The present invention relates to a process for hydrolytically depolymerizing a polyamide prepared from e-caprolactam and an apparatus for carrying out a process for hydrolytically depolymerizing a polyamide prepared from e-caprolactam, preferably for carrying out the aforementioned process.

Polyamide, and in particular polyamide 6 being characterized by the formula (-NH-(CH2)5-CO-) _n , can be found in numerous materials, such as packaging, engineering plastics from automotive and textile filaments. The latter represents about 40 % of the polyamide 6 global market. At present, only a very small part of the textile filaments is recycled while it represents a significant percentage of the global CO2 emissions. There is thus a need to recycle polyamide 6 from such materials. Processes for alkaline depolymerizing a polyamide exists. Thus, there is a need to provide an improved process for depolymerizing a polyamide able to overcome these issues.

Surprisingly, it was found that the process of the present invention according to which polyamide is hydrolytically hydrolyzed is more robust and is cheaper. Using a hydrolytic process compared to an alkaline depolymerization process permits to reduce the CO2 footprint.

Therefore, the present invention relates to a process for hydrolytically depolymerizing a polyamide prepared from e-caprolactam, said polyamide being contained in a solid material M, the process comprising

(i) providing the solid material M containing the polyamide, M having a temperature TM, wherein TM<TP, TP being the melting point of the polyamide;

(ii) providing a liquid aqueous stream Sw, wherein from 90 to 100 weight-% of Sw consist of water and wherein Sw has a temperature Tsw, wherein TS >TP;

(iii) feeding the solid material M provided according to (i) and the liquid aqueous stream Sw provided according to (ii) into a chemical reactor unit Ru, obtaining a mixture;

(iv) subjecting the mixture obtained according to (iii) in Ru to a depolymerization temperature TD at a depolymerization pressure PD, wherein TM<TD<TSW, obtaining an aqueous mixture containing e-caprolactam dissolved in water;

(v) removing an aqueous liquid stream SR from Ru, SR containing e-caprolactam dissolved in water.

Preferably, TD is in the range of from 230 to 320 °C, more preferably in the range of from 250 to 300 °C, more preferably in the range of from 270 to 295 °C.

Preferably, Tsw is in the range of from 240 to 350 °C, more preferably in the range of from 260 to 330 °C, more preferably in the range of from 290 to 325 °C.

The excess heat of the liquid aqueous stream Sw (Tsw) melts the solid material M containing the polyamide which is preferably in the form of granules, and provides the needed reaction enthalpy. Any additional heat required to maintain the reaction temperature can be provided through a heating jacket of the reactor unit Ru, using hot oil as heating medium.

Preferably, AT=TSW-TD is in the range of from 10 to 70 °C, more preferably in the range of from 10 to 50 °C, more preferably in the range of from 10 to 30 °C.

Preferably, PD is in the range of from 40 to 120 bar, more preferably in the range of from 50 to 100 bar, more preferably in the range of from 60 to 90 bar.

Preferably from 91 to 100 weight-%, more preferably from 92 to 100 weight-%, more preferably from 95 to 100 weight-%, of Sw consist of water.

Preferably, the solid material M comprises, more preferably consists of, waste material, wherein said waste material more preferably comprises textile waste material.

Preferably from 10 to 99 weight-%, more preferably from 30 to 98.5 weight-%, more preferably from 50 to 98 weight-%, more preferably from 80 to 98 weight-%, of M consist of the polyamide; or preferably from 10 to 100 weight-%, more preferably from 30 to 100 weight-%, more preferably from 50 to 100 weight-%, more preferably from 80 to 100 weight-%, of M consist of the polyamide.

Preferably, M is in the form of granules, wherein the mean diameter of the granules is preferably in the range of from 0.5 to 10 mm, more preferably in the range of from 1 to 7 mm, more preferably in the range of from 2 to 4 mm.

According to (iii), M and Sw are preferably fed into Ru at a mixing ratio mw/kg : mp/kg, defined as the amount of water contained in Si, mw, relative to the mass of polyamide contained in M, mp, in the range of from 1 :1 to 20:1 , more preferably in the range of from 2:1 to 15:1 , more preferably in the range of from 5:1 to 10:1.

The mixing is preferably ensured by dosing the amount of water (Sw) stepwise with ongoing reaction time, and dosing the solid material M in the reactor unit Ru.

Preferably, M and Sw are fed into Ru one after the other. More preferably, Sw is fed into Ru and subsequently M is fed into Ru containing Sw.

Prior to being fed into Ru, M is neither subjected to melting nor subjected to mashing.

Preferably, the chemical reactor unit Ru comprises z chemical reactors R, i=1 ...z, wherein z is in the range of from 1 to 10, more preferably in the range of from 2 to 8, more preferably in the range of from 2 to 6, more preferably in the range of from 2 to 5, more preferably in the range of from 2 to 4, more preferably 3 or 4, more preferably 4. Preferably, z>1 and at least two reactors R, more preferably the z reactors R, are serially coupled.

Preferably, the z reactors R are serially coupled, wherein according to (iii), M and Sw are fed into R, i=1 ; an aqueous liquid stream Sj containing e-caprolactam dissolved in water is removed from R and fed into R+i, i<z; according to (v), SR is removed from R _z ; wherein in every reactor R, a depolymerization temperature TDI at a depolymerization pressure poi are maintained, wherein, independently of each other, TDI is in the range of from 230 to 320 °C, more preferably in the range of from 250 to 300 °C, more preferably in the range of from 270 to 295 °C, and wherein, independently of each other, poi is preferably in the range of from 40 to 120 bar, more preferably in the range of from 50 to100 bar, more preferably in the range of from 60 to 90 bar.

Preferably, maintaining a depolymerization temperature TDI in a reactor R comprises heating the reactor contents of R, more preferably indirectly heating the reactor contents of R, wherein more preferably, maintaining a depolymerization temperature TDI in a reactor R comprises heating the reactor contents of R by passing a heating medium through a heating jacket of R. The heating medium is preferably hot oil. However, it is noted that other heating media known by the skilled person can be used for passing through the heating jacket of R.

Preferably, the z reactors R are vertically arranged, with Ri being the top-most reactor and R _z being the bottom-most reactor, wherein Sj obtained from R is transferred to R+i by gravity, more preferably by gravity only.

Preferably, at least 1 , more preferably z reactors R, are configured as non-stirred reactors or as non-circulation reactors, more preferably as non-stirred reactors and non-circulation reactors.

The system is preferably operated without stirrer and without circulation pump. That avoids difficult sealings, i.e. high pressure sealings, for the stirrer and pump.

As mentioned in the foregoing, the mixing is preferably ensured by dosing the amount of water stepwise with ongoing reaction time, and dosing the liquid solution, for example, from reactor Ri by gravity to reactor R2 and R3 after parts of the reaction time.

Preferably, the reactors Ri to R _y .i are operated in batch mode and the reactors R _y to R _z are operated in continuous mode, wherein y>1 and y<z, wherein y is more preferably z. Preferably, the residence time in one or more of the reactors Ri to R _y .i, more preferably in the reactors Ri to R _y .i, is in the range of from 5 to 40 minutes, more preferably in the range of from 10 to 30 minutes, more preferably in the range of from 15 to 25 minutes.

Preferably, the residence time in the reactors R _y to R _z , wherein y is more preferably z, is in the range of from 1 second to 40 minutes, more preferably in the range of from 2 seconds to 30 minutes, more preferably in the range of from 3 seconds to 25 minutes.

Preferably, the overall residence time in the chemical reactor unit is in the range of from 15 to 160 minutes, more preferably in the range of from 30 to 120 minutes, more preferably in the range of from 45 to 100 minutes, more preferably in the range of from 60 to 80 minutes.

More preferably, four identical chemical reactors R1-R4 are arranged in series. The first three, R1- R3, are operated in batch mode, all of said reactors having low residence time and the last, R4, in continuous mode to enable continuous feeding of the downstream process steps.

As to the feeding of Sw and M, it is preferred that M and Sw are fed into R one after the other. More preferably, Sw is fed into R and subsequently M is fed into R containing Sw. After a time T, Sj is removed from R and fed to R+i .

Preferably, providing a liquid aqueous stream Sw according to (ii) comprises

(11.1 ) separating at least a part of the water contained in the aqueous liquid stream SR removed from Ru;

(11.2) feeding at least a part of the water separated according to (ii.1 ) back into the process as part of the stream Sw.

This is in particular realized during the on-going process, this permits to recycle water which permits to reduce environmental footprint and reducing costs.

Preferably, providing the solid material M containing the polyamide according to (i) comprises

(1.1 ) providing the solid material in a first zone of a two-zone receiving and discharge means RDM, wherein the temperature of M in said first zone is in the range of from -10 to 50 °C, more preferably in the range of from 15 to 40 °C, more preferably in the range of from 20 to 30 °C, more preferably at atmospheric pressure;

(1.2) passing the solid material provided in the first zone to a second zone of the RDM, wherein said second zone comprises outlet means being connected via a connecting line with the reactor unit Ru;

(1.3) feeding a gas stream into the second zone of the RDM comprising the solid material, said gas stream having a pressure PG with PG>PD, wherein PG is more preferably in the range of PD<PG^ (PD+5 bar), wherein the gas stream has a temperature more preferably in the range of from 10 to 40 °C, more preferably in the range of from 15 to 30 °C;

(1.4) passing the solid material from the second zone of the RDM into the connecting line according to (i.2); wherein the two-zone receiving and discharge means RDM is more preferably a two-zone hopper. The raw material or feed, namely the solid material M, is preferably delivered as granules into silos using trucks and/or big bags. The silos could be under N2 atmosphere to prevent the risk of dust explosion. Granules are preferably fed pneumatically from these silos to a two-zone receiving and discharge means RDM, preferably a hopper, more preferably a two-zone hopper. It is also conceivable that a big bag unloading station discharges directly into the hopper.

Preferably, the receiving and discharge means RDM, more preferably a two-zone hopper, unloads the feed mixture, namely the solid material M, into the reactor unit Ru, more preferably into the first reactor R1 of the reactor unit, using gravity.

Preferably, the gas stream according to (i.3) comprises one or more of nitrogen and water,

The present invention further relates to an apparatus for carrying out a process for hydrolytically depolymerizing a polyamide prepared from c-caprolactam, said polyamide being contained in a solid material M, preferably for carrying out a process according to the present invention, the apparatus comprising

(a) a reactor unit Ru comprising z chemical reactors R, i=1 ...z, wherein z is in the range of from 2 to 8, more preferably in the range of from 2 to 6, more preferably in the range of from 2 to 5, more preferably in the range of from 2 to 4, more preferably 3 or 4, more preferably 4; wherein the z reactors R are serially coupled and vertically arranged, with R1 being the top-most reactor and R _z being the bottom-most reactor; wherein R1 comprises inlet means IM for feeding the solid material M into R1 and inlet means l _S w for feeding a liquid aqueous stream Sw into R1, said inlet means being located at the top of R1; wherein every reactor R, comprises outlet means O _Ri for removing an aqueous liquid product stream Sj from R; wherein a reactor R, i>1 , comprises inlet means l _R for feeding the aqueous liquid product stream Si-1 removed from R via a connecting line CM into R; wherein the outlet stream removed from R _z is an aqueous liquid stream SR, SR containing E- caprolactam dissolved in water.

Preferably at least one reactor R, more preferably all reactors R, are equipped with a heating jacket for passing a heating medium through said jacket. The heating medium is preferably hot oil. It is noted that other heating medium known the skilled person can be used for being passed through the heating jacket of R.

Preferably at least 1 , more preferably z reactors R, are configured as non-stirred reactors or as non-circulation reactors, more preferably as non-stirred reactors and non-circulation reactors.

Preferably at least one connecting line Ci, more preferably all z-1 connecting lines Cj are configured to allow transferring SM from RM to R by gravity, more preferably by gravity only. Preferably at least one connecting line Ci, more preferably all z-1 connecting lines Cj are not equipped with pumping means, more preferably not equipped with conveyor means.

Preferably the reactors Ri to R _y .i are batch mode reactors and the reactors R _y to R _z are continuous mode reactors, wherein y<1 and y<z, wherein y is more preferably z.

Preferably the apparatus further comprises

(b) separating means SEw for separating water from SR; wherein said separating means SEw is arranged downstream of Ru, comprises inlet means ISE for passing SR into SEw, the ISE being connected via a connecting line with the outlet means OR, of the reactor R _z ; and further comprise outlet means OSE for removing water from SEw, the OSE being connected via a connecting line with the inlet means Isw of the reactor Ri.

Preferably the apparatus further comprises

(c) a two-zone receiving and discharge means RDM for metering the solid material M to the reactor unit Ru; wherein said two-zone receiving and discharge means RDM is arranged upstream of Ru, wherein the first zone of RDM is arranged vertically above the second zone of RDM and comprises inlet means l _RD for receiving the solid material M, wherein the second zone of RDM comprises outlet means ORD for removing the solid material from RDM, the outlet means ORD being connected via a connecting line with the inlet means IM of the reactor Ri, wherein the RDM further comprises closing and opening means arranged between the first zone and the second zone of the RDM.

Preferably the second zone comprises inlet means IG for feeding a gas stream, more preferably a high-pressure gas stream, into the second zone.

Preferably the apparatus is arranged vertically above the reactor unit Ru, wherein the connecting line between ORD and IM is configured to allow transferring M from RDM to Ri by gravity, wherein said connecting line is optionally equipped with a conveyor means, more preferably a feeder means, more preferably a rotary feeder means. More preferably, RDM is a hopper.

The present invention is further illustrated by the following set of embodiments and combinations of embodiments resulting from the dependencies and back-references as indicated. In particular, it is noted that in each instance where a range of embodiments is mentioned, for example in the context of a term such as "The process of any one of embodiments 1 to 4", every embodiment in this range is meant to be explicitly disclosed for the skilled person, i.e. the wording of this term is to be understood by the skilled person as being synonymous to "The process of any one of embodiments 1 , 2, 3 and 4". Further, it is explicitly noted that the following set of embodiments represents a suitably structured part of the general description directed to preferred aspects of the present invention, and, thus, suitably supports, but does not represent the claims of the present invention. 1 . A process for hydrolytically depolymerizing a polyamide prepared from e-caprolactam, said polyamide being contained in a solid material M, the process comprising

(i) providing the solid material M containing the polyamide, M having a temperature TM, wherein TM<TP, TP being the melting point of the polyamide;

(ii) providing a liquid aqueous stream Sw, wherein from 90 to 100 weight-% of Sw consist of water and wherein Sw has a temperature Tsw, wherein TS >TP;

(iii) feeding the solid material M provided according to (i) and the liquid aqueous stream Sw provided according to (ii) into a chemical reactor unit Ru, obtaining a mixture;

(iv) subjecting the mixture obtained according to (iii) in Ru to a depolymerization temperature TD at a depolymerization pressure PD, wherein TM<TD<TSW, obtaining an aqueous mixture containing e-caprolactam dissolved in water;

(v) removing an aqueous liquid stream SR from Ru, SR containing e-caprolactam dissolved in water.

2. The process of embodiment 1 , wherein TD is in the range of from 230 to 320 °C, preferably in the range of from 250 to 300 °C, more preferably in the range of from 270 to 295 °C.

3. The process of embodiment 1 or 2, wherein Tsw is in the range of from 240 to 350 °C, preferably in the range of from 260 to 330 °C, more preferably in the range of from 290 to 325 °C.

4. The process of any one of embodiments 1 to 3, wherein AT=TSW-TD and AT is in the range of from 10 to 70 °C, preferably in the range of from 10 to 50 °C, more preferably in the range of from 10 to 30 °C.

5. The process of any one of embodiments 1 to 4, wherein PD is in the range of from 40 to 120 bar, preferably in the range of from 50 to100 bar, more preferably in the range of from 60 to 90 bar.

6. The process of any one of embodiments 1 to 5, wherein from 91 to 100 weight-%, preferably from 92 to 100 weight-%, more preferably from 95 to 100 weight-%, of Sw consist of water.

7. The process of any one of embodiments 1 to 6, wherein M comprises, preferably consists of waste material, wherein said waste material preferably comprises textile waste material.

8. The process of any one of embodiments 1 to 7, wherein from 10 to 99 weight-%, more preferably from 30 to 98.5 weight-%, more preferably from 50 to 98 weight-%, more preferably from 80 to 98 weight-%, of M consist of the polyamide.

9. The process of any one of embodiments 1 to 8, wherein M is in the form of granules, wherein the mean diameter of the granules is preferably in the range of from 0.5 to 10 mm, more preferably in the range of from 1 to 7 mm, more preferably in the range of from 2 to 4 mm.

10. The process of any one of embodiments 1 to 9, wherein according to (iii), M and Sw are fed into Ru at a mixing ratio mw/kg : mp/kg, defined as the amount of water contained in Si, mw, relative the mass of polyamide contained in M, mp, in the range of from 1 :1 to 20:1 , preferably in the range of from 2:1 to 15:1 , more preferably in the range of from 5:1 to 10:1.

11 . The process of any one of embodiments 1 to 10, wherein M and Sw are fed into Ru one after the other, wherein, preferably, Sw is fed into Ru and subsequently M is fed into Ru containing Sw-

12. The process of any one of embodiments 1 to 11 , wherein prior to being fed into Ru, M is neither subjected to melting nor subjected to mashing.

13. The process of any one of embodiments 1 to 12, wherein the chemical reactor unit Ru comprises z chemical reactors R, i=1 ...z, wherein z is in the range of from 1 to 10, preferably in the range of from 2 to 8, more preferably in the range of from 2 to 6, more preferably in the range of from 2 to 5, more preferably in the range of from 2 to 4, more preferably 3 or 4, more preferably 4.

14. The process of embodiment 13, wherein z>1 and wherein at least 2 reactors R, preferably z reactors R are serially coupled.

15. The process of embodiment 14, wherein z reactors R are serially coupled, wherein according to (iii), M and Sw are fed into R, i=1 ; an aqueous liquid stream Sj containing e-caprolactam dissolved in water is removed from R and fed into R+i, i<z; according to (v), SR is removed from R _z ; wherein in every reactor R, a depolymerization temperature TDI at a depolymerization pressure poi is maintained, wherein, independently of each other, TDI is in the range of from 230 to 320 °C, preferably in the range of from 250 to 300 °C, more preferably in the range of from 270 to 295 °C, and wherein, independently of each other, poi is preferably in the range of from 40 to 120 bar, more preferably in the range of from 50 to100 bar, more preferably in the range of from 60 to 90 bar.

16. The process of embodiment 15, wherein maintaining a depolymerization temperature TDI in a reactor R comprises heating the reactor contents of R, preferably indirectly heating the reactor contents of R, wherein more preferably, maintaining a depolymerization temperature TDI in a reactor R comprises heating the reactor contents of R by passing a heating medium through a heating jacket of R. 17. The process of embodiment 15 or 16, wherein the z reactors Rj are vertically arranged, with Ri being the top-most reactor and R _z being the bottom-most reactor, wherein Sj obtained from R is transferred to +i by gravity, preferably by gravity only.

18. The process of any one of embodiments 13 to 17, preferably of embodiment 18, wherein at least 1 , preferably z reactors R are configured as non-stirred reactors or as non-circulation reactors, preferably as non-stirred reactors and non-circulation reactors.

19. The process of any one of embodiments 13 to 18, wherein the reactors Ri to R _y .i are operated in batch mode and the reactors R _y to R _z are operated in continuous mode, wherein y>1 and y<z, wherein y is preferably z.

20. The process of embodiment 19, wherein the residence time in one or more of the reactors Ri to R _y -i, preferably in the reactors Ri to R _y -i, is in the range of from 5 to 40 minutes, more preferably in the range of from 10 to 30 minutes, more preferably in the range of from 15 to 25 minutes; wherein the residence time in the reactor R _y , wherein y is preferably z, is preferably in the range of from 1 second to 40 minutes, more preferably in the range of from 2 seconds to 30 minutes, more preferably in the range of from 3 seconds to 25 minutes.

21 . The process of embodiment 19 or 20, wherein the overall residence time in the chemical reactor unit is in the range of from 15 to 160 minutes, preferably in the range of from 30 to 120 minutes, more preferably in the range of from 45 to 100 minutes, more preferably in the range of from 60 to 80 minutes.

22. The process of any one of embodiments 1 to 21 , wherein providing a liquid aqueous stream Sw according to (ii) comprises

(11.1) separating at least a part of the water contained in the aqueous liquid stream SR removed from Ru;

(11.2) feeding at least a part of the water separated according to (ii.1) back into the process as part of the stream Sw.

23. The process of any one of embodiments 1 to 22, wherein providing the solid material M containing the polyamide according to (i) comprises

(1.1 ) providing the solid material in a first zone of a two-zone receiving and discharge means RDM, wherein the temperature of M in said first zone is in the range of from -10 to 50 °C, preferably in the range of from 15 to 40 °C, more preferably in the range of from 20 to 30 °C, preferably at atmospheric pressure;

(1.2) passing the solid material provided in the first zone to a second zone of the RDM, wherein said second zone comprises outlet means being connected via a connecting line with the reactor unit Ru;

(1.3) feeding a gas stream into the second zone of the RDM comprising the solid material, said gas stream having a pressure PG with PG>PD, wherein PG is preferably in the range of PD<PG^(PD+5 bar), wherein the gas stream has a temperature preferably in the range of from 10 to 40 °C, more preferably in the range of from 15 to 30 °C;

(i.4) passing the solid material from the second zone of the RDM into the connecting line according to (i.2).

24. The process of embodiment 23, wherein the two-zone receiving and discharge means RDM is a two-zone hopper.

25. The process of embodiment 23 or 24, wherein the gas stream according to (i.3) comprises one or more of nitrogen and water.

26. An apparatus for carrying out a process for hydrolytically depolymerizing a polyamide prepared from c-caprolactam, said polyamide being contained in a solid material M, preferably for carrying out a process according to any one of embodiments 1 to 25, the apparatus comprising

(a) a reactor unit Ru comprising z chemical reactors R, i=1 ...z, wherein z is in the range of from 2 to 8, preferably in the range of from 2 to 6, more preferably in the range of from 2 to 5, more preferably in the range of from 2 to 4, more preferably 3 or 4, more preferably 4; wherein the z reactors R are serially coupled and vertically arranged, with Ri being the topmost reactor and R _z being the bottom-most reactor; wherein Ri comprises inlet means IM for feeding the solid material M into Ri and inlet means I sw for feeding a liquid aqueous stream Sw into Ri, said inlet means being located at the top of Ri ; wherein every reactor R, comprises outlet means O _Ri for removing an aqueous liquid product stream Sj from R; wherein a reactor R, i>1 , comprises inlet means l _R for feeding the aqueous liquid product stream S removed from R via a connecting line CM into R; wherein the outlet stream removed from R _z is an aqueous liquid stream SR, SR containing E- caprolactam dissolved in water.

27. The apparatus of embodiment 26, wherein at least one reactor R, preferably all reactors R are equipped with a heating jacket for passing a heating medium through said jacket.

28. The apparatus of embodiment 26 or 27, wherein at least 1 , preferably z reactors R are configured as non-stirred reactors or as non-circulation reactors, preferably as non-stirred reactors and non-circulation reactors.

29. The apparatus of any one of embodiments 26 to 28, wherein at least one connecting line Ci, preferably all z-1 connecting lines Cj are configured to allow transferring SM from RM to R by gravity, preferably by gravity only. 30. The apparatus of embodiment 29, wherein at least one connecting line Ci, preferably all z-1 connecting lines Cj are not equipped with pumping means, preferably not equipped with conveyor means.

31 . The apparatus of any one of embodiments 26 to 30, wherein the reactors Ri to R _y .i are batch mode reactors and the reactors R _y to R _z are continuous mode reactors, wherein y<1 and y<z, wherein y is preferably z.

32. The apparatus of any one of embodiments 26 to 31 , further comprising

(b) separating means SEw for separating water from SR; wherein said separating means SEw is arranged downstream of Ru, comprises inlet means ISE for passing SR into SEw, the ISE being connected via a connecting line with the outlet means OR, of the reactor R _z ; and further comprise outlet means OSE for removing water from SEw, the OSE being connected via a connecting line with the inlet means Isw of the reactor Ri .

33. The apparatus of any one of embodiments 26 to 32, further comprising

(c) a two-zone receiving and discharge means RDM for metering the solid material M to the reactor unit Ru; wherein said two-zone receiving and discharge means RDM is arranged upstream of Ru, wherein the first zone of RDM is arranged vertically above the second zone of RDM and comprises inlet means l _RD for receiving the solid material M, wherein the second zone of RDM comprises outlet means ORD for removing the solid material from RDM, the outlet means ORD being connected via a connecting line with the inlet means IM of the reactor Ri, wherein the RDM further comprises closing and opening means arranged between the first zone and the second zone of the RDM.

34. The apparatus of embodiment 33, wherein the second zone comprises inlet means IG for feeding a gas stream, preferably a high-pressure gas stream, into the second zone.

35. The apparatus of embodiment 33 or 34, being arranged vertically above the reactor unit Ru, wherein the connecting line between ORD and IM is configured to allow transferring M from RDM to Ri by gravity, wherein said connecting line is optionally equipped with a conveyor means, preferably a feeder means, more preferably a rotary feeder means.

36. The apparatus of embodiment 35, wherein the RDM is a hopper.

In the context of the present invention, it is noted that the term „polyamide prepared from £-caprolactam“ as used herein refers to „polyamide 6“ being characterized by the formula (- N H- (CH2)S- CO- ) _n . The term „bar“ as used in the context of the present invention refers to „bar(abs)”, i.e. bar (absolute), sometimes also referred to “bara”. The term “textile material” covers textile raw materials and non-textile raw materials that are processed by various methods into linear, planar and spatial structures. It concerns the linear textile structures produced from them, such as yarns, twisted yarns and ropes, the sheet-like textile structures, such as woven fabrics, knitted fabrics, braids, stitch-bonded fabrics, nonwovens and felts, and the three-dimensional textile structures, i.e. body structures, such as textile hoses, stockings or textile semi-finished products; and it further concerns those finished products which, using the aforementioned products, are brought into a saleable condition by making up, opening up and/or other operations for onward transmission to the processor, the trade or the end consumer.

The term “textile waste material” covers a textile material as defined above, the inherent value of which has been consumed from the perspective of its current holder and, thus, is an end-of-life material for said holder.

In the context of the present invention, a term “X is one or more of A, B and C”, wherein X is a given feature and each of A, B and C stands for specific realization of said feature, is to be understood as disclosing that X is either A, or B, or C, or A and B, or A and C, or B and C, or A and B and C. In this regard, it is noted that the skilled person is capable of transfer to above abstract term to a concrete example, e.g. where X is a chemical element and A, B and C are concrete elements such as Li, Na, and K, or X is a temperature and A, B and C are concrete temperatures such as 10 °C, 20 °C, and 30 °C. In this regard, it is further noted that the skilled person is capable of extending the above term to less specific realizations of said feature, e.g. “X is one or more of A and B” disclosing that X is either A, or B, or A and B, or to more specific realizations of said feature, e.g. ‘ is one or more of A, B, C and D”, disclosing that X is either A, or B, or C, or D, or A and B, or A and C, or A and D, or B and C, or B and D, or C and D, or A and B and C, or A and B and D, or B and C and D, or A and B and C and D.

Description of the figures

Figure 1 is a schematic representation of an apparatus used for the process according to the invention.

The apparatus comprises a reactor unit Ru comprising one chemical rector Ri, preferably a batch-type reactor, and a separation means SEw downstream of the reactor unit. The solid material M is fed via an inlet means IM (not shown in Figure 1) into the reactor unit Ru, in particular at the top of the reactor Ri, as well as the liquid aqueous stream Sw. The product stream SR containing e-caprolactam dissolved in water is then removed from the bottom of reactor Ri and is further passed through the separation means SEw to separate SR from water. Further, water removed from SR is preferably recycled such that it can be introduced in S prior to entering the reaction unit Ru and in particular Ri. The water can be stored in the tank Tw. Furthermore, upstream of the reactor Ri in the apparatus is a two-zone receiving and discharge means RDM for metering the solid material M into the reactor unit Ru and in particular the reactor Ri, wherein zone 1 of RDM is arranged vertically above zone 2 of RDM and comprises inlet means l _RD (not shown in Figure 1) for receiving the solid material M, wherein zone 2 comprises outlet means ORD (not shown in Figure 1) for removing the solid material from RDM, the outlet means ORD being connected via a connecting line with the inlet means IM (not shown in Figure 1) of the reactor Ri, wherein the RDM further comprises closing and opening means arranged between zone 1 and zone 2 of the RDM. Further a gas stream, preferably a high-pressure gas stream, is introduced in zone 2 of RDM. The solid material M is transferred from zone 2 of RDM to Ri by gravity. Finally, the product stream SR exiting the separation means SEw can be further treated (not shown in Figure 1).

Figure 2 is a schematic representation of an apparatus used for the process according to the invention.

The apparatus comprises a reactor unit Ru comprising two chemical rectors Ri and R2, Ri is arranged vertically above R2, and a separation means SEw downstream of the reactor unit. Ri is a batch mode reactor and R2 is a continuous mode reactor. The solid material M is fed via an inlet means IM (not shown in Figure 2) into Ri as well as a liquid aqueous stream S comprising water. An aqueous liquid product stream Si is removed at the bottom of Ri and fed at the top of R2. The aqueous liquid product stream Si is transferred from Ri to R2 by gravity (no pumping, no conveyor means). The product stream SR containing e-caprolactam dissolved in water is then removed from the bottom of reactor R2 and is further passed through the separation means SEw to separate SR from water. Further, water removed from SR is preferably recycled such that it can be added to Sw prior to entering the reaction unit Ru and in particular Ri. The water can be stored in the tank Tw. Furthermore, upstream of the reactor unit Ru in the apparatus is a two-zone receiving and discharge means RDM for metering the solid material M into the reactor unit Ru and in particular the reactor Ri, wherein zone 1 of RDM is arranged vertically above zone 2 of RDM and comprises inlet means l _RD (not shown in Figure 2) for receiving the solid material M, wherein zone 2 comprises outlet means ORD (not shown in Figure 2) for removing the solid material M from RDM, the outlet means ORD being connected via a connecting line with the inlet means IM (not shown in Figure 2) of the reactor Ri, wherein the RDM further comprises closing and opening means arranged between zone 1 and zone 2 of the RDM. Further a gas stream, preferably a high- pressure gas stream, is introduced in zone 2 of RDM. The solid material M is transferred from zone 2 of RDM to Ri by gravity. Finally, the product stream SR exiting the separation means SEw can be further treated (not shown in Figure 2).

Figure 3 is a schematic representation of an apparatus used for the process according to the invention.

The apparatus comprises a reactor unit Ru comprising three chemical rectors Ri, R2 and R3, Ri is arranged vertically above R2, R2 is arranged vertically above R3, and a separation means SEw downstream of the reactor unit. Ri and R2 are batch mode reactors and R3 is a continuous mode reactor. The solid material M is fed via an inlet means IM (not shown in Figure 3) into Ri as well as a liquid aqueous stream Sw comprising water. An aqueous liquid product stream Si is removed at the bottom of Ri and fed at the top of R2. The aqueous liquid product stream Si is transferred from R1 to R2 by gravity (no pumping, no conveyor means). An aqueous liquid product stream S2 is removed at the bottom of R2 and fed at the top of R3. The aqueous liquid product stream S2 is transferred from R2 to R3 by gravity (no pumping, no conveyor means). The product stream SR containing e-caprolactam dissolved in water is then removed from the bottom of reactor R3 and is further passed through the separation means SEw to separate SR from water. Further, water removed from SR is preferably recycled such that it can be added to Sw prior to entering the reaction unit Ru and in particular R1. The water can be stored in the tank Tw. Furthermore, upstream of the reactor unit Ru in the apparatus is a two-zone receiving and discharge means RDM for metering the solid material M into the reactor unit Ru and in particular the reactor R1, wherein zone 1 of RDM is arranged vertically above zone 2 of RDM and comprises inlet means l _RD (not shown in Figure 3) for receiving the solid material M, wherein zone 2 comprises outlet means ORD (not shown in Figure 3) for removing the solid material M from RDM, the outlet means ORD being connected via a connecting line with the inlet means IM (not shown in Figure 3) of the reactor R1, wherein the RDM further comprises closing and opening means arranged between zone 1 and zone 2 of the RDM. Further a gas stream, preferably a high- pressure gas stream, is introduced in zone 2 of RDM. The solid material M is transferred from zone 2 of RDM to R1 by gravity. Finally, the product stream SR exiting the separation means SEw can be further treated (not shown in Figure 3).

Figure 4 is a schematic representation of an apparatus used for the process according to the invention.

The apparatus comprises a reactor unit Ru comprising three chemical rectors R1, R2, Rs and R4, R1 is arranged vertically above R2, R2 is arranged vertically above R3, R3 is arranged vertically above R4, and a separation means SEw downstream of the reactor unit. R1, R2 and R3 are batch mode reactors and R4 is a continuous mode reactor. The solid material M is fed via an inlet means IM (not shown in Figure 4) into R1 as well as a liquid aqueous stream Sw comprising water. An aqueous liquid product stream Si is removed at the bottom of R1 and fed at the top of R2. The aqueous liquid product stream Si is transferred from R1 to R2 by gravity (no pumping, no conveyor means). An aqueous liquid product stream S2 is removed at the bottom of R2 and fed at the top of R3. The aqueous liquid product stream S2 is transferred from R2 to R3 by gravity (no pumping, no conveyor means). An aqueous liquid product stream S3 is removed at the bottom of R3 and fed at the top of R4. The aqueous liquid product stream S3 is transferred from R3 to R4 by gravity (no pumping, no conveyor means). The product stream SR containing e-caprolactam dissolved in water is then removed from the bottom of reactor R4 and is further passed through the separation means SEw to separate SR from water. Further, water removed from SR is preferably recycled such that it can be added to Sw prior to entering the reaction unit Ru and in particular R1. The water can be stored in the tank Tw. Furthermore, upstream of the reactor unit Ru in the apparatus is a two-zone receiving and discharge means RDM for metering the solid material M into the reactor unit Ru and in particular the reactor R1, wherein zone 1 of RDM is arranged vertically above zone 2 of RDM and comprises inlet means l _RD (not shown in Figure 4) for receiving the solid material M, wherein zone 2 comprises outlet means ORD (not shown in Figure 4) for removing the solid material M from RDM, the outlet means ORD being connected via a connecting line with the inlet means IM (not shown in Figure 4) of the reactor Ri, wherein the RDM further comprises closing and opening means arranged between zone 1 and zone 2 of the RDM. Further a gas stream, preferably a high-pressure gas stream, is introduced in zone 2 of RDM. The solid material M is transferred from zone 2 of RDM to Ri by gravity. Finally, the product stream SR exiting the separation means SEw can be further treated (not shown in Figure 4).