer dryer

101 - binding filter

J01 - solvent vapor condenser

K01 - dryer for aluminum

L01 - concentrated solution cooler

LM01 - oven

M01 - solvent heater

NO 1-device for supplying a concentrated solution

- 7 040731

N02 - solvent return device

N03 - device for supplying a concentrated solution

N04 - solvent supply device

O01 - kerosene tank

P01 - aluminum shredder

Q01 - flotation tank

R01 - sieve basket

S01 - press

T01 - circulation pump

U01 - valve

U02 - valve

V01 - return pump

X01 - solvent tank

Y01 - water drain filter

Z01 - pump for supply of washing solvent

Z02 - concentrated solution pump

Z03 - solvent pump

ECAP - cardboard, aluminized and plastic packaging

RME - mechanical grinder

RTS - contaminated waste

TLR - dirty waste washing tank

СР - perforated baskets

FRS - filters for removing impurities

SRF - pollution on filters

ARE - reclaimed water

RTL - clean waste

DHP - disassembly of waste into components in the Hidrapulper device

CCF - fixed cylindrical basket

RPA - Aluminium/Polymer Rich Waste Polymer Composition

PC - cellulose

TTR - tilted rotating drum

HC - hydrocyclones

TET - caterpillar conveyor

- 8 040731

AFIC - filtered water without cellulose content

SEC - drying

CES - dry pulp

MP - paper making machine

FPA - paper sheets

BR - bleach

CEB - bleached pulp

SOLV - recovered solvent for the dissolution process

CAI - sloped gutter

CTL Screen Conveyor Belt

FSPC - filter for solution rich in concentrated polymer

BSPC - Polymer Rich Solution Pump

SPC - solution rich in concentrated polymer

SPD - dilute polymer rich solution

FAIP - aluminum sheets impregnated with polymer and solvent

CAV - vacuum chamber

FAIS - solvent impregnated aluminum sheets

SL - solvent for flushing

SEI - bottom dryer

COS - solvent condenser

FA - aluminum sheets

SOLVQ is a reconstituted hot mortar used for dissolving

SU - separator by ultrafiltration

PFP - viscous polymer

FPL - flush filter press

MDS - solvent mixture

PPU - wet polymer powder

DSS - simple solvent distiller

SEPO - polymer dryer

SLR - rinse solvent reconstituted

PPS - dry polymer powder

CTL - sieve belt conveyor

DSPC - solution filter

- 9 040731

BSPC - solution circulation pump

EH - Hildebrand extractor

RSTC - changing the state of the solution from hot to cold

FFP - filter press

AQS - solution heater

PFP - viscous polymer

TQD - dissolution tank

CR - reflux condenser

TSF - thermosyphon

TS - solvent tank

FL - line filter

TCS - concentrated solvent tank

TSD - dilute solution tank

TES - solution storage tank

SV - vacuum system

NPP - nitrogen for purge

FIA - aluminum film

CRS - reflux condenser

SR - resulting solution

VAS - saturated water vapor

CD 1 - capacitor 1

CD2 - capacitor 2

VA - water vapor

TPP - sump

FIL - polymer filter

TA - water tank

PPS - Dry Precipitated Polymer

TDE - decanting tower

COND - capacitor

DESA - ethanol distiller

DESH - solvent distiller used in dissolution

AER - recovered ethanol

In an effort to improve the process and select additional equipment, various options have been explored and results have been obtained that summarize the optimization process.

A process for separating a carton or other package with aluminum and plastic components in a process involving separating the plastic film from polyethylene or polypropylene with aluminum by dissolving the polymer in a primary compatible solvent, a process carried out at the softening temperature of the polymer and under pressure, followed by non-dissolution by reducing temperature or by adding a secondary solvent similar to the primary solvent and not the polymer solvent, separating the solvent from the polymer and finally filtering and reusing the solvent in the solubilization phase, continuous use in the following sequence:

A) periodically feeding small pieces of film or its equivalent through the film feeder (A01), passing through a shut-off valve (U01) at the inlet to the variable feeder (B01), passing through another shut-off valve (U02) at the inlet to the constant feeder ( B01A);

B) taking a predetermined amount of film from the variable feeder (B01) with the valve (U01) closed, and with the valve (U02) open, transferring the film to the continuous feeder (B01), closing the valve (U02) and opening the valve (U01) and transferring the film from one device (A01) to another (B01), and so on;

- 10 040731

B) film is fed from the continuous feeder (B01A) using an internal threaded carrier, while the solvent is introduced into the slurry tank (B02) with a shut-off valve (U02) with a continuous volumetric supply of solvent through the solvent supply pump (Z01) in a ratio of 8 to 15 parts solvent to one part film to cover the entire film in the slurry tank (B02) and form a polymer/aluminum film slurry in the solvent;

D) feeding the slurry into a dissolver tank (C01), where the slurry is subjected to internal circulation in the form of a spiral and heated from 100 to 105° C. indirectly and with a large circulation turnover, mixing and subsequent better convection, maintaining a residence time of 2-5 seconds;

E) at the end of the dissolution, the liquid flow with a solution of polymer and aluminum in suspension enters a special screen filter (D01) driven by a screw thread, thus aluminum is filtered and a concentrated solution is separated;

E) The concentrated solution passes through the tissue walls, maintaining back pressure on the liquid as the solution exits, in order to keep the dissolver tank (C01) under pressure, and the concentrated solution is collected in the tank (F01) and aluminum with residual polymer is pushed through the filter threads ( D01) to another adjacent compartment, to the polymer waste washing tank (E01) and the pipe will no longer allow it to pass through, and using a different speed, the aluminum is moved to a special device (G01) to remove aluminum from the system;

G) The filtered and condensed solvent from the solvent tank (X01) is injected into the waste polymer washing tank (E01) through the inside of the tank screw thread axis (E01) to remove the remaining polymer solution in aluminum, and the diluted solution passes through a sieve, keeping at there is back pressure in the liquid at the outlet of the solution to keep the dissolver tank (C01) pressurized and the solution is collected in the dilute solution tank (F02);

H) The concentrated solution, after reaching the desired regime, is collected in the concentrated solution tank (F01) and continuously pumped using the concentrated solution pump (Z02) to cool from 50 to 70 ° C, initially in the heat recovery compartment (LM01), to give some heat to the filtered and condensed solvent; in addition to the concentrated solution cooling compartment (L01) to precipitate and reduce the solubility of the polymer, then proceed to filtration in the viscous polymer filter. (I01), from where the filtered solvent is collected together with the solvent from the condenser (J01) in the solvent tank (X01) and returned through the furnace (LM01), through the solvent pump (Z03), through the solvent heater (M01) and through the screw shaft tank threads for washing polymer waste (E01);

i) The dilute solution obtained by washing the aluminum in the polymer waste scrubber (E01) is collected in the dilute solution tank (F02), and then the continuous process is restarted by supplying the washing solvent through the supply pump (Z01);

K) the cake after filtering enters the polymer dryer (H01) and the solvent vapor enters the condenser (J01), and the condensed solvent is combined with the condensed solvent from the aluminum dryer (K01);

K) all solvent vapor chains, after condensation, go to the solvent tank (X01), and they are reused for aluminum purification and from there they again fall into the beginning of the whole process;

M) aluminum is removed intermittently through a special aluminum exit device (G10) with its periodic opening and closing, circular and reciprocating vertical movement to also keep the pressure inside the dissolve tank (C01), and the aluminum from which the polymer was removed is transported to drying in the dryer (K01), separating from the solvent vapors, which follows the condenser (J01), combining with the condensed solvent from the polymer dryer (H01);

H) dry aluminum, containing small amounts of both cellulose fiber and pieces of plastic caps, and polypropylene tapes, in each batch is fed into the grinding tank (P01), then room temperature kerosene is added and grinding is carried out by cutting into pieces, not only removing residual polymer, but also freeing residual cellulose fibers;

O) in this way, the stirring mode is switched off and the aluminum slurry is transferred to the flotation tank (Q01), air is sprayed through the device contained at the bottom of the grinding tank (P01), foam is formed, which contains fibers, pieces of polypropylene tapes and cellulose fibers;

P) this foam is continuously removed by draining the liquid supernatant stream, which passes through a sieve basket (R01), where the lighter polypropylene particles and fibers are retained, then returning the kerosene to the tank by pumping with a circulation pump (T01) through its bottom; And

P) aluminum slurry after removal of impurities is drained through the filter (Y01), kerosene is pumped by the reverse pump (V01) and returned to the kerosene tank (O01), which will provide the next batch, and aluminum follows for pressing on the press filter (S01) for removal most

- 11 040731 kerosene, and the next step is melting, where the remaining kerosene evaporates.

Alternatively, the periodically optimized process can be run with the following modified steps:

A) feeding small pieces of film or its equivalent intermittently through the film dispensing device (A01) through a shut-off valve (U01) at the inlet to the intermittent feeder (B01) and then through another shut-off valve (U02) at the inlet to the slurry tank (B02) ;

B) after closing the valve (U01) between the film dispenser (A01) and the intermittent feeder (B01), the film is dispensed together with the solvent supply to the slurry tank (B02) and during each such feed to the intermittent feeder (B01), the valve (U02) between it and the suspension tank (B02) remains closed;

C) intermittent volumetric supply of a concentrated solution through a strong solution supply device (N01) and a solvent for washing through a solvent return device (N02), performed through a positive bias, the first is valid only before entering the mode, in a ratio of 8 to 15 parts of solvent to one piece of film to cover the entire film in the slurry tank (B02) and form a polymer/aluminum film slurry in the solvent;

D) the concentrated solution, after reaching the regime, is collected in the concentrated solution tank (F01) and transferred periodically using the concentrated solution supply device (N03) for cooling from 50 to 70 ° C, initially in an oven (LM01) to obtain filtered and concentrated solvent heat and an additional concentrated solution are cooled in a cooler (L01) to precipitate and reduce the solubility of the polymer, and then proceed to filtration in a viscous polymer filter (I01), in which the filtered solvent accumulates, together with the solvent from the condenser (J01) in the tank for the solvent (X01), and periodically it is returned through the furnace (LM01), by means of the solvent supply device (N04) through the solvent heater (M01) and through the screw thread axis of the waste resin disposal tank (E01); And

E) The dilute solution obtained by purifying aluminum in the waste polymer washing tank (E01) is collected in the dilute solution tank (F02), and then the continuous process is restarted by backfeeding the solution (N02).

To conduct a continuous recycling process by separating the components of plastic and aluminized, carton and non-carton packaging, the following equipment was used: a volumetric film feeder (A01) with a rotary valve, either a screw conveyor or a belt conveyor; an intermittent feeder (B01) of cylindrical shape and a conical bottom located between the continuous feeder (B01A) and the film feeder (A01) and an inlet diaphragm type blocking valve (U01); continuous feeder (B01A) of cylindrical shape and conical bottom with an internal screw conveyor, with a blocking valve (U02) of the diaphragm type at the inlet and a tangential abutment of the solvent supply; a dissolver tank (C01) having a cylindrical section and with a heating jacket; inside it, along its vertical section, there is a fixed spiral with a circular cross section; a special filter (D01) of a conical shape and with a conical screw thread is installed on the screen wall and a check valve at the outlet to the tank for a concentrated solution (F01), which interacts with the tank for washing polymeric waste (E01), through an air duct leading to another compartment; a tank for washing polymeric waste (E01) with a cylindrical configuration of the channel and with a large cross section, and inside of which there is a cylindrical screw thread with perforation on its axis and a check valve at the outlet to the dilute solution tank (F02); tank for concentrated solution (F01); dilute solution tank (F02); a special aluminum release device (G10) rotating and pulsating with a piston (G11) that moves inside a cylindrical shell (G12) with a top hole (G12) that keeps the system under pressure and a bottom hole (G12B) located at the bottom, away from of the upper part and slightly larger than the height of the upper hole and is deflected by 180 degrees from the first hole and interacts with the external environment, the piston (G11) has a cavity (G11A) of a semi-cylindrical shape with an internal cutout inclined at an angle of 45 degrees, and at the top it is limited three sealing rings above and three more equidistant rings below, located at a distance slightly greater than the corresponding height of the cavity; polymer dryer (H01) screw conveyor type with indirect heating; dryer for aluminum (K01) screw conveyor type with indirect heating jacket; concentrated solution cooler (L01) heat exchanger type; viscous polymer filter (I01) under continuous or semi-continuous pressure; solvent tank (X01); solvent vapor condenser (J01) heat exchanger type; oven (LM01) type heat exchanger; flushing solvent pump (Z01); concentrated solution pump (Z02); solvent pump (Z03); kerosene tank (O01); aluminum shredder (P01) of cylindrical type with sharp knives and baffles; flotation tank (Q01) with an elongated cylindrical shape and an air sprinkler located at the bottom of the tank; sieve basket (R01); press (S01) piston type; circulation pump (T01); return pump (V01); and drain filter (Y01) basket type.

In order to carry out intermittent processing by separating the aluminized or plastic components of a carton or other packaging, the following alternative equipment can be used to replace any function: a cylindrical slurry tank (B02) with a conical bottom located between the intermittent feeder (B01) and dissolver tank (C01); a concentrated solution feeder (N01) and a solvent return feeder (N02), positive displacement, piston type or piston pump type.

For the case of separation of the components of aluminized and plastic packaging, where the aluminum is isolated in the form of a pigment, the same previous steps will be used, but the aluminum isolation step should be carried out by filtering and washing the aluminum with elements having tightly closed ceramic pores, performed at the dissolution temperature , and then the filtrate is cooled after the polymer precipitation step, which is re-filtered by the porous element in the viscous polymer filter I01).

In the specific case of processing aluminized and plastic carton packaging, the method according to the present invention has the following steps:

A. Stage A: separation of pulp from cardboard, aluminized and plastic packaging in the following sequence:

A.a. Inspection of shredded packaging waste for contamination.

A.b. Rinse the dirty pieces of waste by intensive mixing with water at room temperature, preserving the pieces of packaging that are separated from the dirty water, which, after circulating in a closed system, passes through filtration and removal of impurities, becoming purified water for reuse for washing, and clean pieces of packaging with polymer polymer/aluminum rich composition are cleaned, set aside and sent to the dismantling stage.

A.s. Waste sorting, cutting the mass and getting paper, then mixing and disintegration of the raw material takes place, and cellulose fibers with smaller sizes and lower density remain in the resulting residue, which, with the help of an automated vortex formed during mixing, are passed through a sieve, and then the speed is lost, resulting in a rich polymeric composition of concentrated polymer/aluminum waste, substantially free of cellulose, which is sent to the drying stage A.d. and separating the slurry from the pulp that passes on the outside of the sieve, then decanted, removed from the process and sent to stage A.e.

A.d. The waste polymer composition rich in polymer/aluminum is subjected to a drying process carried out indirectly with slightly superheated steam or saturated steam, or directly with heated air or combustion gases (gases supplied) and after drying the waste polymer composition with high polymer/aluminum content is followed to isolate and isolate the aluminum and polymer in the B stage.

A.e. Filtration of the cellulose pulp slurry, where the cellulose pulp is drained and sent to step A.f. and the filtrate, i.e. the filtered, cellulose-free water returns to the A.e stage, circulating and helping to sort out the waste.

A.f. The cellulose pulp is subjected to partial drying, as a result we get dry cellulose or send it to the production of paper sheets or bleached cellulose.

The execution of the process of stage A - the separation of cellulose from cardboard, aluminized and plastic packaging occurs using the following equipment in the following sequence:

E.A.a. Shredding of the packaging in a mechanical shredder, resulting in dirty waste, which follows the E.A.b.

E.A.L. Washing waste with filtration in the washing tank, actively mixing, pre-shredded waste is in perforated baskets, and the baskets are placed inside the tank filled with water; the waste is actively mixed with peaks, which direct under pressure jets of water tangentially into the basket, towards the center, causing a strong movement of the waste; water with dirt particles passes through the sieve of the basket, and, circulating in a closed system, passes through a set of filters to remove contaminants, returning water to the tank through the peaks, and the dirt is retained on a set of disposable filters, and clean waste is in the baskets, which are taken out and sent to stage E.A.s.

E.A.s. Desegregation of clean waste in a hidrapulper type apparatus, consisting of a fixed cylindrical perforated basket or sifter located on the inside of a cylindrical vessel with a large diameter, and a propeller with blades in the form of knives located on a fixed base above the basket with an axle and a propeller inside this basket, by mixing and desegregating cellulose fibers with smaller dimensions and lower density in the resulting residue, which, using an automated vortex generated during mixing, are passed through a sieve; since the diameter of the basket is smaller than the diameter of the grinder, the cellulose as it passes through the sieve slows down and no longer uses the effect of the vortex inside the basket with the resulting waste polymer composition rich in polymer / aluminum, a concentrate practically free of cellulose, which is released from the bottom of the container with the help of an angle the valve located in the lower part, and the cellulose pulp, when leaving the area of influence of the propeller, is on the outer side of the sieve, then it is decanted and removed from the process through the lower valve

- 13 040731 tank and send it to the stage E.A.e.

E.A.d. Waste polymer composition rich in polymer / aluminum is subjected to a drying process carried out in a rotating inclined drum with slightly superheated steam or saturated steam, or with heated air or combustion gases (gases are supplied), when the heating liquid is sprayed from sieves of a rotating cylinder along its axis, and after drying, the waste polymer composition with a high content of polymer / aluminum follows to isolate the composition rich in polymer to stage B.

E.A.e. When filtering the pulp, it is directed first to a set of hydrocyclones, and then to a sieve of a belt conveyor combined with press chains, where the pulp is drained and sent to the E.A.f. stage, and the filtrate, i.e. cellulose-free filtered water, EAC, returns to the E.A.c stage, circulating and continuously assisting in the grinding process; And

E.A.f. Drying the pulp in a conventional dryer to produce dry pulp, or a shot of water is sprayed onto the pulp and fed to a paper machine to produce sheets, or to be bleached in bleach, thereby producing bleached pulp.

B. Step B: separating and isolating the aluminum and the polymer contained in the polymer/aluminum rich polymer composition waste in the following sequence:

V.a. Dissolving the polymer/aluminum-rich waste polymer composition in a low to medium boiling point (60 to 250° C.) alkane family dissolution solvent, preferably hexane, and alternatively kerosene or mineral oil, in combination with agitation or vigorous movement at a temperature of 100 to 105°C (preferably with kerosene at 100°C) with a polymer concentration in solution for a residence time of 2 s, to drain the solution rich in concentrated polymer, which is directed to stage B, and the separation of aluminum sheets impregnated with polymer and solvent.

V. b. Washing the solvent impregnated aluminum sheets followed by draining to remove the solution rich in concentrated polymer which is directed to the B.d. stage and separating the solvent impregnated aluminum sheets.

V.s. Washing of aluminum sheets with a special solvent from the low boiling alkane family (petroleum ether) or ethanol 96 GL, the most solvent solvent, by draining to remove a solution rich in concentrated polymer in stage B.d. and finally separating the aluminum foil by drying and evaporating, and then condensing the solvent, which is returned hot and recovered, used in the dissolution process, to step B.a.

b.d. The separation of the solvent from the polymer is carried out by cooling the solution from 50 to 70°C, and the separation of the polymer from the solution rich in concentrated polymer is carried out using hot filtration under a pressure of 1.0 to 10 bar, then the concentrated polymer in a viscous form is sent to increase the concentration mass through the subsequent filtration stage, stage B, and through the hot reconstituted solution used for dissolution, for a new dissolution process, stage B.a.

W.e. Filtration with mass washing under pressure, where most of the residual hot recovered solvent intended for dissolution is drained and returned to the dissolution process, i.e. stage B.a., and get a cake with the characteristics of a crumbly wet powder, impregnated with a solvent for the dissolution process.

B, f. If the wash solvent is not the same as the solvent for the dissolution process, the filter cake is washed with a small volume of wash solvent selected from low boiling alkanes, preferably hexane or ethanol 96 GL, which removes most of the solvent absorbed into the cake , resulting in a mixture of solvents and a wet polymer powder, and all this goes to stage B.i.

B.g. Separation of a small volume of the solvent mixture by distillation and return of the recovered hot solvent from the bottom of the distillation column for re-dissolution in the B.a. step, the recovered wash solvent from the top of the distillation column is returned for a new wash.

B.h. If the solvent to be dissolved has a low boiling point, the impregnated cake is a wet polymer powder with no traces of the high boiling point solvent; And

B.i. The wet polymer powder is dried and the final product is a dried polymer powder, the residual solvent vapors are condensed and the reconstituted hot solution for the dissolution process is returned for a new dissolution, step B.a.

The execution of the process of stage B, the separation of the polymer from aluminum in its preferred form, is carried out using the following equipment in the following sequence:

E.V. A. Dissolution of waste polymer composition rich in polymer / aluminum in equipment equipped with an inclined trough in the form of steps with lower curved surfaces, where from

- 14 040731 passages are fed at the top and at the transition through the chute, turbulence and complete dissolution of the polymer occur, and at the end of the chute, the aluminum suspension in the polymer solution falls into the sieve of the belt conveyor, where the initially drained solution circulates through a pump for a solution rich in concentrated polymer, and a filter for a solution rich in concentrated polymer, and at the end it is drained with a solution rich in concentrated polymer, which is sent to the E.B.d. stage, separating the aluminum sheets impregnated with polymer and solvent.

E.V. b. Washing of aluminum sheets impregnated on a conveyor belt with a solvent spray used for the dissolution process, and concomitant drainage with a solution rich in concentrated polymer, initially by gravity and then by vacuum through a vacuum chamber, is directed to stage E.B.d. and separating the solvent impregnated aluminum sheets.

E.B.c Washing of aluminum sheets impregnated on a conveyor belt with a solvent spray used for the dissolution process, and concomitant drainage with a solution rich in concentrated polymer, initially by gravity and then by vacuum through a vacuum chamber, is aimed at stage E.B.d. and separating the aluminum sheets, which are dried in the lower dryer, heated with low pressure saturated steam, and the absorbed solvent is removed by evaporation and subsequent condensation in the solvent condenser, which returns the solvent as a hot and reduced solvent used in the dissolution process for the corresponding process dissolution stage E.V.a.

E.B.d. Separation of polymer solvent from a solution rich in concentrated polymer using hot ultrafiltration at a pressure of 2 to 10 bar, using a ceramic separator for this purpose, redirecting the polymer in a viscous state after cooling for filtration by pressing, the E.B.e stage and redirecting the hot reduced solvent for use in the dissolution process for the new dissolution process, E.V.a.

E.V. e. When filtering the composition, which follows the subsequent filtration with a filter press with washing, where most of the residual recovered hot solvent used for the dissolution process is drained and returned to the dissolution process to the E.B.a. stage, and the resulting cake, with loose powder characteristics, washed with a reduced volume of solvent for washing, which removes all the solvent absorbed into the suspension, and the result is a separate small volume of solvent mixture and wet polymer powder; And

E.B.f. Separation of a small volume of solvent mixture by distillation in a simple solvent still, with hot recovered solvent returned for use in the dissolution process from the bottom of the distiller, for re-dissolution, E.V.A. stage, the recovered solvent for washing from the top of the distiller is returned for a new washings, and the wet polymer powder is dried in a polymer dryer, and the final product is obtained as a dry polymer powder, and the residual solvent vapor is collected in a solvent condenser, and the hot recovered solvent used in the dissolution process is returned to a new dissolution stage, stage E. V.a.

The implementation of stages B.a of the process of separating the polymer from aluminum in its first alternative is carried out using the following equipment in the following sequence:

E.V. a.1. Immersion of waste resin composition rich in polymer/aluminum in the solvent used in the dissolution process into the sieve of the belt conveyor with vigorous agitation, the solvent jets circulate behind the solvent filter and solution circulation pump, in which the concentration of polymer in solution is lower during the residence time , and the drainage of the saturated solution enriched with the concentrated polymer through the sieve under the action of gravity, and the aluminum sheets impregnated with the polymer and the solvent pulled out of the solution are kept insulated on the tape.

Implementation of V.a. the process of separating the polymer from aluminum in its second alternative is carried out using the following equipment in the following sequence:

E.V. a.2. Dissolution of waste resin composition enriched with polymer/aluminum in the solvent used for the dissolution process in a Hildebrand type extractor, with gravity drainage with a solution enriched with concentrated polymer, and aluminum sheets impregnated with polymer and solvent as it exits the solution.

Implementation of B.d. The process of separating the polymer in its alternative form is carried out using the following equipment in the following sequence:

E.B.d.1. The separation of the solvent from the polymer is obtained by cooling the solution to 50-70°C in a heat exchanger and filtering with a press filter at a pressure of up to 1.5 bar, with hot recovered solvent used for the dissolution process at a temperature of approximately 5070°C, by reheating in a solvent heater at 100°C and can be reused in a new dissolution process, step B.a. and stages B.e. for the filtration process by

- 15 040731 compressing the polymer in a viscous form.

As an alternative, a complete separation of the polymer from aluminum is obtained by using the E.B and E.C stages, as well as the following equipment and the following process sequence:

B. Stage B: obtaining an aluminum film separated from a polymer solution with a high polymer content, using a solvent and a boiling point in the operating temperature range of the process.

EVE. Waste polymer composition enriched with polymer/aluminum is contained in a perforated basket inside the dissolution tank in such a way that in its position inside the tank the basket does not come into contact with its bottom, but is supported by holders in the walls of the tank, and then the tank is closed; the tank has two separate heating systems, both supplied with saturated steam: the first system consists of a thermosiphon (in order to be able to handle large volumes of solvent (boiling point is within the process temperature), into which the basket is completely immersed when the stage is dissolution); and a second system with a steam jacket at the bottom of the tank (in order to be able to work with a small volume of solvent from where the basket protrudes, i.e. above the solvent level, in the aluminum washing stage, works like a Soxhlet); this is connected to the reflux condenser, which controls the temperature, pressure and water flow, (which controls the supply of heating steam, as well as the reflux water supply rate and allows you to control the circulation of the thermosyphon and the pressure inside the dissolver); and has a bottom valve (for transferring the solution to a tank in which the solvent is collected).

E.V.V. Transferring the solvent used for the dissolution process (its boiling point is within the operating temperature range of the process) from the solvent tank to the dissolution tank to cover the polymer composition waste rich in polymer/aluminum contained in the basket, and starts the dissolution process of the polymer composition with high By supplying water vapor to the thermosyphon connected to the dissolution tank, heating occurs and the solvent inside the pipes evaporates, which, therefore, moves the liquid column responsible for the upward movement of the liquid solvent and its circulation through the pieces of waste polymer composition enriched with polymer / aluminum returning back to the bottom and feeding it back into the tube bundle (creating an efficient circulation system, i.e. this is an effect that promotes dissolution); remains in circulation for 1-5 minutes when partial evaporation of the solvent occurs, which is collected in a reflux cooler, returning to the tank, and ultimately drained by a polymer composition solution enriched with concentrated polymer through the bottom valve and passing through a mains filter into a tank collecting solvent and proceeds to step E.B.F. (The high temperature of the solution during filtration simplifies this process, since it significantly reduces the viscosity and, due to the action of the solvent used, has the consistency of a paste after cooling).

E.V.S. The solvent is transferred once more from the solvent tank to the dissolution tank at a level below the bottom of the basket, and flushing is started by introducing water vapor to the shell of the dissolution tank, the solvent contained at the bottom of the vessel is heated, and the vapors are understood and pass through the basket, following to the return fridge; the process is maintained at a pressure corresponding to the dissolution temperature and the solvent, condensed at a temperature slightly below the saturation temperature, seeps through the contents of the basket, and when in contact with the rising steam, absorbs heat, and the steam remains heated when lowered over the waste, washing the waste of the polymer composition, enriched with polymer, these wastes additionally include aluminum, this solution must then be transferred to the space located below the base of the basket, obtaining a complete and continuous washing of aluminum; and finally, it is transferred by internal pressure, the dilute solution containing the polymer composition rich in polymer, through the side valve of the tank, to the dilute solution tank, containing its own reflux condenser, located above the tank, to feed a new batch of waste polymer composition with high polymer/aluminum content supplemented with fresh or reconstituted solvent.

E.B.D. After all the liquid solvent has moved out of the dissolver after flushing and the outlet at the bottom of the dissolver has closed, the vacuum procedure begins using the vacuum system, directing the steam to a reflux condenser, and from there to the atmosphere, and keeps the tank heated with steam on the jacket, and then proceeds to the operation of purging the residual vapors contained in the dissolver, which are entrained in the nitrogen stream for purging the reflux condenser, and from there to the atmosphere.

E.V.E. Then the dissolver is opened, the basket is removed, and after removing the pieces of aluminum film free of the polymer-rich polymer composition, we return to the E.A.b stage, and the recovered aluminum is sent for processing in a melting furnace, for casting, or another stage.

E.B.F. A solution containing a polymer composition enriched with a concentrated polymer contained in a tank where the solvent is collected is subjected to heating for distillation

- 16 040731 part of the solvent, and the vapors are sent to a reflux condenser, which transfers the hot recovered solvent, intended for the dissolution process, to the solvent storage tank, which supplies the dissolver, obtaining a final solution containing a polymer composition enriched with a higher viscosity polymer, and it can then be directed to the E.B.G stage. or steps C.1.a, C.2.a, C.3.a C.4.a or C.5.a; And

E.B.G. The resulting solution containing a polymer composition enriched with a high viscosity polymer, from which the solvent has been partially removed, is subjected to transfer using saturated steam, the process takes place at a temperature close to the softening temperature of the polymer composition enriched in polymer and using saturated steam in this operation (in In this situation, the solvent removal is more intense and efficient, since the steam enthalpy is increased in this state) and indirect steam at the temperature of the steam is injected into the shell of the tank, which is next to the injected saturated steam (since the vessel is supported in this operation by atmospheric pressure, and the working temperature is higher than the boiling point of the solvent, practically all of it is removed), the vapor stream (water and solvent) from this operation moves to the condenser, where the water is condensed and drained, and the solvent vapor exits the top of this first condenser, passes to the second another condenser, where the solvent condenses, which follows, while still hot, to the solvent storage tank, which feeds back to the dissolver the hot recovered solvent used in the dissolution process (the solvent storage still heated indicates energy savings in the process); this step controls the removal of the solvent, tuned to various processes for the recovery of a solution of a polymer composition with a high polymer content, in relation to its final form; in the form of a film, powder or granules.

C. Step C: obtaining a polymer for reuse.

C.1. in the form of sediment.

E.C.l.a. The resulting solution containing the high viscosity polymer enriched polymer composition is cooled and precipitated in ethanol with stirring and cooling in an indirect settler.

E.C.l.b. The precipitated polymer is filtered in a filter, the resulting powder is separated, then transferred to a tank with water, where the removal of solvents will follow.

E.C.1.c. The solvent is removed by direct heating with water vapor, the resulting solvent vapor is sent to a condenser and then to a settling tank to separate the supernatant phase and the immiscible solvent.

E.C.1.d. The aqueous phase is a distillation to recover the ethanol dissolved in the distiller, and the organic phase, which contains more solvent for the dissolution process, and all this goes to the subsequent distillation in the distiller, recovering from this mixture, the solvent for dissolution, as well as a small the amount of ethanol, and distributes in balance with the solvent to dissolve in phase equilibrium; And

E.C.1.e. The obtained polymer is filtered in a filter and dried in a conventional dryer, and a dried precipitated polymer is obtained.

In the case of containers containing only aluminized polymer films, without paper and not containing polypropylene and polyethylene, the same procedures of steps B and C (after pulp extraction) should be followed, i.e. recovery of residual polymer / aluminum, similar to the previous case, only with a difference in operating temperature. If it is brought to 100°C, then only polyethylene dissolves, and polypropylene remains undissolved. In this state, the hot solution is filtered and brings with it the solids of the undissolved components, polypropylene and aluminum, after washing with petroleum ether and then ethanol, they are dispersed in the liquid by grinding into small pieces, in a kind of blind blender. The liquid may be, for example, ethanol. In this state, the aluminum is pulverized, leaving a larger PP, thus allowing it to be easily separated by sieve filtration.

The process can be further optimized in terms of energy if the entire recovery chain is considered, whether it is the separation of paper pulp, polymer and aluminum, heat recovery at all stages of the process, for example, the use of boiler gases (in the chimney), an output of ~ 250 ° C for a dryer towers or belts for polymer drying, after evaporation of the solvent to wash the polymer. In the case of the aluminum melting process, the cooling of the ingot can be carried out in a chamber in which the hot gases resulting from cooling would recover the heat of the aluminum, then it can be passed either to heat some of the solvents, or used for drying in general, for example, for films, obtained after the removal of cellulose, before starting the solubilization process, drying the polymer with the composition sprayed onto it, after removing the washing solvent. This is possible because we will have hot gases at our disposal with an initial temperature of 650°C, and at the end the temperature can reach 105°C.

Claims (7)

1. A process for the continuous recycling of waste by separating the aluminized and plastic components of a cardboard or other packaging, characterized by the separation of the components of a plastic film made of polyethylene or polypropylene with aluminum by dissolving the polymer in a primary polymer-compatible solvent with a short C5-C7 polymer chain, under pressure at a temperature below polymer softening temperature, followed by precipitation due to temperature decrease, separation of the primary solvent from the polymer, and finally filtration and reuse of the primary solvent in the solubilization step in the following sequence: A) small pieces of film or film equivalents are fed intermittently by means of a feed dispenser (A01) through a stop valve (U01) into an intermittent feed unit (B01), and from there through a stop valve (U02) into a continuous feed unit (B01A), wherein the predetermined amount of film is fed from the intermittent raw material supply device (B01) to the continuous raw material supply device (B01A) with the valve (U01) closed and the valve (U02) open, and after the transfer is completed, the valve (U02) is closed, and the valve (U01 ) reopen; B) From the feedstock continuous feeder (B01A) with shut-off valve (U02), the feedstock is fed into the slurry tank (B02) by means of an internal screw conveyor under the condition that a highly dilute polymer solution is simultaneously continuously fed through the feed pump (Z01), while the polymer solution fed in a ratio of 8 to 15 parts to one part of the raw material to cover it completely in the slurry tank (B02) to form a polymer film/aluminum slurry in the solvent; C) from the tank (B02), the suspension is fed into the dissolver (C01), in which the suspension is subjected to active mixing for 2-5 s by moving along a spiral ramp placed in it and subject to maintaining the temperature in the range of 100 to 105 ° C by indirect heating; D) then a liquid stream consisting of a polymer solution and suspended aluminum is fed into a screen filter (D01) driven by a screw conveyor, while separating aluminum to form a concentrated polymer solution; at the same time, the concentrated polymer solution passes through the walls of the screen, providing back pressure for the dissolver tank (C01) and enters the tank for the concentrated polymer solution (F01), and aluminum with residual polymer enters the polymer waste scrubber using the filter screw conveyor (D01) (E01) for further separation of the polymer, the pipe connecting the screen filter (D01) and the polymer waste scrubber (E01) prevents its further advancement, and the separated aluminum enters the device for extracting aluminum from the system (G10) at a different speed; E) to remove polymer residues, the filtered and condensed solvent from the primary solvent tank (X01) is injected through intermediate devices into the scrubber (E01) through a nozzle made inside a spiral element fixedly placed in the scrubber, after which the resulting dilute polymer solution enters the dilute solution tank polymer (F02) and passing through the screen creates a back pressure in the dissolver tank (C01); F) the concentrated polymer solution collected in the tank (F01) is subjected to cooling to a temperature of 50-70°C by continuously feeding it with a pump of the concentrated polymer solution (Z02) initially to the heat exchanger (LM01), to simultaneously heat the filtered and condensed solvent entering to the heat exchanger (LM01) from the tank (X01), and then to the cooler of the concentrated polymer solution (L01), to precipitate and reduce the solubility of the polymer, after which the solution is fed to a low-porosity ceramic filter (I01), from where the filtered solvent together with the solvent from the vapor condenser solvent (J01) is fed into the primary solvent tank (X01) and then through the heat exchanger (LM01), primary solvent pump (Z03), primary solvent heater (M01) and scrubber spiral shaft (E01) into the dilute solution tank polymer (F02), after which the continuous process of waste recycling begins anew by feeding a highly dilute polymer solution through a dilute polymer solution pump (Z01); G) after filtering on a low-porosity ceramic filter (I01), the formed polymer cake enters the polymer dryer (H01), and the solvent vapor enters the solvent vapor condenser (J01), where the solvent vapor also enters from the aluminum dryer (K01); H) the solvent after its condensation from the vapor state at different stages of the process enters the tank for the primary solvent (X01) for further reuse by feeding it into the tank for suspension (B02); i) The separated aluminum is periodically removed through the aluminum recovery device (G10) by periodically opening and closing it with circular and reciprocating vertical movement to maintain pressure inside the dissolver tank (C01), while being cleaned - 18 040731 from the polymer, aluminum from the device (G10) enters the dryer (K01), while the solvent vapors formed in the dryer enter the condenser (J01), combining with the condensed solvent stream from the polymer dryer (H01); J) since dry aluminum contains small amounts of cellulose fibers, fragments of plastic caps and polypropylene tapes, it is fed from the dryer (K01) to the grinder (P01) into which room temperature kerosene is added from the tank (O01), grinding is carried out by cutting the incoming material into fragments , while carrying out not only the separation of the residual polymer, but also the release of residual cellulose fibers; K) turn off the grinding mode and the resulting suspension of aluminum is fed into the flotation tank (Q01), while air is supplied to the tank (Q01) through a device located at its bottom, for example, a sprinkler, while foam containing pieces is formed in the tank (Q01) polypropylene tapes and cellulose fibers; L) said foam is continuously removed by draining from the tank (Q01) the liquid supernatant stream entering the sieve basket (R01), where the lighter polypropylene particles and fibers are retained, and the kerosene is fed into the lower part of the tank by means of a circulation pump (T01). (Q01); M) after removing impurities, the resulting aluminum suspension is drained from the tank (Q01) through the drain filter (Y01) to the press (S01) to remove kerosene, the residual and filtered kerosene is pumped using a return pump (V01) into the kerosene tank (O01) for further use, while the filtered aluminum is fed to the melting, where the remaining kerosene evaporates. 2. The process according to claim 1, characterized in that the precipitation of the polymer at stage F in the tank (F01) is carried out by using a secondary solvent - any solvent with a low boiling point, in particular ethanol, which is able to react with the primary solvent without dissolving the polymer, for example polyolefin, polyethylene or polypropylene. 3. A process for batch recycling by separating the aluminized and plastic components of a carton or other packaging, characterized by separating the plastic film components of polyethylene or polypropylene with aluminum by dissolving the polymer in a polymer-compatible primary solvent with a short C5-C7 polymer chain, under pressure at a temperature below temperature polymer softening, followed by precipitation due to temperature decrease, separation of the primary solvent from the polymer, and finally filtration and reuse of the primary solvent in the solubilization step in the following sequence: A) small pieces of film or film equivalents are fed intermittently by means of a feed dispenser (A01) through the inlet shut-off valve (U01) into the intermittent feeder (B01), and from there through the outlet shut-off valve (U02) into the slurry tank ( B02); B) after closing the valve (U01), the valve (U02) is opened and the raw material, while supplying the primary solvent, is dosed into the suspension tank (B02), after each such supply, the valve (U02) is closed; C) intermittent supply of the concentrated polymer solution is carried out through the supply device of the concentrated polymer solution (N01), and intermittent return supply of the dilute polymer solution is carried out through the corresponding device (N02), using a piston displacement pump, while the supply device of the concentrated polymer solution (N01) is in operating condition until a ratio of 8-15 parts of solvent to 1 part of foil is reached to cover the entire film in the slurry tank (B02) to form a suspension of the polymer and aluminum film in the solvent; D) then a liquid stream consisting of a polymer solution and suspended aluminum is fed into a screen filter (D01) driven by a screw conveyor, while separating aluminum to form a concentrated polymer solution; at the same time, the concentrated polymer solution passes through the walls of the screen, providing back pressure for the dissolver tank (C01) and enters the tank for the concentrated polymer solution (F01), and aluminum with residual polymer enters the polymer waste scrubber using the filter screw conveyor (D01) (E01) for further separation of the polymer, the pipe connecting the screen filter (D01) and the polymer waste scrubber (E01) prevents its further advancement, and the separated aluminum enters the device for extracting aluminum from the system (G10) at a different speed; E) to remove polymer residues, the filtered and condensed solvent from the primary solvent tank (X01) is injected through intermediate devices into the scrubber (E01) through a nozzle made inside a spiral element fixedly placed in the scrubber, after which the resulting dilute polymer solution enters the dilute solution tank polymer (F02) and passing through the screen creates a back pressure in the dissolver tank (C01); F) the concentrated polymer solution collected in the tank (F01) is subjected to cooling to a temperature of 50-70 ° C by continuously supplying it using a concentrated solution pump - 19 040731 polymer (Z02) initially into the heat exchanger (LM01), for simultaneous heating of the filtered and condensed solvent entering the heat exchanger (LM01) from the tank (X01), and then into the cooler of the concentrated polymer solution (L01), for precipitation and solubility reduction polymer, after which the solution is fed to a low-porosity ceramic filter (I01), from where the filtered solvent, together with the solvent from the solvent vapor condenser (J01), is fed into the tank for the primary solvent (X01), and then through the heat exchanger (LM01), the pump for the primary solvent ( Z03), the primary solvent heater (M01) and the scrubber spiral shaft (E01) into the dilute polymer tank (F02), after which the batch recycling process is restarted by supplying the primary solvent through the dilute polymer solution feed pump (Z01); G) after filtering on a low-porosity ceramic filter (I01), the formed polymer cake enters the polymer dryer (H01), and the solvent vapor enters the solvent vapor condenser (J01), where the solvent vapor also enters from the aluminum dryer (K01); H) the solvent after its condensation from the vapor state at different stages of the process enters the tank for the primary solvent (X01) for further reuse by feeding it into the tank for suspension (B02); I) the concentrated polymer solution collected in the tank (F01) is subjected to cooling to a temperature of 50-70°C by periodically supplying it with the help of a concentrated polymer solution supply device (N03) initially to the heat exchanger (LM01), for simultaneous heating of the filtered and condensed solvent, entering the heat exchanger (LM01) from the tank (X01), and then to the cooler of the concentrated polymer solution (L01), to precipitate and reduce the solubility of the polymer, after which the solution is fed to a low-porosity ceramic filter (I01), from where the filtered solvent together with the solvent from the condenser Solvent vapors (J01) are fed intermittently into the primary solvent tank (X01) and then through the heat exchanger (LM01), with the help of the solvent supply device (N04), the primary solvent heater (M01) and the axis of the scrubber spiral element (E01) into the tank for a dilute polymer solution (F02), a dilute solution obtained by purifying a The aluminum in the scrubber (E01) is collected in the dilute solution tank (F02), after which the batch recycling process is started again by feeding the solvent through the device (N02). J) since dry aluminum contains small amounts of cellulose fibers, fragments of plastic caps and polypropylene tapes, it is fed from the dryer (K01) to the grinder (P01) into which room temperature kerosene is added from the tank (O01), grinding is carried out by cutting the incoming material into fragments , while carrying out not only the separation of the residual polymer, but also the release of residual cellulose fibers; K) turn off the grinding mode and the resulting suspension of aluminum is fed into the flotation tank (Q01), while air is supplied to the tank (Q01) through a device located at its bottom, for example, a sprinkler, while foam containing pieces is formed in the tank (Q01) polypropylene tapes and cellulose fibers; L) said foam is continuously removed by draining from the tank (Q01) the liquid supernatant stream entering the sieve basket (R01), where the lighter polypropylene particles and fibers are retained, and the kerosene is fed into the lower part of the tank by means of a circulation pump (T01). (Q01); M) after removing impurities, the resulting aluminum suspension is drained from the tank (Q01) through the drain filter (Y01) to the press (S01) to remove kerosene, the residual and filtered kerosene is pumped using a return pump (V01) into the kerosene tank (O01) for further use, while the filtered aluminum is fed to the melting, where the remaining kerosene evaporates. 4. The process according to claim 1, characterized in that in step D the aluminum is isolated in a finely divided form by filtering the liquid stream, consisting of a polymer solution and suspended aluminum, and then washing the filtered aluminum on a low-porous ceramic filter (I01), while the resulting filtrate is fed into a tank (F01) for further precipitation of the polymer. 5. A device for carrying out a continuous waste recycling process by separating aluminized and plastic components of a cardboard or other packaging for carrying out the method specified in claim 1, characterized in that it contains a feed dispenser (A01) with a rotary valve or a similar device, an intermittent feed device raw materials (B01) of cylindrical shape and conical bottom, a continuous feed device (B01A) of cylindrical shape and conical bottom with an internal screw conveyor, while the diaphragm-type shut-off valve (U01) and the diaphragm-type shut-off valve with tangential adjoining solvent supply (U02) are located at the inlet and outlet of the intermittent feed device (B01), the continuous feed device (B01A) is connected to the suspension tank (B02), which, in turn, is connected to the dissolver tank (C01), which has a cylindrical body with a heating jacket, inside it, and along its vertical axis is fixed sp iral-shaped ramp with a round cross section; tank (C01), in turn, is connected to a conical screen filter (D01) and - 20 040731 with a screw conveyor located inside on the wall of the screen and a check valve at the outlet to the tank for a concentrated polymer solution (F01); wherein the filter (D01) is connected to the waste polymer scrubber (E01), through a pipe connecting the screen filter (D01) and the waste polymer scrubber (E01); the specified scrubber (E01) has a cylindrical body with a large cross-section inside which is placed a cylindrical screw conveyor with a hollow axis and a check valve at the outlet to the tank for a dilute polymer solution (F02); the scrubber (E01) is also connected to an aluminum recovery device (G10) containing a casing (G12) of a cylindrical shape with an upper (G12A) and a lower (G12B) opening, inside the casing there is a vertically movable rotating piston (G11), while the distance between the lower (G12B) and upper (G12A) holes are slightly larger than the height of the upper hole, and they are located on the piston (G11) at an angle of 180° to each other, while the piston (G11) contains a cavity (G11A) of a semi-cylindrical shape with an internal cutout , inclined at an angle of 45 °, above and below the cavity, the piston contains three sealing rings, while the distance between the rings is slightly greater than the height of the cavity; the device (G10) is connected to an aluminum dryer (K01) with a screw conveyor and a heating jacket; in turn, the dryer (K01) is connected to an aluminum grinder (P01) of cylindrical shape with sharp knives and baffles and a solvent vapor condenser (J01) of the heat exchanger type; at the same time, the aluminum grinder (P01) is also connected to the kerosene tank (O01) and the flotation tank (Q01) of an elongated cylindrical shape with a screen basket (R01) and an air sprinkler placed at its bottom; while the bottom of the basket (R01) has a hole in the lower part and is connected through the circulation pump (T01) to the tank (Q01); wherein the tank (Q01) at the bottom is connected to a basket-type drain filter (Y01), which in turn is connected to a piston-type press (S01); while the filter (Y01) and press (S01) through the return pump (V01) are connected to the tank for kerosene (O01); wherein the dilute polymer solution tank (F02) is connected to the slurry tank (B02) via a dilute polymer solution supply pump (Z01); the tank for the concentrated polymer solution (F01) is connected to the heat exchanger (LM01) via the pump for supplying the concentrated polymer solution (Z02); in turn, the heat exchanger (LM01) through the primary solvent pump (Z03) and the primary solvent heater (M01) is connected to the scrubber (E01); wherein the heat exchanger (LM01) is connected through a heat exchanger-type concentrated polymer solution cooler (b01) to a low-porosity ceramic filter (I01) for filtering the viscous polymer under pressure; wherein the low-porosity ceramic filter (I01) is connected to a polymer dryer (H01) with a screw conveyor, as well as to a primary solvent tank (X01); wherein the primary solvent tank (X01) is connected to a heat exchanger (LM01); wherein the polymer dryer (H01) is connected to the solvent vapor condenser (J01) and the condenser (J01) is connected to the primary solvent tank (X01). 6. The device according to claim 5, characterized by the presence of a low-porosity ceramic filter (I01) located after the cooler of the concentrated polymer solution (L01) and connected to the polymer dryer (H01) and the primary solvent tank (X01). 7. A device for carrying out a batch recycling process by separating aluminized and plastic components of a cardboard or other packaging for carrying out the method according to claim 3, characterized in that it contains a feed dispenser (A01) with a rotary valve or a similar device, an intermittent feed device (B01) of cylindrical shape and conical bottom, continuous feed device (B01A) of cylindrical shape and conical bottom with internal screw conveyor, while the diaphragm type check valve (U01) and the diaphragm type stop valve with tangential adjoining solvent supply (U02) are located on at the inlet and outlet of the intermittent feed device (B01), the continuous feed device (B01A) is connected to the suspension tank (B02), which, in turn, is connected to the dissolver tank (C01), which has a cylindrical body with a heating jacket, inside it, and a spiral is fixed along its vertical axis scarlet-shaped ramp with a round cross section; the tank (C01), in turn, is connected to a screen filter (D01) of a conical shape and with a screw conveyor located inside on the wall of the screen and a check valve at the outlet to the tank for a concentrated polymer solution (F01); wherein the filter (D01) is connected to the waste polymer scrubber (E01), through a pipe connecting the screen filter (D01) and the waste polymer scrubber (E01); the specified scrubber (E01) has a cylindrical body with a large cross-section inside which is placed a cylindrical screw conveyor with a hollow axis and a check valve at the outlet to the tank for a dilute polymer solution (F02); the scrubber (E01) is also connected to an aluminum recovery device (G10) containing a casing (G12) of a cylindrical shape with an upper (G12A) and a lower (G12B) opening, inside the casing there is a vertically movable rotating piston (G11), while the distance between the lower (G12B) and upper (G12A) holes are slightly larger than the height of the upper hole, and they are located on the piston (G11) at an angle of 180 ° to each other, while the piston (G11) contains a cavity (G11A) of a semi-cylindrical shape with an internal cutout inclined at an angle of 45 °, above and below the cavity, the piston is - 21 040731 holds three sealing rings, while the distance between the rings is slightly greater than the height of the cavity; the device (G10) is connected to an aluminum dryer (K01) with a screw conveyor and a heating jacket; in turn, the dryer (K01) is connected to an aluminum grinder (P01) of cylindrical shape with sharp knives and baffles and a solvent vapor condenser (J01) of the heat exchanger type; at the same time, the aluminum grinder (P01) is also connected to the kerosene tank (O01) and the flotation tank (Q01) of an elongated cylindrical shape with a sieve basket (R01) and an air sprinkler placed at its bottom; while the bottom of the basket (R01) has a hole in the lower part and is connected through the circulation pump (T01) to the tank (Q01); wherein the tank (Q01) at the bottom is connected to a basket-type drain filter (Y01), which in turn is connected to a piston-type press (S01); while the filter (Y01) and press (S01) through the return pump (V01) are connected to the tank for kerosene (O01); wherein the dilute polymer solution tank (F02) is connected to the slurry tank (B02) via a dilute polymer solution supply pump (Z01); the tank for the concentrated polymer solution (F01) is connected to the heat exchanger (LM01) via the pump for supplying the concentrated polymer solution (Z02); in turn, the heat exchanger (LM01) through the primary solvent pump (Z03) and the primary solvent heater (M01) is connected to the scrubber (E01); wherein the heat exchanger (LM01) is connected to a low-porosity ceramic filter (I01) through a polymer solution cooler (L01) of the heat exchanger type to filter the viscous polymer under pressure; wherein the low-porosity ceramic filter (I01) is connected to a polymer dryer (H01) with a screw conveyor, as well as to a primary solvent tank (X01); wherein the primary solvent tank (X01) is connected to a heat exchanger (LM01); while the polymer dryer (H01) is connected to the solvent vapor condenser (J01), and the condenser (J01) is connected to the primary solvent tank (X01), the slurry tank (B02) is cylindrical in shape with a conical bottom, located between the intermittent supply of raw materials ( B01) and dissolver tank (C01); device for periodic supply of concentrated polymer solution (N01); a device for periodic backfeeding of a dilute polymer solution (N02); device for intermittent supply of concentrated polymer solution (N03).