WO2006092306A1 - Method for depolymerising residues containing hydrocarbons and device for carrying out said method - Google Patents

Abstract

The invention relates to a method for depolymerising raw materials containing hydrocarbons, such as residues in a continuous process. To achieve a uniform operation using a comparatively simple technique, the raw material, which has been pre-heated to a liquid or pulpy consistency, is continuously injected under pressure into a reactor (4), which has been heated to a decomposition temperature and a gaseous fraction is continuously withdrawn from the reactor for further processing, whilst a bottom fraction is continuously removed or removed at intervals. The raw material is preferably pre-heated, liquefied and injected by an injection pump or extruder screw. A high degree of availability is guaranteed in conjunction with a mixer or doctor head, which cyclically removes deposits on the interior walls of the reactor.

Description

 Process for depolymerizing hydrocarbon-containing residues and apparatus for carrying out this process

The invention relates to a process for the depolymerization of carbonaceous residues, in particular for the production of diesel and heating oil, according to the preamble of claim 1 and an apparatus for carrying out this process according to the preamble of claim 15.

In the depolymerization of carbonaceous residues, in particular for the production of diesel oil, are plastics, oils, fats, dried garbage, electrical cables, wood, paper, digested sludge, agricultural residues, natural fibers and many other waste or waste materials with the Purpose catalytically depolymerized to obtain as few solid and gaseous conversion products. These processes occur at peak temperatures in the treated material between 300 and 450 ⁰ C, but in most cases at a temperature in the range of 400 ⁰ C, ie 340 ° C to 440 ⁰ C from. In the presence of ion-exchanging catalysts, the depolymerization process, ie the molecular shortening of long-chain hydrocarbon compounds, takes place relatively rapidly owing to the catalytic cleavage. there The hydrocarbon molecules attach themselves to the catalysts until they have reached the - depending on the type of residue - reaction temperature and vaporize the cleavage products. It is common to circulate a liquid / catalyst mixture between the vaporization temperature and the feedstock feed temperature. Feedstock feed reduces the mixture temperature. In a sequential heater, such as a tube heat exchanger, the vaporization temperature of the desired and lower boiling fractions is regained. The remaining liquid components are returned to the raw material feed. The forming in this cycle process agglomerations of catalyst material and higher boiling components of the raw material are discharged and further processed. The leaving the circuit vaporous fraction is in a distillation unit to obtain z. B. diesel or fuel oil distilled fractionally. Gaseous components are burned to produce hot combustion exhaust gases that provide the amount of heat and process temperature (gap temperature) required for evaporation in the fluid circuit. Insofar as the raw material contains chlorine, sulfur, phosphorus and / or other components which are undesirable in the product (diesel or heating oil), these are removed in the cycle process. This is done, for example, by using calcium aluminum silicate or sodium aluminum silicate as the ion-exchangeable catalyst and adding z. As lime in order to bind the chlorine, sulfur or phosphorus components to be removed from the raw material.

For carrying out these known catalytic depolymerization processes, various circulation processes have been described, for example in DE 100 49 377 A1 and DE 103 16 969 A1. In the former case, shredded, finely divided raw material is introduced via a metering screw from above into a first reactor in which there is a mixture of circulation oil, catalyst and already circulated raw material. This reactor is fed with the liquid vapor mixture from a heater. From there, the vaporous fraction and the forming solid fraction is removed. That mixed well with the liquid Raw material is heated and passes in a mixed into the liquid form via a pipe to the heater (DE 100 49 377 A1).

The catalytic depolymerization plant according to DE 103 16 969 A1 likewise circulates a catalyst suspended in a cycle oil. The latter is formed by the depolymerization reactor, a hydrocyclone and a separation vessel. The heating takes place in the specially constructed reactor by electric wall heating. This reactor has a central supply pipe for raw material, fresh catalyst, lime and circulating oil, which is guided with a screw conveyor down and mixed there with the recirculation liquid flowing back from the separation vessel. The central tube is surrounded within the reactor by several riser tubes, which allow an increase in the reactor sump resulting mixture via augers. An electrical wall heating of the riser pipes ensures that the gap temperature is reached so that a liquid vapor mixture is withdrawn at the upper end of the reactor.

It has been found that the heating of the raw material and the liquid containing the raw material to the gap temperature is extremely critical, because only by very gentle heating can be avoided that by local overheating of the liquid mixture to be heated pyrolysis of components of the mixture begins and the forming Carbon clogs on reactor walls or reactor internals, in particular on heat exchanger surfaces. This has led to the tubes becoming clogged and the process stopping, especially at the tube reactor. In general, this deposit is rock hard, so that the reactor can not be used again.

On this basis, a method with the features of claim 1 and a device having the features of claim 15 is proposed in a generic depolymerization to improve the raw material and heat input. The invention is based on the idea, the raw material in one - A - inject heated to nip temperature reactor in liquid or pasty consistency in a preheated state under pressure.

On the one hand, the invention makes it possible to produce, in particular, diesel / heating oil in a simple manner and with high yield from various organic substances; on the other hand, the generation of by-products such as dioxin, methane and others can be avoided in this method of waste and residual material utilization. The gas production is extremely low and can e.g. be reduced to about 4.5% of the raw material. For underfiring this gas is anyway reusable in the process. The use of catalysts is possible, but advantageously the process allows the avoidance of catalysts and the associated procedural difficulties and costs.

It has been found that this substantially simplifies the handling of raw materials and significantly reduces the risk of adhesion in the transport and feed system as well as the risk of caking in the fission reactor. Another advantage is that proven standard components for the pressure injection can be used, as they are known from the injection molding of plastics.

According to the invention, a wide variety of hydrocarbon-containing raw materials (collectively referred to herein as residues) can be processed into liquid products, such as, in particular, diesel oil. As raw material (residues) are mainly old, residual and waste materials into consideration, such as plastics, oils (also used and flushing oils), fats, dried garbage, electric cables, wood, paper, digested sludge, agricultural residues, natural fibers and many other waste or waste materials, but also renewable raw materials and rubbers. Particularly advantageous is the processing of plastics and waste oils. The process of cracking or depolymerization can thus be used to produce a high quality asset, namely fuel oil or diesel fuel from waste oil and plastics again. Particularly preferred is a pre-heating of a mixture of plastics and waste oils, which, particularly preferably, is carried out at temperatures above 200 ⁰ C, in particular to temperatures between about 250 ⁰ C and 300 ⁰ C. A significant advantage here is that water components of the feed mixture evaporate and do not enter the reactor. In addition, all other low-boiling substances are expelled, which therefore do not have to be channeled through the system. For this purpose, the waste heat of the cleavage reactor can be used.

The introduced plastics are thus, for example, recuperative, regenerative or by friction, preheated, conveyed to an injection nozzle such as an extruder and injected there under a certain or adjusting pressure in the reactor. By the correct choice of the pressure build-up and / or the injection nozzle, which can also be formed by the mouth of a pipeline, it can be achieved that this process is carried out continuously, ie that the raw material feed into the reactor is continuous and approximately constant , Of course, keeping the level in the reactor constant also requires that the removal of gases and of solid and liquid constituents and the feed-in of raw materials be adapted to each other. This leads to constant process conditions, which ensure a consistent product quality. Waste oil can be introduced in the same way in the reactor. In the reactor, the raw material is further heated, whereby the long-chain hydrocarbons are broken down into shorter-chain molecules. These have the energy at this temperature to leave the melt as gas and ascend into a distillation column. Depending on their length they are collected in different stages of the column. If the process parameters of the column are set correctly in a manner known per se, then in a condenser, with z. B. water cooling, the product - this oil or fuel oil - won. So far, the feedstock without special measures in finely divided state was fed into the reactor. The injection is carried out for the purpose of careful further heating in a centrally located area of the reactor.

To further optimize the heating of the raw material, it is proposed to use the reactor as a particularly rotationally symmetrical pot, e.g. with a parabolic or hygrobular inner contour in which a multi-bladed mixer rotates. It is advantageous if the ends of the mixing arm made of temperature-resistant ceramic or graphite material and / or the inner contour of the reactor are modeled substantially and provided with, in particular very little game, so as to prevent or eliminate deposits. As a result, the interfering carbon is deposited on the bituminous sludges forming as a waste product and is removed with these instead of being baked on the heated walls of the reactor.

If a pot-like reactor with stirring arms is used, the heat transfer is intensified and turbulences in the liquid arise, which allow the temperature at the pot surface to lower, which leads to a reduced formation of free carbon. Stirring near the surface or even scratching prevents deposits and avoids overheating while at the same time improving the heat transfer through the reactor wall.

The surface cleaning on the inner wall of the reactor can, if appropriate, also be carried out without a targeted mixing action by means of a cyclically operating scraping device, which is of independent inventive significance and is preferably guided cyclically along the contour of the inner wall of the reactor with minimal or no lateral play. Rotationally symmetric reactor inner wall contours are preferred for this purpose. A scraper head of the scraper device in this case carries at least two rotationally driven contour-matched scraper elements. These may be equipped with a replaceable wear pad, with the exceeding of a permitted wear clearance, for example, can be detected electrically measured. If the scraping head with its own weight or under the action of a force introduced by its rotational force to the reactor inner wall is applied or pressed, even small agglomerations can be removed from the reactor inner wall and fed to a reactor sump for discharging.

Under certain circumstances, such cocking devices are subject to their own risk of build-up, which could limit their effectiveness. In this way, the scraping device can be protected by a self-cleaning element, which can be activated from time to time for, in particular, scraping cleaning of the scraper elements via the scraping head. Typical cleaning cycles of a rotating scraper with two blades are about 1 to 1000 cleaning cycles per hour, preferably the rotational speed of a scraper head is from 1 to 20, preferably from 5 to 10 revolutions per minute. Depending on the size of the reactor and the susceptibility of the raw material to be depolymerized, the weight of the scraping device, which generates a certain contact pressure, may be a few grams to a few thousand kilograms. With a reactor capacity of about one cubic meter, typical self-weights of the scraping head are on the order of 10 kg to 1000 kg, preferably between 50 kg and 200 kg.

Under the action of such a scraper, which, as preferred, also has a mixing effect, the temperature differences between the mean desired temperature in the liquid to be depolymerized within the reactor and on the outer wall of the reactor can be kept advantageously low and can, for example, in the order of 20 ° and 8O ⁰ C are kept.

A further aspect of the invention is the improvement of a scraping device for demopolymerisationsreaktoren and the like as such. In that regard, a self-cleaning element of the scraper head is proposed for occasionally cleaning the scraper element during the ongoing depolymerization operation. As one of the practical rule realizations is provided to let perform the self-cleaning element under mutual contact with the scraper element relative movement with respect to the scraper element. Such can be done both across the scraping edge and along the same. The actuation preferably takes place via the rotational shaft, in particular by a telescoping movement. Self-cleaning scraping elements are of independent inventive importance.

Another aspect of the invention is a reactor construction which promotes the long-term availability of the depolymerization plant. In that regard, it is proposed that the reactor, together with its heating separately from a reactor lid with the distillation column can be separated by lowering and exchanged for a new or overhauled reactor. If the reactor is pot-shaped and insertable into a heating mantle, the reactor may be e.g. be quickly replaced for overhaul purposes. Flow guiding elements on its outer surface allow effective heat guidance both during heating, during temperature maintenance and during cooling. This aspect of the invention is also of independent inventive significance.

The above-mentioned and the claimed components to be used according to the invention described in the exemplary embodiments are not subject to special conditions of size, shape, material selection and technical design, so that the selection criteria known in the field of application can be used without restriction

Further details, features and advantages of the subject of the invention will become apparent from the subclaims, as well as from the following description of the accompanying drawings and table, in which - by way of example - an embodiment of a catalytic depolymerization is shown.

In the drawing show: Fig. 1 is a block diagram of a Depolymerisationsanlage;

Fig. 2 is an overview view of the practical construction of a depolymerization plant;

3 is a schematic representation of the reactor of a depolymerization plant including the reactor heating as a schematic representation in vertical section through the reactor center.

4 shows a detail view of the coupling of a scraping head to a rotating shaft for a reactor according to FIG. 3;

Fig. 5 of the same reactor is a sectional view (section along the line

V-V) according to FIG. 3, which shows a scraper element held and moved by a receptacle;

Fig. 6 of the reactor of Figure 3 is a perspective view of the outside view;

FIG. 7A shows a scraping head in the scraping position for a depolymerization reactor; FIG.

Fig. 7B the same scraper head in self-cleaning position;

8A shows an alternative embodiment of a scraping head in the scraping position;

Fig. 8B of the same scraper head an enlarged sectional view in a position during the self-cleaning of the scraper head and

Fig. 8C from the same scraper head (in the position corresponding to Fig. 8B) a further enlarged detail. The block diagram of Figure 1 shows that an existing made of plastics and waste oil raw material 1 is heated in a preheater 2 to 250 ⁰ C and subsequently a device for pressure injection, such as for injection molding of plastic known pressure and delivery pump (injection 3) is fed , This pump allows the direct injection of the raw material into a cleavage reactor (reactor 4), the liquid content by heating 5 (with eg oil or gas and an exhaust gas temperature of about 800 ° C) at a gap temperature between about 300 ° and 46O ⁰ C, preferably between 340 ° C and 440 ⁰ C and in particular between 390 ° C and 42O ⁰ C is maintained and its waste heat in part in the preheating stage 2, z. B. a recuperator, is recovered. From the reactor 4, a vapor fraction is withdrawn, which is obtained after appropriate treatment, such as a fractional distillation, as product 6. Likewise, in a conventional manner from the reactor 4 of the resulting solid material is removed, usually de-oiled and recovered as residue 7 and optionally further processed.

It is understood that the reactor 4 can be constructed in many different ways, as well as for the heating 5 no very narrow limits.

FIG. 2 gives a basic idea of the possible structure of a depolymerization plant according to the invention. The preheating of the raw material 1 takes place in a conveyor and compressor screw by external heating and / or friction. Various raw materials are supplied at various points, such as plastics, oils, in particular old / flushing oils and optionally additives. After at least partial preheating is a pressure release. In the expansion stage 2A water vapor and other gases can be supplied via an exhaust duct, for example a filter. The now almost or already completely liquid or pasty raw material is conveyed further by means of the outer end of the screw conveyor under possibly further heating and generation of internal pressure and injected into the interior of a pot-shaped, externally heated Depolymerisationsreaktors 4. The reactor lid 4D carries a distillation column 9, which has a top condenser and a product tank, eg downstream of fuel oil / diesel. Swamp products are discharged at 4B for further processing / use. After leaving the depolymerization reactor, the vaporous cleavage products are preferably passed through a high-speed cylinder with a large safety container. This cleans the vapors of aerosols entrained particles via so-called demistors. From there, the desired cleavage products reach the distillation column. The level in the reactor 4 is preferably measured and regulated to a desired setpoint. This is done with known measuring probes, leaving a gas space 4A (see FIG. 3).

By means of a mixing / scraping head which can be seen from FIG. 3, the reactor inner wall 4C is permanently cleaned, solid constituents being fed down the reactor sump in a preferably helical movement. The filling state of the reactor sump with solid constituents is monitored, preferably without contact. The sump product receiving reservoir 4B allows the accumulation of solids in a flow-calm zone.

Fig. 3 shows in the form of a schematic representation (in central vertical sectional view) by way of example a pot-shaped, rotationally symmetrical reactor 4 with a stirrer 8 with a plurality of stirrer arms 8A and wing-like mixing elements 8B, which may consist at least partially of ceramic or graphite material. The mixer elements 8B are adapted to the dome-shaped inner contour, ie, the inner wall 4C of the reactor 4, wherein a comparatively small gap distance S can be maintained. As a result, the inner contour of the reactor 4, which is preferably heated externally, is constantly freed from caking deposits that form. In addition, the mixing of the contents of the reactor prevents overheating of the contents of the reactor near the heat-carrying walls. In the embodiment, the reactor outer wall 4E forms part of a windbox of heating 5. For this purpose, the reactor pot 4G is mounted with its peripheral mouth flange 4G 'on a flange 5A' of a box-shaped heating jacket 5A. Within the heating jacket 5A there is a break-through intermediate bottom 5B, which is supplied via a flexible line 5C from a mixer 5D with eg 560 ° C hot gas. This is created by mixing the exhaust gases of a gas-heated flame, which is mixed via a blower 5E air, for example, to room temperature (RT). The hot exhaust gases leave the heating jacket via a trigger 5F. The reactor 4 is tightly closed by a reactor lid 4D lying on the mouth bottle 4G '. This lid carries a distillation column 9 and receives the raw material feed 4H. He is kept stationary on a suitable rack. For cleaning purposes and the like, the reactor pot 4G together with the heating mantle 5A can be detached from the reactor lid 4D and lowered as shown by double arrows A and subsequently moved out of the position below the reactor lid 4D, eg by pivoting (double arrows R). At the same time, the stirrer or doctoring head to be described can be removed at the same time (FIG. 4). The outlet for residues is correspondingly flexible or detachable connected to a residue line. In the exemplary embodiment, the outlet consists of a reactor sump 4B _{1 provided} with a thermally insulated wall 4B ¹ through the heating jacket or windbox out and intermittently closed with a discharge lock 4J.

As can be seen from FIG. 4, the decoupling of the rotation shaft 4E of a scraper or mixing head represented in FIGS. 7 and 8 can be effected by a pluggable rotary drive connection, so that a vertical play is permitted for the head while the drive motor M with its drive shaft is stationary on the shaft Reactor cover 4D remains.

FIGS. 7A / 7B show a first embodiment of a scraping head 10D, which can be used as a stirrer in the exemplary embodiment according to FIG. In these figures, two side representations with a) and c) and the view from above with b) are designated. From FIG. 7B a), the two approximately quarter-round wings 10B, which together form approximately a crescent shape, can be seen, which act or are formed on their radially outer side as scraper elements 10C. The scraping elements 10C can be attached to the Inner wall 4C of the reactor 4 abut under the weight of the scraping head 10D. During the depolymerization process, the scraping head 10D, which also acts as a mixer, is rotated slowly, for example at 5 to 10 revolutions per minute. The reactor walls are kept free from deposits. After a certain period of operation, which can be determined by experience or measurement, the scraping head 10D is cleaned by continuous rotation or during interruption of the rotation by a self-cleaning element 10G. This is simulated in the embodiment of the sickle shape of the wings 10B and is during the normal scraping operation in a position spaced from the reactor wall position, as shown in Figure 7B. The self-cleaning element 10G is connected to a drive element 10H, which is telescopically guided in or on the rotation shaft 10E. By a telescoping movement of the driving member 10H, the self-cleaning member 10D is vertically displaced. In this case, his scraping edge 10G ^{1 is applied} to the wings 10B and removes any caking schabend from the front in the direction of rotation wing surfaces close to or up to the scraping edge of the scraper element 10C zoom. This scraping self-cleaning step can also be done by multiple up and down movement. - Alternatively, it is also possible to perform for self-cleaning, the relative movement between self-cleaning element and cocking element so that the self-cleaning element remains in its original position and the cocking element is pulled up by a suitable amount and then lowered again.

In the embodiment shown in FIGS. 8A to 8C, the scraper elements 10C are provided with cross-sectionally C-shaped profiles which adjoin the lower end of a rotary shaft 10E and each receive a driving element 10H in a guiding manner. A self-cleaning head 10G "is also routed and abutted against the scraper 10C. This self-cleaning head is connected to one end of the associated driver 10A and thereby travels along the scraper edge as the driver 10H is telescopically moved relative to the rotary shaft 10E. The figures show different intermediate positions of the self-cleaning head. This knows in the illustrated embodiment, for example, a U-shape, wherein the U-legs do not project beyond the scraping edge of the scraper element 10C to the outside. The possibilities of use correspond to the exemplary embodiment according to FIGS. 7A to 7C.

Incidentally, the scraper elements can be designed in very different ways. In the embodiment according to FIG. 5, the scraper element 10C consists of a material profile held by a receptacle 10F with the interposition of a separating layer 12A, wherein the material can be selected according to the desired wear resistance or / or reactor wall protection. In the embodiment, the wear is already well advanced, so that the receptacle 10F almost touches the reactor wall. If the wear has progressed so far that such a contact occurs, the receptacle 10F and the scraping element 10C are electrically conductively bridged by the reactor wall 4C. An evaluation circuit then determines the permissible limit wear and states that the cocking element 10C is to be replaced.

From Figure 6 it can be seen that the reactor pot 4G is provided on its outer wall 4E with flow guide elements 4F which promote efficient heating or cooling. In particular, a circulation flow of the heating air can be achieved. The heating jacket 5A of the heating 5 can be shaped accordingly to further promote this purpose. Likewise, the flow guide can be adapted to the inner contour of the heating jacket 5A. By a fixed connection of the flow directing elements with the outer wall of the reactor, a particularly rapid exchange of the reactor pot is possible because it can be separated from the heating jacket in a simple manner. LIST OF REFERENCE NUMBERS

1 raw material 8 Ruhrer

2 preheating stage 8A arms

2A expansion stage 8B mixer elements

3 injection 9 distillation column

4 reactor 25 10 cocking device

4A gas chamber 10A arms

4B sump 10B wing

4B ¹ wall 10C scraping elements

4C inner wall 10D scraper head

4D reactor cover 30 10E rotation shaft

4E outer wall 10F recording

4F flow guide elements 10G self-cleaning element

4G reactor pot 10G 'scraping edge

4G 'mouth flange 10G "self-cleaning head

5 Heating 35 10H Drive element

5A heating jacket 12 wear detection device

6 product 12A release layer

7 residue

Claims

claims: 1. A method for depolymerizing raw materials containing kohulstoffwasserhaltigen, such as residues in a continuous process, characterized in that the raw material continuously injected in a vorbeheizten state and in liquid or pasty consistency in a heated gap temperature reactor under pressure and a gaseous fraction for further treatment continuously withdrawn from the reactor and a bottom fraction is discharged continuously or batchwise from the reactor. 2. The method according to claim 1, characterized in that the injection takes place under pressure by means of an injection pump or extruder screw, in particular one such as is known from plastic injection molding 3. The method according to claim 1 or 2, characterized in that the raw material in an injection pump or extruder screw is subjected to a pressure between 100 and 1 bar, preferably between 100 and 2 bar. 4. The method according to any one of claims 1 to 3, characterized in that the preheating is carried out to a temperature of above about 100 ⁰ C, preferably above about 250 ⁰ C. 5. The method according to any one of claims 1 to 4, characterized in that the preheating takes place in two stages, wherein in a first stage raw material with kneading and compressing to remove gases and interspace volumes reaches a temperature of about 100 ⁰ C to 15O ⁰ C. is carried out, and in a second stage with simultaneous pressure build-up, a preheating to about 200 ° C to 300 ° C. 6. The method according to claim 5, characterized in that the first preheating first a pressure relief stage for the separation of vapors, such as water vapor, followed. 7. The method according to any one of claims 1 to 6, characterized in that the raw material contains at least one plastic. 8. The method according to any one of claims 1 to 7, characterized in that the raw material contains at least one oil. 9. The method according to any one of claims 1 to 5, characterized in that heated wall zones of the reactor are cooled by near-wall stirring of the reactor contents. 10. The method according to any one of claims 1 to 9, characterized in that the reactor temperature at the inner wall during depolymerization to a temperature between 300 ° and 460 ⁰ C, preferably between 340 ° and 440 ⁰ C and most preferably between 390 ⁰ C. and 420 ° C is maintained. 11. The method according to any one of claims 1 to 10, characterized in that the raw material is supplied at a distance from the reactor wall, in particular in a central region of the reactor of the liquid subjected to the depolymerization. > Βr. Method according to one of claims 1 to 11, characterized in that heated wall zones of the reactor are cleaned by means of a wall contour formangepass- scraper during depolymerization over its entire surface cyclically of any caking. 13. The method according to claim 12, characterized in that the scraper is subjected to a self-cleaning from time to time. 14. The method according to any one of claims 1 to 13, characterized in that the reactor is replaced by separation from its lid and / or the further treatment stage, such as from a distillation column and lowering and lateral method or pivoting as needed. 15. An apparatus for depolymerizing raw materials containing hydrogen sulfide, such as residues, in a continuous process, in particular according to one of claims 1 to 13, consisting of a heated cleavage reactor (4), a device (2) for preheating liquid, pasty and / or solid hydrocarbon-containing raw materials, a device (3) for feeding the raw material s (1) in liquid or pulpy consistency into the reactor (4) a distillation column (9) fluidically connected to a gas space (4A) of the reactor (4), a reactor sump (4B) for discharging sump material and a scraping device (10) for cyclically cleaning at least the liquid-covered reactor inner walls (4C) during the depolymerization process. 16. The apparatus according to claim 15, characterized by a pressure injection device, such as an injection pump or an extruder screw, for vorbeheiztes raw material (1), which is upstream of the cracking reactor (4) for injecting the reheated raw material under pressure in the cleavage reactor as feed device (3). 17. The apparatus of claim 15 or 18, characterized by a cup-shaped reactor (4). 18. The apparatus according to claim 17, characterized in that the reactor (4) has a rotationally symmetrical inner contour. 19. The apparatus according to claim 18, characterized in that the reactor (4) has an approximately convex inner contour. 20. Device according to one of claims 15 to 19, characterized by a multi-bladed rotating / rotating mixer or stirrer (8) with arms (8A) and wings (8B). 21. The apparatus according to claim 20, characterized in that the wings (8B) at least partially made of temperature-resistant ceramic or graphite material. 22. Device according to claim 19 or 20, characterized in that the wings (8B) of the inner wall contour of the reactor (4) are substantially simulated. 23. Device according to one of claims 15 to 22, characterized in that scraper elements (10C) of the scraper device (10) of the inner wall contour of the reactor (4) are substantially simulated. 24. The device according to claim 23, characterized in that the scraping device (10) has a scraper head (10D), which consists of a rotary shaft (10E) and at least two wings (10B), which have the scraper elements (10C) consists. 25. The device according to claim 24, characterized in that the scraping head 10D bears against the inner wall (4C) of the reactor (4) with its own weight and / or by means of a pressure force maintained above the rotation shaft (10E). 26. The device according to claim 25, characterized in that the rotary shaft (10E) has a, in particular pluggable, rotary drive connection, which allows with increasing wear of the scraper elements (10C) movement of the scraper head (10D) to compensate for the wear clearance. 27. Device according to one of claims 23 to 26, characterized in that the wings (10B) of the scraper head (10D) have a receptacle for a scraper element designed as a wear part (10C). 28. The device according to claim 27, characterized by a separating layer (12A) for avoiding contact between the receptacle (10F) and the scraper element (10C) on the wings (10B). 29. Device according to one of claims 23 to 28, characterized by a wear detection device (12) for the scraper elements (10C). 30. The device according to claim 29, characterized by an electrical circuit which detects an electrically conductive bridging between a scraper element (10C) and a receptacle or attachment of the scraper element (10C) as a signal for advanced wear of the scraper element 10C. 31. Device according to one of claims 23 to 30, characterized by a self-cleaning element (10G) of the scraper head (10D) for occasional cleaning of the scraper elements (10C), in particular during the ongoing De- polymerization operation. 32. Apparatus according to claim 31, characterized in that the self-cleaning element (10G) performs a relative movement to the scraper element (10C) with mutual contact with the scraper element (10C). 33. Device according to claim 31 or 32, characterized in that the self-cleaning element (10G) is displaceable along the scraper element via a drive element guided on or in the rotation shaft (10E). 34. Apparatus according to claim 32 or 33, characterized by one of the contour of the scraper elements (10C) in substantially corresponding contour of a scraping edge (10G ') of the self-cleaning element (10G). 35. Device according to one of claims 31 to 34, characterized in that the self-cleaning element (10G) is arranged on the front side located in the direction of movement of the scraper element 10C. 36. Device according to one of claims 31 to 33, characterized by a along the scraping edge of the scraper element 10C along movable self-cleaning head 10G ". 37. Apparatus according to claim 36, characterized in that the self-cleaning head by means of a along the scraper element (10C) guided flexurally elastic drive element (10H) along the scraper element (10C) is movable. 38. Device according to one of claims 15 to 37, characterized in that the reactor (4) together with its heating (5) preferably separated from a reactor cover (4D), by lowering the distillation column (9) separable and against a new or refurbished Reactor is interchangeable. 39. Device according to one of claims 15 to 38, in particular according to claim 38, characterized in that the reactor (4) is crucible in a heating jacket (5A) can be used. 40. Device according to one of claims 15 to 39, in particular according to claim 38 or 39, characterized in that the reactor on its outer wall Strömungsleitelemente to intensify the thermal contact between the reactor (4) and the reactor outer wall (4E) cooling or heating fluid has , 41. Apparatus according to claim 40, characterized in that the flow guide elements cause a circulating fluid flow at least on a Teilumfangs- area of the reactor (4).