DE2406569A1 - Thermoplastic extrusion press - with two chambers and multiple extruder screws - Google Patents

Abstract

In the extrusion- and injection moulding of thermoplastic resins, alone or in admixt. with stabilising, oxidation-resistant, coloured, rubber-like, reinforcing materials and various additives, by transport of the resin through a melting zone and expulsion through a single extrusion orifice, the operational step of transporting and melting is carried out in a first chamber, the resin and mixt. then being supplied to a second chamber off-set relative to the first chamber and in which the operational step of extrusion of the molten resin is carried out. In particular, the transfer of the molten material from the first to the second chamber takes place in passages in which the material is subjected to considerable shear stresses and to a de-gassing.

Description

Method and device for extrusion of thermoplastic materials.

The present invention relates to a very adaptable method for the extrusion of thermoplastic materials, in which the operations the conveying and melting of the resins are carried out in a first room, during the extrusion operation, axially in a space opposite the first offset second room is carried out. The melted mass is from the first Space into the second space gradually when they are formed through channels or openings That puts a large shear stress on the melted Exercise mass.

The invention also relates to the devices for carrying out the process in question, which are represented by machines, which are essentially a series of screws arranged in the first substantially annular space, at least one other space, axially offset in relation to the first space, in the second space arranged screw and substantially along the generatrix of the first space and have channels or passages carved out towards the end thereof, the thermoplastic compound as soon as it is in the best condition in the first room has reached complete melting, the screw or screws of the second To supply space.

The most popular extrusion machines today consist of screw extruders, which consist of a mostly cylindrical housing in which a single worm is arranged. The thermoplastic material fed in from a funnel occurs in the solid state at the inlet end of the screw, is caused by the action of heat (titer the cylindrical jacket cover) and through mechanical action (friction) softens and melted and is finally removed from the other end of the screw Extruder discharged. The usual extrusion process for plastics is divided thus considered as one, in three different work processes, which in the same way many areas are carried out: 1) Operation or area of promotion of the solid substance or registration> 2) Work process or area the pressing or softening, and 3) operation or area of promotion and the discharge of the softened mass, i.e. the actual extrusion.

The third area is the proportion of undesired> not melted Material is difficult to check, which is why this proportion is often above the desired Limit lies and thus make processing more difficult and reduce manufacturing output will.

With the large number of different types made today Plastics, as well as the various varieties of each type of plastic, are up to now the theories of extrusion and the rheology involved far from being an exhaustive grasp of the problems involved. the end for this reason, the construction of the screws is very difficult and the proportion is not Melted mass emerging from the extruder is almost always assessed incorrectly.

In order to improve the melting, different solutions were made made, such as the attachment of special "torpedoes" to the end of the screw (see Bruce H.Maddock "An Improved Mixing Screw Design" - S.P.E.

Journal July 1967 page 23).

Even if these solutions undoubtedly have certain advantages, so they have still not completely eliminated the problem, so that even that the best system to date or the best device to date in terms of defects on the proportion of melted Has mass, mainly as regards the temporal stability of this proportion.

This resistance is particularly subject to changes when the Plastic is changed or, if the type of plastic is the same, the compound will be changed. Therefore, the usual machines (with a single screw) are missing the desired level of general use and adaptability (in terms of on the various commercially available plastics) and are rather narrow, in terms of their capacity, mode of operation and space requirements.

It is true that special screws (the design of which is explained below becomes known), but they do not solve the problem of adaptability.

A first object of the invention is to propose a method with which the above-mentioned deficiencies are corrected and extruded masses are achieved that contain exceptionally high levels of softened mass.

Another object of the invention is to provide a method to provide which is actually efficient, i.e. with which one decidedly larger Amounts of plastic can be discharged than is possible with the usual methods is possible, with the operating costs correspondingly with retention of others Conditions are lower and where the properties of the extruded mass are not only better, but also more consistent and checked.

Another object of the invention is devices to create which, thanks to their new construction, realize the process in question and a high degree of universal use and adaptability as well as more have high performance capabilities, lower operating costs and little space requirements.

The inventive method is characterized in that the Operations for the promotion and for the melting carried out in a first room that the plastic and the mixture gradually merge after they have softened second room are supplied and the operation for the extrusion of the total Melted plastic is carried out in the second space, which is opposite the first space is axially offset, the transition from the first to the second space takes place via passages in which the melted mass is subject to considerable shear stresses is exposed.

According to an advantageous feature of the invention, the melted Plastic in a completely melted state just in the transition from the first in the second space is subjected to degassing.

According to the invention comprises a machine for realizing the in question standing process, the supply means for the thermoplastic resin (or those Mixtures) to a first space, conveying and melting organs for the resin, which are distributed in the first externally heated room, means of transition of the resin (as it gradually melts from the first space into a second To allow space, third to the molten Resin during of the transition to be subjected to degassing and squeezing out organs, which are in the second Space are located to just the extrusion of the melted, supplied from the first space resin to run.

The machine according to the invention also comprises a heated outer cylinder and within the same at least one further cylinder, which however is only extending a longitudinal portion along the first cylinder, wherein the annular, between the outer cylinder and the inner cylinder existing part the first space forms, on the scope of a number of conveying and melting organs for the Resin are evenly distributed.

In a preferred embodiment, both the conveyor and Melting organs, as well as the melting organs snails, whereby the melting organs are arranged in a circle around at least one central screw. All Melting screws are driven at an unwinding speed of those given to the extrusion screw speeds can be independent. The extrusion screw can also experience displacement and injection molding carry out.

The invention is described below with reference to the accompanying Drawings described in more detail, in schematic form and for example (and non-limiting) represent some preferred embodiments of the invention. Show in the drawings Figures 1 and 2 are two schematic longitudinal partial sections, i.e. the vertical planes contain the longitudinal axis of the machine according to the invention; 2A and 2B show two schematic partial cross-sections according to FIG Machine axis perpendicular planes have the intersection lines A-A and fl-B according to Figure 2; FIG. 3 shows an enlarged section corresponding to FIG to better represent the melted mass from one room to another; the Fig.4 a section corresponding to FIG. 1, but in a more schematic form, in order to better represent the path of the cup.

In FIG. 1, the one on the far right represents the dashed line and with NA denoted part represents a drive of an extruder E according to the invention. With C is the barrel of the extruder E is indicated. The inside of the cylinder C is divided into several ring-shaped, divided concentric areas.

For the sake of simplicity, the interior of the cylinder C is shown in FIG a cylindrical inner wall Ci only divided into two rooms. So that is Interior of the cylinder C in a first annular, peripheral or outer Space SAe formed between the outer wall Ce and the inner wall Ci of the cylinder C. is, and in a second annular inner space SAi, which between the of the Wall Ci is formed in limited areas.

In the embodiment shown in the drawings extends the peripheral or outer annular space SAe becomes larger in the longitudinal direction section along the extruder E, but not along the entire length Longitudinal expansion.

Apart from the longitudinal extension of the drive MA (the, so to speak does not belong to extrusion in and of itself, the cylinder C of the extends Extruder from the inlet end 11 for the cup fed from the funnel T to the outlet end 12 for the extruded mass. The first annular peripheral space SAe extends on the other hand, in longitudinal coloring along a larger section between 11 and 12, but not along the entire distance between 11 and 12.

For example, the first space SAe is between the entry end 11 formed for the resin and the end 14 that is connected to the end of the melting range coincides.

Within the annular space SAe there are n conveying and melting organs OCFn arranged for the resin.

These n organs OCFn are preferably along the central circumference 15 (Figs. 2A and 2B) of the annular space SAe are uniformly distributed. These n funding and opening organs OCFn preferably consist of helical screws, For example screws of the usual type with constant screw pitch and thread thickness. Two organs OCFn-m and OCFn-n can be seen from FIGS. 2 and 4, while in the According to the embodiment shown in FIGS. 2A and 9E, six conveying and melting organs there are those with OCFI, OCF2, OCF3, OCF4, OCF; and OCF6 specified and uniform are distributed along the circumference 15.

The inner, ring-shaped space SAi is, however, with organs OE for the Strangpnssen alone occupied. Any number of these organs OE can also be used to be available. In the preferred embodiment according to Figures 2A and 2B exist the extrusion organs OE from a single screw OE, which is preferably longitudinal extends the entire longitudinal extent of the cylinder C, even if to the actual Machining the resins, the screw OE also have a more restricted extension could.

Surprisingly, it was found that on penetration of the resin fed in from the hopper or hoppers or of the corresponding back-pressing Compounds via the loading nozzles BC in only the conveying and melting organs OCFn and with appropriate heating of the cylinder C, the resin achieves a complete lifting along the entire section OCFn, i.e. along the den Mündstüc # en BC opposite entry section opposite section. If along this section indicated with 17-18 in the inner wall Ci of the cylinder C slots or passages are provided, the unpredictable phenomenon occurs on that the resin or compound (squeezing out) from the outer space SAe (i.e.

from the conveying and melting organs OCFn) into the inner space SAi (i.e. to extruder OE) occurs as soon as the resin has reached the desired complete level Melting reached.

Therefore, the arrangement and the dimensions of the slots PF are special decisive. Become the same in the area of the organs OCFn and of the beginning of the organs OE and must have a length 17-18 so that from space SAe to space SAi the thermoplastic mass can be transferred as soon as this has melted. The width and depth of the slots or passages PF must also have such dimensions that a significant shear stress is exerted on the melted mass, which is transferred to the screw OE, which brings the mass to the extrusion mouthpiece at the end 12, where the mass is not without completely melted portions are discharged. The length of the passages or slots PF, i.e. the distance between 17 and 13, is between 5% and 60%, preferably between 15 and 35% of the total length of the organs OCFn. The peripheral opening the slot is within a small percentage range in relation on the entire circumferential extent of the inner wall Ci.

Preferably, the end of all screws OCFn is with a "torpedo" TOCF provided. These only have the job of being melted, at the ends of the Snail OCFn located mass via the channels 20 and 20t (in the knee ME E of the ,! and Ce worked out) to the inner space SAi and therefore to the second section of organ 0E to pass over.

As stated above, MA denotes schematically the complex of Drive mechanisms of the conveying and lifting organs OCFn and the extrusion organs OE.

One driven by a motor, not shown wave 31 operates a gear 32, which in turn moves a gear 33 that controls the wheels 34 and 341, each of which is attached to an OCFi body. In Fig.1 operate the two wheels 34 and 341 which are assigned to the organs OCFn-n and OCFn-m Waves 35 and 36.

Each of these cells is mounted on thrust bearings 37.

A shaft 40 is driven by a motor not shown (but the same can be, which drives the shaft 31) moves and operates the shaft 41, which with the central screw OE is connected. The shaft 40 is supported on thrust bearings 42. It seems clear that the transmission gear NA is not an essential part of the invention and can be carried out differently than shown in FIG.

At this point it should be emphasized that the e.g.

Part of the screw OE lying between points 50 and 51 is missing could. However, it is advantageous to have a screw OE available that extends from 12 to 11 so as to be the portion between 50 and 51 essentially to use for the transmission of motion (in section 50-51 the worm the thread is easily missing).

FIG. 4 is a schematic repetition of FIG.

1, in order to determine the path of movement of the resin coming from the hopper T. to represent.

At the entrance of the cylinder C, the resin penetrates through the mouthpieces BC only in the space SAe, as this is indicated by the arrows fi.

The conveying and melting organs OCFn in the area SAe cause the advancement of the resin due to the heating of the cylinder C. and the pressure exerted on it by the organs OCFn gradually melts. In 18 the opening PF begins, which extends to 17 and is arranged in such a way that that in FIG. 18 the complete melt area of the resin begins, which according to FIGS Arrows fp now enters the inner space SAi and therefore on the central scroll OE, while the resin itself gradually melts.

The last part of the resin reaches the screw OE according to the arrows fr on channels 20 and 20 ?. All of the completely melted on the snail OE transferred resin, is pushed forward by the same and at the end 12, as with indicated to the arrow.

2 is a section similar to the sections of FIGS. 1 and 4, however, with a longitudinal plane corresponding to the section line X-X in FIG. 2A was made. As can be seen from this figure, this plane runs through the full area between two organs OCF, e.g. between OCFI and OCF6.

This area is preferably from the degassing channel 60 for the melted Resin crosses, this channel extends to the mouth DG for gas extraction.

The channel 60 connects the annular inner region SAi (i.e. OE) with the space outside the wall Ce of the cylinder C (see Fig. 2A). The ones on the Snail OE is the mass coming from the organ OCFn namely completely melted and can therefore be degassed at the moment in which it emerges from the slots PF and before it is conveyed to the exit of the extruder will. In FIG. 2, RE indicates the heating coils or resistors. the FIG. 2B is a section similar to the section 2A of FIG. 2, but with a Plane was made that runs through the feed mouth BC and the cutting line B-B owns. This Fig. 2B shows the mouth BC, which only the outer space SAe, ie: feeds the organs OCFn. The through-holes indicated with 65 are for circulation any thermally influencing agent.

FIG. 3 is a section similar to the section in FIG is enlarged in order to better show the downturn area PF of the melted mass, which gradually expand as they advance along the organs OCFn-m in the section between 17 and 18 forms. The torpedo TOCF is also shown enlarged with its Channel 20.

The arrangement that the machine adopts when the organ or the Extruder screw OE that works for injection molding is not very different from that shown in Figs. It turned out to be surprising found that the method and device according to the invention have good advantages can also be achieved in injection molding, in which the extruder screw is rotating The punch worm is made with a rotary motion and with a displacement along their longitudinal axis is operated. The screw IE is on the head part with a usual sealing valve provided that the backflow of the mass during injection molding prevented. The screw OE is shifted by an oleodynamic unit issued that controls a piston. Of course, any known mechanism can be used be used that of the screw OE the displacement and the orbital movement, such as can lend in the usual injection screws.

Among the most significant and advantageous features of the invention the following should be emphasized.

a) The organs or snails OCFn only have the task, the mass to promote and melt down (they do not, however, have the task of which is suitable for being removed from the continuous casting area). This limitation of tasks to the usual snails gives the first one Part of the process is adaptability and allows the same snails for the processing of different masses and different varieties of the same mass to use.

The difference between the snails and the species OCFn is therefore only necessary if the apparent specific gravity changes significantly, i.e. in the continuous casting of powdery instead of granular mass (in general, at of the same type of mass the weight of a liter of powdery mass lower than one liter of granular mass).

b) The fact that the mass is gradually melting from the outer snails OCFn to the inner ones Screw OE passes over, zero always allows the resin to be degassed. The extruder according to the invention is therefore more advantageous than any conventional extruder for this reason alone Type without degassing.

c) The speed or number of revolutions of the organs OCFn can be compared that of the organ OE can be changed at will.

The increased speed of rotation of the OCFn type of screw there is no need to worry that too much air or volatile substances have been taken in could be, since the same in any case at the transition of the melted mass from the outer space into the inner space via the slots PF, i.e. during degassing, was completely withdrawn.

d) The transition of the melted mass, during its formation, prevented from snails of the OCFn species to the snails of the OE species, that this mass is further processed and therefore overheated. At the same time affects this smaller bulk processing on power consumption which is smaller than in a conventional extruder.

As for the reduced machining and the lower power consumption is concerned, it can be said that the method according to the invention has the same advantages which are attributed to the special snails that are nowadays used for the most advanced, like e.g. the snail type blaillefer (see C.tIaillefer A Two Channel Extruder Screw'1 Modern Plastics 40, page 132, 1963).

e) Since the mass is melted by the snails according to the type OCFn transferred to at least one screw OE via passages with rather small dimensions (depending on the mass, the cutting speeds are between 100 and 300 sec), is the surface of the melted one exposed to degassing Much larger mass than in an extruder with a conventional degassing system.

The surface exposed to degassing is in the extruder according to the invention a dm3 mass is very large, e.g. 300 dm, while in a conventional extruder the exposed surface is much smaller and, at best, is 30 dm2, for example.

f) The central extrusion screw OE can control the rotational speed change independently of the conveying and melting screws. This enables that extruder according to the invention a considerable adaptability, as the following Defects of the extruder can be eliminated with the conventional degassing systems.

f) It is not necessary depending on the profile of the screw (with degassing) to change after the pressure of the extruder head, or in its subordination, it is no need to attach a valve to the extruder head to regulate the counter pressure. (It is known that with a profile that does not match the pressure on the screw head is, there is a risk that mass will escape through the degassing, or the delivery rate is pulsating).

f) The extrusion screw OE does not have to be used in the event of a change in the type of mass be changed, since the task of the extrusion organ according to the type OE only therein there is to convey the melted amount brought about by the screws OCFn, what can happen with a mere change in speed.

The statements made under points f and f can be can be proven by the formula of the delivery rate (Q) of an extrusion screw Q = K. N-K2f (# 8 P) f (m) (1) where Kt and K2 are two constants derived from the geometric Characteristics of the screw depend on, ft ß P) is a function of the pressure difference taken into account between the head and the beginning of the worm, f (m) is a function, which takes into account the rheological properties of the mass, and N the speed the snail is.

that From the above formula (1) it can be seen / a certain delivery rate Q with an appropriate speed N (with K1 and K2 as constants) at any Values of f (# #P) and f (m) can be achieved.

For a Newtonian liquid, the following applies with Q = flow rate cm3 D = diameter of the screw cm h = height of the thread cm d = angle of incline of the thread degrees N = speed rev / sec.

L = screw length cm PP = (pressure on screw head minus pressure on 2 screw start) + = viscosity kg.sec / cm2 f (h P) = bP f (t) = I / 7t The formula (2) shows that if either the (pressure difference) or the rheological properties (e.g. viscosity µ)) or both of these parameters change, it is always possible to choose an appropriate speed in order to achieve the desired flow rate Q.

In the known technology, however, the adaptability is lacking can be better recognized below.

g) The extrusion screw OE thus conveys a securely melted one Wet. This means that a screw of smaller dimensions (e.g. D = 120 mm) can also be used for Much larger flow rates can be used than a conventional extruder because there are no problems for an increase in the rotational speed.

In a conventional extruder, there are problems for the elevation the speed of rotation in the conveying areas of the non-melted mass or in the conveying and pressing areas.

If namely the cutting speeds acting on the mass can be considered in conventional extruders, one can determine that these speeds increase with the increase in diameter the Screws are getting smaller and smaller, precisely because of the rotational speeds of the screw themselves are lower.

The cutting speed is namely where D and h are normally increased proportionally to each other as the maximum speed N decreases.

if in a conventional extruder with a diameter of D = 120 mm, the screw with a speed of 150 rpm. could go around like this is normal for extruders with a diameter of D = 45 mm to D = 60 mm, so could the production services are doubled compared to the current services, although maintaining the same cutting speed or the same mass processing will.

In the extruder according to the invention, the screw can have a diameter from 120 mm at 150 rpm. circulate and therefore deliver twice the power than that Screw with a diameter of 120 mm in a conventional extruder.

h) Another advantage is given by the possibility of masses of various types to be brought directly into the central screw, so that the masses even the melted mass when mixing, without excessive processing to experience. This possibility is of the greatest usefulness when using fiberglass, asbestos etc. Reinforced strands are made where a good one Incorporation of the reinforcement material while avoiding the reinforcement fibers is required.

In this case the fiber feed can pass through the degassing orifice or take place via another appropriately provided loading opening.

i) Among the other advantages, the one that consists of two or more different ones with the outer scrolls of the OCFn type To convey masses and to melt them, with the masses in the central screw Do not mix until they have melted.

1) Another advantage is the dimensions of the extruder, because with the same performance, the length of the extruder according to the invention by half is shortened compared to that of a conventional extruder. A like in Fig.1 and 2 shown extruder, the six screws OCFn with a diameter of D = 60 mm, with a length of L = 14 D and a screw OE with a diameter of D = 120 mm, which extends by 8 D beyond the slots PF in the longitudinal direction extends, has a 1300 mm long cylinder, while an extruder with the conventional one Degassing has a 3600 mm long cylinder.

m) As far as the manufacturing costs of the machine according to the invention are concerned, it has to be taken into account that the mechanical part is rather simple and that the Dimensions, weight and used power are lower than in an extruder with the conventional one Degassing and with the same Delivery rate.

For this reason, the manufacturing cost is easily competitive and are all the more advantageous, the larger the delivery rates.

The following examples illustrate some of the features of the invention however, without restricting the invention itself.

Examples The average delivery rate of the extruders with degassing and with a diameter that is available from different manufacturers of extruders offered on the world market, for example, can be cited as ABS and polystyrene (shockproof) 500 - 600 kg / h polyethylene 400-- 500 kg / h polypropylene 300 - 400 kg / h The same conveying capacities can be achieved with that of the applicant Extruder can be achieved, which six screws OCFn with a diameter of D = 60 mm has # -, which with 120 Z 150 rpm. revolve, and with a central snail OE with a diameter of D = 120 mm, the 80 - 120 rpm. running around.

An extruder according to the invention, which has a cylinder that merely is 300 mm longer than that in the previous example and that with six peripheral Screws OCFn with a diameter of D = 80 mm, which with 120 - 150 U / # lin. circulate, and with a central screw OE with a diameter of D = 120 mm, which with 120 . 150 U / # lin. circulates, is equipped, has the following conveying capacity ABS and polystyrene (shockproof) 800. 1000 kg / h polyethylene 600 ^ 800 kg / h polypropylene 500 - 600 kg / h.

These conveying lines are conventional with an extruder Degassing with a diameter of D = 150 and with a cylinder length, however is at least 4500 mm, difficult to achieve.

A clearer picture of the current situation in the field of conventional Extruder can be supported by an important statement on the part of Messrs. R.T. Fenner and S.G.W.G Watt in the article "Continuous ram extrusion of polymers: preliminary investigations" (Plastics and Polymers - August 1972, page 199).

'' The single-screw extruder is still the most widely used today Machine for processing polymer materials. To meet the requirements, Many larger extruders are now manufactured in terms of their diameter and length The users however, the extruder encounter ever greater problems due to the excessive extrusion temperatures, of shear stresses and thermal degradation. For construction improvement Much can be inferred from the snail and much has been done, whereby however, there is a limit to what can be done. For example, the increased Rotational speeds the snail causes a larger inclusion of air and volatile substances, which, on the other hand, are ejected through the funnel at lower circulation speeds would have been.

Thus the extruder with degassing has been developed.

All the improvements in the design of the augers have however, the result is that the use of a snail is increasingly limited Range of substances and working conditions is limited, with thus adaptability of the extruder is reduced. The screw extruder is a machine namely not particularly adaptable. Apart from regulating the temperatures, which is not particularly effective in the large extruders, is the only immediate one Means for adjusting the speed of rotation of the screw.

The delivery rate, the temperature of the melted mass, the outlet pressure and the degree of mixing are strictly dependent on each other and cannot can be regulated independently of each other. It is easily a single screw extruder To be criticized, so far, however, no alternatives recognized by all have been found The invention now overcomes these difficulties by providing extruders that are certainly more adaptable than the conventional extruders and whereby that alternative was realized that has not yet been conceived and was carried out, even if it was desirable and therefore sought by many (It is noteworthy that one of the authors of the above article, namely R.T. Fenner, also the well-known author of the book Extruder Screw Design " Verlag ILIFFE 1970 ist) For better understanding, the invention has been incorporated by reference on embodiments shown in the drawings. However, it lies suggest that the invention is not limited to these embodiments, but that different variants and modifications are possible, which in the wider area of the present invention and so accessible to those of ordinary skill in the art are.

Claims (12)

P A T E N T A N S P R Ü C H E 5 C Hv E E 1. Process for extrusion and injection molding of thermoplastic resins those alone or in a mixture with stabilizing, oxidation-resistant, coloring, rubbery, reinforcing materials and various additives are present by means of Conveyance of the resin itself through a melting area and by means of discharge characterized by an actual extrusion opening in that the operations the promotion and the Aufschnlelze; 's in eilioll. first room, that the resin and the mixture gradually melt after they have melted in the first paum a second room can be supplied and the operation of extrusion of the complete The melted resin runs in the second space, opposite the first Space is axially offset. 2) Method according to claim, arc characterized in that the transition voiil first in the second room via passages in which the melted wet is exposed to significant shear stresses 3) Procedure according to the response 1 and 22 characterized in that da.- resin in rolling melted state in the transition from the first to the second space of a degassing is subjected. 4) Method according to the preceding claims, as by £ enaseichne let. the first is hardly substantially an annular ring, and that the second Room. is cylindrical space that is coaxial within within the first Space arranged; is. 5) Method according to the preceding claims, characterized in that that the resin or its mixture is in a firm initial state in the first Space entered and the second space through one essentially to the axis of the two Crooked vertical displacement is fed. 6) #; machine for implementing the method according to the preceding Claims, characterized by: supply means for the thermoplastic resin (or its mixtures) to a first space, conveying and softening organs for the resin, which are distributed in the first, externally heated room, about the transition of the resin (as it gradually melts) from the first space into a second ## aum, means to dissolve the molten resin during the transition from degassing to undergo, and extrusion means, which are located in the second room, to only carry out the extrusion of the melted resin supplied from the first room. 7) Machine according to claim 6, characterized by a heated outer cylinder and, within it, by at least one further cylinder, which, however, extends only a longitudinal section along the first cylinder, the annular one existing between the outer cylinder and the inner cylinder Part of the first room forms, on the intermediate perimeter of a number of conveying and Melting organs for the resin are uniformly distributed. S) machine according to claim 7, characterized in that the first Outer cylinder and the second inner cylinder with limited extension are coaxial with one another and have at least one extrusion element for the melted, resin received from the first room are provided. 9) Machine according to the preceding claims, characterized by Slits provided in the inner cylinder and through degassing channels starting from lead from these slots to the outside. 10) Machine according to the preceding claims, characterized in that that the conveying and melting organs and the extrusion organs are screws. 11) Machine according to the preceding claims, characterized by two cylinders coaxial with one another, of which the one with the smaller extension has a smaller diameter, this cylinder having a first annular one common space in which a number of conveyor and melting screws is arranged along the circumference, and a second cylindrical inner space forms, in which an extrusion screw is arranged, the inner cylinder at one end slots for the passage of the resin as it gradually melts having and wherein the conveyor and Aufscnmelzungssc -hnecken operated by mechanisms that can give the screws rotational speeds that of those the extrusion screw are independent. 12) Machine according to claim 11, characterized in that the extrusion screw also undergoes a shift to transfer molding the resin.