EP4511202A1 - Process and apparatus for increasing intrinsic viscosity of polycondensates - Google Patents

Abstract

Process and apparatus for processing of polycondensates, in particular for recycling processing of contaminated polycondensates, comprising the following processing steps: a) initially charging the polycondensates/materials to be processed, in particular in a container, b) at least partially, especially completely, melting the polycondensates, in particular by extruding in an extruder, and preparing a polymer melt, c) mixing the polymer melt, d) cooling the polymer melt, e) treating the mixed and cooled polymer melt in a melt reactor, in particular for polycondensation/postcondensation, to increase the intrinsic viscosity and/or to purify the polymer melt.

Description

METHOD AND DEVICE FOR INCREASING THE INTRINSIC VISCOSITY OF POLYCONDENSATE

The present invention relates to a method and a device for processing polycondensates or materials containing polycondensates, in particular for recycling processing of contaminated polycondensates, according to claim 1 or claim 12.

Essentially, it is about a process sequence or a device sequence that can be used when processing recycling materials consisting of or containing thermoplastic polycondensates. Polycondensates are the products of polycondensation, in which monomers with at least two reactive functional groups are linked to the polymer with the elimination of low-molecular compounds. Along with chain polymerization and polyaddition, polycondensation is one of the most important polymerization reactions.

The polycondensates that often occur in the course of recycling processing include, in particular, PET, PET-G, PET-A and their co-polymers, PA, PC, polycondensates from renewable raw materials such as PLA, but also other ester compounds, which include: Temperature and vacuum polymerize or polycondense.

During recycling processing, the polycondensates, which are solid in the state of use, are first transferred into a polymer melt, in particular with an extrusion system, e.g. with a known PCU (preconditioning unit) / cutting compressor-extruder system, whereby the PCU can be placed under vacuum or inert gases . The melt can be filtered and is then transferred via a melt cooler into a melt reactor - MSP (melt state process) reactor or an LSP (liquid state process) reactor - where a reaction, in particular a (post)polycondensation, and/or cleaning of the polymers takes place. Subsequently, the melt treated in this way is fed to a downstream device, which either produces granules or semi-finished products are produced in line, such as fibers, filaments, tapes, pre-forms for the production of bottles or containers or films with corresponding downstream processes.

Methods and devices that are generally suitable for recycling polycondensates are known from the prior art. Polycondensates, such as polyethylene terephthalates, are sensitive and are subject to various degradation processes, for example hydrolytic degradation, thermal degradation or thermo-oxidative degradation. Thermal degradation is primarily a problem in processes in the melting phase and leads, for example, to a decrease in the intrinsic viscosity iV, to the formation of carboxyl end groups or acetaldehyde or to the yellowing of the polymer, etc. Oxygen further accelerates these degradation reactions with the formation of free radicals and reinforced.

High mass or melt temperatures often lead to a negative impact on the quality of the end polymers and cause, among other things, a shortening of the molecular chains, undesirable gel formation or burning of particles and polymer in the melt. The decomposition of the polymer or ingredients is also promoted by high temperatures. This means that some of the efforts of the upstream processes to increase material quality, e.g. pretreatment, filtration, degassing, are reversed or counteracted.

In this context, the property of polycondensates is exploited in that damage caused during the production and/or use of the products - for example the shortening of the polymer chains due to thermal and/or hydrolytic degradation, or the penetration of foreign substances into the polymer - is relatively easy need to be “repaired”, for example through re-polymerization. This means that the same or almost the same properties as the original product can be produced again. Some properties can even be improved by such a treatment, for example the mechanical properties, but also the reduction of foreign substances that have previously migrated into the polymer during use.

The influence on the properties of used polycondensate products is largely known and can be carried out by polycondensation reactions or cleaning by diffusion, before melting, during melting or after the melting process in the liquid phase or in the solid phase. For this purpose, solid-phase post-condensation reactors (solid state SSP reactors) or melt reactors (MSP or LSP reactors) are usually used.

Solid phase post-condensation (SSP) is a process for the further condensation of polycondensates in order to increase their molecular weight under the gentlest possible conditions. The granulated polycondensate is post-treated under inert gas or vacuum. This process has the advantage of being deeper than melt polycondensation Reaction temperature and therefore less discoloration of the polycondensates. It also avoids viscosity problems that can be serious in a polycondensate melt. However, an SSP treatment usually requires more time, e.g. 10-20 hours compared to around 1 hour for an MSP or LSP treatment. The systems are therefore larger and less flexible. Variable viscosities (iV) in the input are more difficult to regulate.

Melt polycondensation under vacuum also uses the inherent property of polycondensates, especially PET, to (re)condense in the melt phase, which leads to an increase in the IV value and the efficient removal of volatile impurities. Compared to SSP, the reaction rate in the melt is significantly higher than in the solid phase.

In the case of treating materials from the field of processing industrial or post-consumer waste using a melt and a melt reaction treatment, the following problem often arises due to the different properties of the input materials, in particular the differences in viscosity, contamination, ingredients, etc :

When transferring it into the melt, for example through an extrusion system, it is often not possible or sufficient care is not taken to achieve a narrow temperature distribution of the melt. This is partly in the area of the melting process, partly in the area of mechanical filtration of the melt, whereby different melt temperatures are generated depending on the polymer properties and degree of contamination. In some cases, low-viscosity parts of the melt remain colder and high-viscosity parts of the melt receive more energy in the form of shear, for example in the extruder screw or during filtration, and therefore heat up more. These differences in viscosity are very often already present in the input material and are sometimes not known or recognizable or are not taken into account. However, this leads to problems in the processing process and reduced quality of the end products.

It is therefore the object of the present invention to create a method and a device for the advantageous preparation of polycondensates or materials containing polycondensates, with which increased process reliability and increased quality of the end products can be achieved. In particular, this should also increase the intrinsic viscosity of the material and reduce the content of impurities or impurities. This object is achieved according to the invention by a method for processing polycondensates or materials containing polycondensates, in particular for recycling processing of contaminated polycondensates, for example PET, PA, PC or PLA, the method comprising the following processing steps: a) presentation of the ones to be processed Polycondensates or materials, in particular in a container, b) at least partial, in particular complete, melting of the polycondensates, in particular by extrusion in an extruder, and creating a polymer melt, c) mixing the polymer melt, d) tempering, in particular cooling, the polymer melt, e) Treatment of the mixed and tempered, in particular cooled, polymer melt in a melt reactor, in particular for polycondensation or post-condensation, to increase the intrinsic viscosity and/or to clean the polymer melt.

Analogously, the objective object is achieved according to the invention by a device for processing polycondensates or materials containing polycondensates, in particular for recycling processing of contaminated polycondensates, the device comprising: a melting device for melting the polycondensates to be processed and for producing a polymer melt, one of A mixing device following the melting device for mixing the polymer melt, a temperature control device following the melting device, in particular a cooling device, for temperature control, in particular reduction, of the temperature of the polymer melt, a melt reactor connected thereto for treating the mixed and tempered, in particular cooled, polymer melt, in particular for polycondensation or post-condensation , to increase the intrinsic viscosity and/or to clean the polymer melt.

When reprocessing different or inhomogeneous materials, different material flows arise, for example from the packaging of containers and bottles have a high initial viscosity, with materials from the field of deep-drawing films that have a lower viscosity in the melt and/or with fibrous materials that have a very low viscosity. For some PET mixtures, the average core temperature of the melt is 275 °C, with a significant range of +/- 20 °C.

When treating a polycondensate melt in a melt reactor, for example an MSP reactor, a reaction and/or cleaning is carried out under temperature, residence time and with the removal of, among other things, moisture, oxygen, glycol or other substances.

If such a polymerization or post-condensation is carried out in the melt reactor, the molecular chain distribution becomes narrower the narrower the temperature spectrum of the input melt and the narrower the residence time spectrum in the melt reactor.

The residence time spectrum in the melt reactor is kept in the narrowest possible range by suitable measures, for example conveying devices, level measurements, etc. Furthermore, applying a vacuum and/or flushing with inert gases ensures that the reaction proceeds largely the same along the reactor.

Taking into account that the reaction rate of a chemical reaction approximately doubles with a temperature increase of 10 ° C, it is advantageous if the melt has a narrow temperature distribution when it enters the melt reactor.

Furthermore, it has proven to be advantageous that the absolute temperature of the melt upon entry into the melt reactor is chosen to be as low as reasonably possible. Although this reduces the reaction speed and extends the time required in the reaction system, it leads to greater process reliability and better final quality. The influence of temperature on reaction rates is subject to an exponential relationship, whereas the change over residence time only follows a linear relationship. The viscosity range or molecular chain distribution can also be kept narrower by setting a lower temperature of the melt, since short-chain polymer parts, i.e. polymer parts with lower viscosity, polymerize more quickly in relation to long-chain molecules at a certain temperature.

It should also be noted that during the reaction in the melt reactor, in addition to the desired polycondensation reactions, there are various undesirable side reactions that negatively affect the quality of the final polymer. These side reactions fall also significantly lower at lower temperatures. The residence time has an increasing influence on these side reactions, but the temperature has an exponential influence on them, ie at higher temperatures the number of undesirable side reactions increases disproportionately.

A particularly undesirable disruptive substance in this context is acetaldehyde. Acetaldehyde creates a fruity apple taste, especially in beverage bottles, but this is extremely undesirable, especially when packaging water. However, such by-products can also have a negative influence on processability.

High demands are also regularly placed on the range of melt viscosity of the end products. For new goods, a range of +/- 0.002 dl/g is a common value. Due to the high use of recyclates, this range can also be maintained during reprocessing.

The different content of residual catalysts, fillers, etc. influences the reaction rate and partly also the diffusion rate. For these reasons too, it is advantageous to set the lowest sensible reaction temperature and temperature range.

Another situation that typically occurs during recycling is the remaining residues of migration substances, contamination, etc. in the polymer. These foreign or disruptive substances regularly lead to losses in the quality of the material produced. For example, a material discolors significantly more at elevated temperatures than when the time is extended.

Accordingly, there are several factors to consider, especially

- that increasing the temperature of the melt is often disadvantageous and undesirable for the subsequent process,

- that inconsistent and excessively high melt temperatures often lead to quality problems, and/or

- that a homogenized, mixed and tempered, especially cooled, melt is often advantageous for improved product quality and thus a constant output volume and a homogeneous viscosity distribution can be achieved. According to the invention, there is a special combination of extruder, melt mixer and melt temperature controller, in particular melt cooler and melt reactor. The requirements and preparation of the melt for a process in a melt reactor MSP/LSP are particularly delicate and demanding - appropriate preparation and setting of the melt parameters is therefore more important and more difficult than for an SSP, for example.

For this reason, the invention proposes that when processing polycondensates, in particular from secondary raw material sources, using a melt reactor, the temperature of the melt is equalized, tempered, in particular lowered, and width reduced before the melt reactor. Particular attention must be paid to this, especially given the elevated temperatures that regularly occur in the melt reactor. All of this is guaranteed by the method according to the invention and the device according to the invention.

The equalization of the temperature is to be understood both in terms of time and location, i.e. the temperature should be as constant as possible over a longer period of time, i.e. from several minutes to hours, and the local or local deviation transverse to the direction of flow should also be as small as possible.

In every channel system there is a certain temperature distribution or a radial temperature gradient from the inside to the outside across the direction of flow. At higher throughputs, appropriate channel cross-sections are required and this results in local temperature inhomogeneity across the flow direction. Local cross-mixing of the melt is therefore advantageous.

In the course of the continuous process, especially through the extrusion process, there are also temperature changes over time, e.g. due to the cleaning of the filters, there is briefly higher shear in the extruder and this leads to increased temperatures over time. Due to different material forms, e.g. regrind, partially crystallized fibers, thick fibers, highly stretched fibers, but also iV differences in the starting material, the material is sheared differently in the extruder, which also leads to further temperature inhomogeneities over time and the resulting viscosity fluctuations in the course of the process leads.

Temperature equalization: targeted temperature control reduces the time component of the temperature deviation. Temperature width reduction: the melt temperature has a distribution across the channel and a distribution over time that is determined by the previous influences and/or the material components. Mixing reduces this temperature range, but also tempering.

In the present case, the term tempering means an adjustment of the temperature of the melt to the desired or advantageous temperature. This can be a reduction or an increase in temperature. The temperature control device or the melt/temperature control mixer is suitable, designed, controlled and/or provided for cooling and/or heating.

Advantageously, tempering involves reducing the temperature or cooling. This advantageously takes place in a corresponding cooling device or in a melt/cooling mixer.

However, there are also situations in which an increase in temperature, usually a small one, is advantageous or necessary, usually only by a few degrees. This is the case, for example, if the temperature in front of the cooler is too low and the melt needs to be heated, for example if the melt comes too cold from the upstream extrusion process because it is very thin and therefore has less energy input into the extruder. Accordingly, tempering involves increasing the temperature or heating. This advantageously takes place in an appropriately suitable and designed temperature control device or the melt/temperature control mixer.

In the method according to the invention, the processing steps are advantageously carried out in the specified order a) to e).

However, it is particularly advantageous if steps c) and d) take place simultaneously or in a common process step, i.e. if the polymer melt is mixed and tempered, in particular cooled, at the same time.

In order to improve cleaning, it is advantageous if the polymer melt is filtered before steps c) and d) to remove unmelted components and/or impurities.

An increase in product quality also results from the fact that the filtered polymer melt is degassed before steps c) and d). A particularly efficient and advantageous mixture and a fundamentally advantageous narrow residence time spectrum are achieved when the polymer melt is mixed distributively.

It is advantageous for product quality if the polymer melt is mixed and/or tempered, in particular cooled, in such a way that the temperature distribution in the polymer melt, particularly in the phase from before mixing or tempering, in particular cooling, to immediately before the melt reactor, preferably in the phase from the start of melting during extrusion to before the melt reactor, in particular over the entire process, < +/- 10 ° C, in particular < +/- 5 ° C, preferably < +/- 1 ° C. This means that a narrow viscosity range or molecular chain distribution can be achieved.

In order to achieve high product quality and higher process reliability and to avoid side reactions, it is further advantageous if the polymer melt is tempered, in particular cooled, in such a way that the temperature of the polymer melt immediately before or upon entry into the melt reactor is 5-25% lower is the temperature of the polymer melt immediately before mixing and tempering, in particular cooling, or before steps c) and d).

In this context, it is also advantageous and the advantages just mentioned can be achieved if the polymer melt is tempered, in particular cooled, in such a way that the temperature of the polymer melt immediately before or upon entry into the melt reactor is only relatively slightly, i.e. around 1 -10 %, is above the melting range of the polymer.

An advantageous procedure provides for special steps at the beginning of the processing process, namely that the polycondensates or materials are comminuted and/or heated before melting according to step b), in particular during step a), it being preferably provided that the polycondensates or materials while maintaining their lumpiness and free-flowing properties, are heated and permanently mixed, and if necessary degassed, softened, dried, increased in viscosity and/or crystallized.

A further advantageous and efficient procedure is that at least the processing steps c), d) and e), in particular all the intended processing steps, follow one another immediately and directly in terms of time and location, in each case without any further intermediate processing step. In the device according to the invention, it can advantageously be provided that the melt reactor is spatially directly and directly connected to the mixing device or the temperature control device, in particular cooling device, in the conveying direction, without any further intermediate functional unit, or is connected downstream of the mixing device or the temperature control device, in particular cooling device, and is procedurally linked one after the other.

An effective and advantageous device provides that the melting device is an extruder, the extruder in particular comprising a melt filter and/or a degassing zone.

An overall arrangement that is advantageous for achieving high-quality end products is characterized in that the melting device is preceded by a cutter-compressor, in particular a cutter-compressor-extruder combination being provided for comminuting and/or heating the polycondensates or materials. The cutting compactor is preferably set up and suitable for heating and permanently mixing the presented polycondensates or materials while maintaining their lumpiness and free-flowing properties, and if necessary for degassing, softening, drying, increasing their viscosity and/or to crystallize.

An efficient and advantageous device provides that the mixing device is a distributive mixer.

It is particularly advantageous in this context if the mixing device is at the same time the temperature control device, in particular a cooling device, with in particular a melt temperature control mixer or melt temperature control/mixer, preferably a melt cooling mixer or melt cooler/mixer, being provided.

An MSP reactor or an LSP reactor is advantageously provided as the melt reactor.

For the intended use according to the invention, the exact design of the melt reactor is relatively irrelevant. It can advantageously be a melt reactor of the type DE 1745541, but also of the type DE 4013912 or DE 4126425.

What all melt reactors have in common is that an attempt is made to greatly increase the surface area of the melt under reduced pressure conditions or in an inert gas flow and to start a polycondensation reaction in order to lengthen the polymer chains and thus improve the mechanical properties of the polymer when it is reused to optimize an end product. Furthermore, the diffusion process enables the removal of undesirable substances that may have gotten into the polymer through previous use. This creates the possibility of using these polymers again in applications where food suitability, smell and skin compatibility must be guaranteed. The reaction products or diffusion products are removed either by the negative pressure or by the inert gas flow.

In order to achieve good product quality, it is advantageously provided if the mixing device and/or the temperature control device, in particular cooling device, or the melt temperature control mixer, preferably the melt cooling mixer, are controllable or controlled in such a way that the temperature distribution in the polymer melt < +/- 10 ° C, in particular < +/- 5 ° C, preferably < +/- 1 ° C. In this context, it is particularly advantageous if this temperature distribution is in the area in front of the mixer or temperature controller, in particular the cooler, up to directly up to or in front of the melt reactor, preferably in the area of the melting unit or extruder up to in front of the melt reactor, in particular in the entire area System or device is achieved.

In order to achieve and set good product quality and higher process reliability, it is advantageously provided if the mixing device and/or the temperature control device, in particular the cooling device, can be controlled or controlled in such a way that the temperature of the polymer melt immediately before or upon entry into the melt reactor is increased by 5- 25% lower than the temperature of the polymer melt immediately in front of the mixing device and the temperature control device, in particular cooling device, or in front of the temperature control mixer, preferably cooling mixer. In this way, side reactions can be reduced and a narrow iV range can be obtained in the final product.

In order to also achieve these advantages, it can advantageously be provided that the mixing device and/or the temperature control device, in particular the cooling device, are controllable or controlled in such a way that the temperature of the polymer melt immediately before/upon entry into the melt reactor is 1-10% above that Melting range of the polymer is.

From a plant engineering point of view, it can be advantageous to use feed pumps for the melt both before the temperature controller, in particular cooler, or mixer, as well as after the temperature controller, in particular cooler, or mixer, and/or after the melt reactor, in order to eliminate any pressure differences overcome. However, it is important to ensure that this, particularly through a possible pump after the temperature controller, in particular cooler/mixer, there is no significant increase in temperature in front of the melt reactor.

The core temperature of the melt is advantageously selected according to the desired residence time and the desired reaction rate in the melt reactor or reaction vessel. It has been shown that you should generally try to set the lowest possible core temperature.

The temperature control medium, in particular cooling medium, of the melt temperature control system, in particular melt cooling system, e.g. the melt cooler/mixer, is regulated according to the core temperature of the melt. For this purpose, the temperature can be recorded both before and after the melt temperature control system, in particular the melt cooling system. In advantageous temperature control systems, in particular cooling systems, the temperature of the melt can also be sensed in the temperature control section, in particular the cooling section. This temperature is used to adjust the temperature control medium, in particular the cooling medium.

It is advantageous if the melt temperature is sufficiently representative. The melt temperature in a supply pipe sometimes differs significantly on the wall or in the middle of the pipe. It is therefore recommended and useful to measure both the temperature on the wall and in the middle of the pipe. The thicker the cable, the more sensible it is to measure at several points across the cross section.

Advantageous embodiments of the method according to the invention and the device according to the invention are illustrated and explained below using more general and specific exemplary embodiments, which are not to be understood as restrictive:

What is often desired is the recycling processing of PET materials from very different sources, for example from leftover filaments, fiber residues, thermoforming films (e.g. cheese or sausage packaging, tool or electronics packaging), PET bottle material (e.g. water bottles or soft drinks), etc. The The viscosity range is usually considerable and is around 0.5 dl/g (for fibers) to 0.79 dl/g (for bottle grinds).

Such an inhomogeneous input material mix results in a correspondingly broad molecular chain distribution or a broad viscosity range. Furthermore, such Mixtures rarely contain exactly the same components, which means that the quantitative proportions of the different materials are different and also change constantly.

In the melting process, the particles, usually smaller particles in the form of polymer flakes, fibers or films, experience different shear stresses depending on their mechanical properties (size, stretch, thickness, etc.) and their viscous properties. This leads to a wide melt temperature distribution, e.g.: 276 °C +/- 20 °C (after the extruder), with the disadvantageous effects described above that are associated with such a wide and varying temperature distribution. After the filter, the melt temperature distribution is still around 277 °C +/-15 °C. After the melt cooler/mixer, the melt temperature distribution is 260 °C +/- 3 °C, although a range of under 3 °C can also be achieved. This means that the temperature of the melt is evened out, lowered and reduced in width before the melt reactor.

Example PET (A-PET) for packaging and fibers: melting temperature ranges PET

Melting temperature of PET: > 250 °C, typically 256 °C

Melt temperature for recycling as a rule: 275 °C to 310 °C (depending on the process and contamination and filtration fineness) Target temperature range before LSP: 260 °C to 270 °C +/- 3 °C

Cooling in the range of: 5 to 25% (at reference temperature 260 °C)

Viscosity lift depending on melt temperature:

The residence time t in the melt reactor is constant.

The input viscosity before the melt reactor is 0.5 dl/g.

Melt temperature: 270 °C, viscosity reached 0.53 dl/g

Melt temperature: 280 °C, viscosity reached 0.57 dl/g

Melt temperature: 290 °C, viscosity reached 0.62 dl/g

An advantageous diagram of an advantageous device or arrangement or system 1 is shown in FIG. 1 and an exemplary method is also explained with reference to FIG. This is an exemplary schematic representation for illustrative purposes the most important components and units of this device. This representation therefore makes no claim to the complete accuracy of all constructive details and proportions.

Not shown in Fig. 1 is an optional container in the form of a classic cutting compactor or a preconditioning unit (PCU). In the present case, this could be arranged to the right or in front of or upstream of the extruder. Such a cutting compactor or container is filled with the recycled polymer material to be processed. The polymer material is placed in the container, comminuted using mixing and comminution tools, mixed and heated until softened, although regularly not melted. The lumpiness of the sticky polymer particles is retained. In addition, the material undergoes a pretreatment and is, for example, dried, pre-compacted and, depending on the material, the viscosity is increased.

When processing secondary raw materials from polycondensates, an extrusion process is used to melt the polycondensates, depending on the shape of the materials present (e.g. fibers, granules, agglomerates, film snippets, thick-walled regrind, etc.). The secondary raw materials can come from different sources and be contaminated with solids but also with liquid substances, such as cotton fibers or spinning aids, which can consist of oils. Furthermore, these substances often have different viscosities when melted.

In the lowest area of this cutting compactor or container, the extruder 2 shown in FIG. 1 can be connected tangentially. The material is discharged from the container and transferred to the extruder 2, where it is captured by the screw. In the frontmost section of the extruder 2, on the left in FIG. 1, the material is melted and plasticized while increasing the pressure.

Single-screw extrusion systems or multi-screw extrusion systems, such as twin screws, can be used in this melting process. The well-known PCU extruder system has proven particularly useful, as it allows unwanted substances to be partially evaporated in the PCU, the material to be compressed and heated or softened. This system also has forced feeding of the extruder, which is particularly advantageous for poorly flowing fiber materials. The extruder then melts the material and optionally degasses the polymers. Furthermore, this process can be supported by negative pressure or inert gases in the PCU. The melt is then filtered in a filtering unit 3, which removes solid but also gel-like components from the melt.

Downstream and then to the filtering unit 3, and after this process of melting and the first cleaning step, the melt is transferred to the melt cooler/mixer 4, usually via a melt pump (not shown). This has the task of reducing the temperature inhomogeneities that have occurred, both spatially and temporally. At the same time, the average melt temperature is reduced. This is necessary because, among other things, the scattering of the different input materials results in different melt temperatures. Furthermore, the filtration process also leads to temporal or local inhomogeneities.

After the temperature of the melt has been lowered and equalized in the melt cooler/mixer 4, the melt is transferred to the melt reactor 5.

After going through the reaction or cleaning process in the melt reactor 5, the molten material then goes into a discharge unit and can optionally be post-processed, for example subjected to granulation. However, it can also be formed directly into an end product or semi-finished product, e.g. into fibers, films, bottle preforms, etc.

The amount, temperature and/or speed of the cooling medium is adjusted by measuring the melt temperature before or after the melt cooler/mixer 4 so that the desired target temperature is achieved. As can be seen in FIG. 1, at least the melt temperature 1 is recorded here and the temperature control medium is adjusted so that the desired temperature is achieved. This can be controlled with melt temperature 2. The temperature measurement can be carried out at different locations within the pipe, at the outermost edge and/or in the middle of the pipe. For very high system throughputs, it is advantageous to install thicker lines and/or multiple lines. In the case of thick pipes, the temperature is advantageously recorded at several points within the pipe. The temperature measurement is ideally carried out with several temperature recording devices, with the temperature being recorded representatively across the cross section of the inflow and/or outflow channel

By measuring the temperature distribution within the inlet and outlet lines, both the mixing quality and the cooling rate can be checked. The mixing quality is the tighter Temperature distribution can be seen and the cooling quality can be seen by reducing the average temperature.

Comparison tests:

The following tests were carried out on an exemplary test system according to the invention. This was a PCU/extruder combination INTAREMA 80 TE, equipped with a melt filter SW 4/134 according to the following system configuration:

The materials processed in this way are made up of fiber waste from a wide variety of areas of a spinning factory. Start-up waste (lumps), undrawn fibers, monofilaments and drawn fibers were used. Furthermore, the fibers had different spinning oil contents in the range of 0.3 to 2% by weight. The initial moisture contents were also different, in some cases they were 10% by weight or more.

The material was pre-shredded using the single-shaft shredder. Alternatively, mills can also be used for this. Using the PCU/extruder combination, the fibers were compressed, dried and heated and, after an appropriate residence time in the PCU, transferred to the single-screw extruder. After melting, the material was degassed and passed through the melt filter device.

The filtered melt was then conveyed via the melt pump to the melt cooler/mixer. The cooler/mixer used in this case was a static mixer without moving elements. The temperature control of the cooler/mixer was carried out using thermal oil that can be both heated and cooled. Both the melt temperature before the cooler/mixer and the temperature afterwards were recorded to check the effectiveness of the unit. Furthermore, the viscosity was measured after the melt reactor. Particular attention was paid to the stability of the viscosity over time.

For comparison, the melt cooler/mixer was removed and the melt was transferred directly to the melt reactor.

The melt reactor was a horizontal disk reactor, similar to the design according to DE 1745541. The polymer mass is passed through the reaction space several times in freely falling veils. Rotating disks pull the polymer mass out of a sump and the polymer mass flows back again as a thin film. This process achieves a very large surface area in relation to the volume of the reaction mass, which enables the reaction products released to evaporate in a short time and a polymer reaction is promoted.

In this case, the disk reactor was subjected to a negative pressure of 6 mbar. The disks rotated at a speed of 1 rpm. The average residence time of the material in the reactor was approximately 60 min.

After leaving the reactor, the material was granulated in the strand pelletizer.

The results were as follows:

Without melt cooler/mixer:

Throughput of approx. 350 kg/h. A mixture of PET waste from bottles, fibers and thermoforming films was used as input material.

Operating time approx. 10 hours

The melt temperature was recorded in front of the melt reactor (Fig. 2, lower curve). The temperature of the polymer mass was measured using a temperature sensor that was immersed approximately 20 mm in the melt stream. The average entry temperature was approximately 288 °C. The range of fluctuation in the melt temperature was approx. 35 °C.

The intrinsic viscosity was measured inline after the melt reactor and was on average approximately 0.69 dl/g with a fluctuation range of approximately 0.07 dl/g (FIG. 2, upper curve).

With melt cooler/mixer:

Throughput of approx. 350 kg/h.

The same mixture of PET waste from bottles, fibers and thermoforming films was used as input material.

Operating time approx. 20 hours

The melt temperature was recorded before the mixer/cooler (FIG. 3, middle curve) and after the mixer/cooler (FIG. 3, bottom curve). The temperature of the mass was measured with a temperature sensor that was immersed approximately 20 mm in the mass flow. The average entry temperature was approximately 293 °C. The melt was cooled to an average of 260 °C.

The intrinsic viscosity was measured inline after the melt reactor and was on average approximately 0.65 dl/g. The fluctuation range could be completely eliminated and was therefore better than the industry standard of +/- 0.002 dl/g (Fig. 3, top curve).

This clearly shows the advantageous uniformity, predominantly lowering and width reduction in the temperature of the melt and the intrinsic viscosity.

Claims

Patent claims 1. Process for processing polycondensates or materials containing polycondensates, in particular for recycling processing of contaminated polycondensates, comprising the following processing steps: a) presentation of the polycondensates or materials to be processed, in particular in a container, b) at least partial, in particular complete , melting the polycondensates, in particular by extrusion in an extruder, and creating a polymer melt, c) mixing the polymer melt, d) tempering, in particular cooling, the polymer melt, e) treating the mixed and tempered, in particular cooled, polymer melt in a melt reactor, in particular for polycondensation or post-condensation, to increase the intrinsic viscosity and/or to clean the polymer melt. 2. The method according to claim 1, characterized in that the processing steps take place in the specified order. 3. The method according to claim 1 or 2, characterized in that steps c) and d) take place simultaneously or in a common process step or that the polymer melt is mixed and tempered, in particular cooled, at the same time. 4. The method according to any one of claims 1 to 3, characterized in that before step c) and d), the polymer melt is filtered to remove unmelted components and/or impurities. 5. The method according to any one of claims 1 to 4, characterized in that the filtered polymer melt is degassed before steps c) and d). 6. The method according to any one of claims 1 to 5, characterized in that the polymer melt is mixed distributively. 7. The method according to any one of claims 1 to 6, characterized in that the polymer melt is mixed and/or tempered, in particular cooled, in such a way that the temperature distribution in the polymer melt is <+/- 10° C, in particular <+/- 5° C, preferably < +/- 1 ° C. 8. The method according to any one of claims 1 to 7, characterized in that the polymer melt is tempered, in particular cooled, in such a way that the temperature of the polymer melt immediately before or upon entry into the melt reactor is 5-25% lower than the temperature of the Polymer melt immediately before mixing and tempering, in particular cooling, or before steps c) and d). 9. The method according to any one of claims 1 to 8, characterized in that the polymer melt is tempered, in particular cooled, such that the temperature of the polymer melt immediately before or upon entry into the melt reactor is 1 - 10% above the melting range of the polymer . 10. The method according to any one of claims 1 to 9, characterized in that the polycondensates or materials are comminuted and/or heated before melting according to step b), in particular during step a), it being preferably provided that the polycondensates or .Materials are heated and permanently mixed while maintaining their lumpiness and flowability, and if necessary degassed, softened, dried, increased in viscosity and/or crystallized. 11. The method according to any one of claims 1 to 10, characterized in that at least the processing steps c), d) and e), in particular all the intended processing steps, follow one another immediately and directly in terms of time and location, in each case without any further intermediate processing step. 12. Device for processing polycondensates or materials containing polycondensates, in particular for recycling processing of contaminated polycondensates, comprising a melting device (2) for melting the polycondensates to be processed and for producing a polymer melt, a mixing device (3) following the melting device (2). ) for mixing the polymer melt, a temperature control device, in particular cooling device, (4) following the melting device (2) for temperature control, in particular reduction, of the temperature of the polymer melt, a melt reactor (5) connected thereto for treating the mixed and tempered, in particular cooled, polymer melt, in particular for polycondensation or Post-condensation, to increase the intrinsic viscosity and/or to clean the polymer melt. 13. The device according to claim 12, characterized in that the melt reactor (5) is spatially directly and directly connected, without any further intermediate functional unit, in the conveying direction to the mixing device (3) or the temperature control device, in particular cooling device (4) or the Mixing device (3) or the temperature control device, in particular cooling device, (4) is connected downstream and is coupled one behind the other in terms of process. 14. Device according to one of claims 12 to 13, characterized in that the melting device (2) is an extruder, the extruder in particular comprising a melt filter and / or a degassing zone. 15. Device according to one of claims 12 to 14, characterized in that the melting device (2) is preceded by a cutting compressor (1), in particular a cutting compressor-extruder combination being provided for shredding and / or heating the polycondensates or materials , wherein the cutting compactor (1) is preferably set up and suitable for heating and permanently mixing the presented polycondensates or materials while maintaining their lumpiness and free-flowing properties, and if necessary for degassing, softening, drying and increasing their viscosity and/or to crystallize. 16. Device according to one of claims 12 to 15, characterized in that the mixing device (3) is a distributive mixer. 17. Device according to one of claims 12 to 16, characterized in that the mixing device (3) is at the same time the temperature control device, in particular cooling device, (4), in particular a melt cooling mixer being provided. 18. Device according to one of claims 12 to 17, characterized in that the melt reactor (5) is an LSP reactor or an MSP reactor. 19. Device according to one of claims 12 to 18, characterized in that the mixing device (3) and / or the temperature control device, in particular cooling device, (4) can be controlled or controlled so that the temperature distribution in the polymer melt < +/- 10 ° C, in particular < +/- 5 ° C, preferably < +/- 1 ° C. 20. Device according to one of claims 12 to 19, characterized in that the mixing device (3) and / or the temperature control device, in particular cooling device, (4) can be controlled or controlled in such a way that the temperature of the polymer melt immediately before or when entering the melt reactor (5) is 5-25% lower than the temperature of the polymer melt immediately in front of the mixing device (3) and the temperature control device, in particular cooling device, (4) or in front of the temperature control mixer, in particular cooling mixer. 21. Device according to one of claims 12 to 20, characterized in that the mixing device (3) and / or the temperature control device, in particular cooling device, (4) can be controlled or controlled in such a way that the temperature of the polymer melt immediately before / upon entry into the Melt reactor (5) is 1-10% above the melting range of the polymer.