Process for separating high boilers from polyamide 6 depolymerization mixtures

Abstract

A continuous process for separating one or more organic compounds X from an aqueous liquid stream SL0 comprising monomeric ε-caprolactam and said one or more compounds X, the process comprising (i) providing the stream SL0; (ii) providing a non-aqueous stripping gas stream SG0 comprising at least one inert gas G; (iii) producing in a stripping unit US1 from the stream SL0 an aqueous gas stream SV1 and a liquid stream SL1; (iv) producing in a separation unit US2 from the stream SV1 an aqueous gas stream SV2 and a liquid stream SL2.

Description

Process for separating high boilers from polyamide 6 depolymerization mixturesThe present invention relates to a process for separating high boiling compounds from a stream which comprises the high boiling compounds and E-caprolactam; this stream is preferably obtained from the depolymerization of polyamide contained in a solid material, wherein this material is preferably a waste material. Further, the present invention relates to said process which, downstream of the high boiler separation, comprises further purification of E- caprolactam, leading to a stream comprising highly purified E-caprolactam. Yet further, the present invention relates to the respectively obtained highly purified E-caprolactam and its use as an educt material, preferably for preparing polyamide 6. Therefore, the present invention in particular relates to a recycle loop of E-caprolactam.Polyamide, and in particular polyamide 6 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. The purification process for E-caprolactam downstream of the depolymerization step is not a straight-forward task, for example due to the various possible chemical compositions of waste materials comprising polyamide 6 which form the educt materials for the recycling process.US 2016 / 221943 A1 relates to a process for the recovery of E-caprolactam from extract water of polycaprolactam obtained by hydrolytic polymerization, and also relates to the use of the intermediate and end product streams obtained in the process.TW I 663 186 B relates to a method for the production of polyamide 6 with low extract content and a device for it, wherein a melt of non-extracted polyamide 6 is cleaned from monomer and oligomers in a degasification device in vacuum, wherein the vapor being withdrawn from the degasification device by the vacuum generation device is cleaned from monomer, oligomers and optionally water at first in a direct condenser which is operated with liquid E- caprolactam and subsequently in a pre-separator which is cooled with a coolant, before it reaches the vacuum generation device.US 2016 / 221943 A1 relates to a process for the recovery of E-caprolactam from extract water of polycaprolactam obtained by hydrolytic polymerization, and relates to the use of the intermediate and end product streams obtained in the process.US 2017 / 305835 A1 relates to a method for purifying raw dinitrotoluenes resulting from dinitration of toluene in the presence of a nitric acid / sulfuric acid / nitrating acid mixture, and a device or plant for performing the method, and a corresponding production plant for producing dinitrotoluene.It was found that said waste materials will contain certain compounds which, either prior to or after depolymerization of polyamide 6, lead to a stream comprising E-caprolactam and compounds having a higher boiling point than E- caprolactam. Due to possibly different chemical compositions of said waste material, however, these compounds having a higher boiling point than E-caprolactam will usually differ from time to time, both with regard to the content in the stream to be purified and in chemical nature. Therefore, there is a need for a robust process which is suitable for purifying crude E-caprolactam streams comprising said high boiling compounds and which allows for dealing with different qualities of streams to be purified.Surprisingly, it was found that using a specific stripping technology making use of a specific stripping medium, a process can be realized according to which, compared to other processes, a specific downstream purification stage can be omitted. Using this new process in a preferred design, it turned out that it is further possible to realize an advantageous re-use of the stripping medium and, at the same time, to realize a heat-integration stage making the overall process economically and ecologically advantageous, a process feature which is of particular importance for polyamide 6 recycling processes.Therefore, the present invention relates to a continuous process for separating one or more organic compounds X from an aqueous liquid stream SLO comprising monomeric E-caprolactam and said one or more compounds X, the process comprising(i) providing the stream SLO having a temperature TLO and exhibiting a total concentration CLO(X) of the one or more compounds X, a concentration CLO(C) of monomeric E-capro-lactam, and a concentration CLO(W) of water;(ii) providing a non-aqueous stripping gas stream SGO comprising at least one inert gas G and having a temperature TGO with TGO > TLO;(iii) producing in a stripping unit Usi from the stream SLO an aqueous gas stream Svi and a liquid stream SLI, comprising(iii.1 ) passing the stream SLO and the stream SGO into the stripping unit Usi;(111.2) bringing the stream SLO and the stream SGO in the stripping unit Usi at stripping conditions into contact with each other, wherein the stripping conditions comprise a stripping pressure ps and wherein at the stripping pressure ps, the one or more one organic compounds X comprised in the stream SLO have a boiling point TBX and monomeric E-caprolactam has a boiling point TBC with TBX > TBC;(111.3) removing the stream Svi from the stripping unit Usi, the stream Svi having a temperature Tvi with TLO < Tvi < TGO and exhibiting a total concentration cvi(X) of one or more compounds X, a concentration cvi(C) of monomeric E-caprolactam, a concentration Cvi(W) of water and a concentration Cvi(G) of the at least one inert gas G, with cvi(C) > CLO(C) and cvi(X) < CLO(X);(111.4) removing the stream SLI from the stripping unit Usi, the stream SLI having a temperature TLI with TLO < TLI < TGO and exhibiting a total concentration CLI(X) of one or more compounds X and a concentration CLI(C) of monomeric E-caprolactam, with CLI(X) > Cvi(X) and CLI(C) < Cvi(C);(iv) producing in a separation unit Us2 from the stream Svi an aqueous gas stream Sv2 and a liquid stream SL2, comprising(iv.1 ) passing the stream Svi removed from the stripping unit Usi into the separation unit Us2 and subjecting the stream Svi in the unit Us2 to separation conditions;(iv.2) removing the stream Sv2 from the separation unit Us2, the stream Sv2 exhibiting a total concentration cv2(X) of one or more compounds X, a concentration cv2(C) of monomeric E-caprolactam, a concentration cv2(W) of water and a concentration cv2(G) of the at least one inert gas G, with cv2(W) < Cvi(W);(iv.3) removing the stream SL2 from the separation unit Us2, the stream SL2 exhibiting a total concentration CL2(X) of one or more compounds X, a concentration Ci_2(C) of monomeric E-caprolactam and a concentration CL2(W) of water, with CL2(X) > Cv2(X), Ci_2(C) > Cv2(C), and CL2(W) < Cv2(W).Preferably, the temperature TLO of the stream SLO provided according to (i) is in the range of from 75 to 120 °C, more preferably in the range of from 80 to 110 °C, more preferably in the range of from 85 to 100 °C.Regarding the concentration of the monomeric E-caprolactam CLO(C) and the total concentration CLO(X) of the one or more compounds X CLO(X) in the stream SLO provided according to (I), it is preferred that the sum thereof, CLO(C) + CLO(X), is in the range of from 60 to 95 weight-%, more preferably in the range of from 70 to 90 weight-%, more preferably in the range of from 80 to 85 weight-%, based on the weight of the stream SLO. The term "total concentration CLO(X)” as used according to the present invention refers to the sum of the concentrations of all individual compounds X contained in the stream SLO.Further, it is preferred that in the stream SLO provided according to (I), the weight ratio of the one or more compounds X to monomeric E-caprolactam is in the range of from 50:50 to 5:95. Conceivable ranges, for example, are 50:50 to 40:60 or from 40:60 to 30:70 or from 30:70 to 20:80 or from 20:80 to 10:90 or from 10:90 to 5:95.Generally, the chemical nature of the one or more compounds X depends on the composition of the stream SM comprising a solid material M which in turn comprising polyamide 6, said stream being provided according to (1.1) as described herein. It is preferred that the one or more compounds X comprised in the stream SLO comprise at least one of at least one aromatic amine which includes at least one of an aromatic monoamine, an aromatic diamine, an aromatic triamine and an aromatic tetramine; and / or at least one aliphatic amine which includes at least one of an aliphatic monoamine, an aliphatic diamine and an aliphatic triamine; and / or at least one aliphatic amide; and / or at least one aromatic alcohol which includes at least one of an aromatic monool and an aromatic diol; and / or at least one aliphatic alcohol which includes at least one of an aliphatic monool and an aliphatic diol; and / or at least one aromatic acid; and / or at least one and aliphatic acid; and / or at least one E-caprolactam oligomer; and / orat least other compound selected from the group consisting of one or more cleavage products of dyes such as optionally chlorinated aromatic diamines, one or more water-soluble oligomeric cellulose cleavage products, and one or more water-soluble oligomers of terephthalic acid and hexamethylenediamine.Specifically, it is preferred that the at least one aromatic amine includes one or more of 4, 4'-methylenedi aniline (MDA), isomers thereof such as 2,4’-methylenedianiline and 2,2’-methylenedianiline, and polymethylen polyphenylen polyamines (pMDA); the at least one aliphatic amine and the at least one aliphatic amide include one or more of hexamethylenediamine adipate, 6-aminocaproic acid and oligomers thereof, including 6-aminocaproic acid dimer and higher oligomers such as 6-aminocaproic acid trimer, 6-aminocaproic acid tetramer, 6- aminocaproic acid pentamer, 6-aminocaproic acid hexamer, N'-(6-aminohexyl)hexane-1,6-diamine, N-methyl- hexane-1,6-diamine, 6-ami nohexaneamide, derivatives of E-caprolactam other than E-caprolactam oligomers and having a boiling point higher than E-caprolactam such as 1-(6-aminohexyl)azepan-2-one; the at least one aliphatic alcohol includes one or more of butanediol and oligomers thereof, including butanediol dimer and higher oligomers such as butanediol trimer, including polytetrahydrofuran; the at least one aromatic acid and the at least one aliphatic acid include one or more of terephthalic acid and adipic acid; the at least one E-caprolactam oligomer includes one or more of E-caprolactam dimer E-caprolactam trimer, E- caprolactam tetramer, E-caprolactam pentamer, and E-caprolactam hexamer.As described, the stream SLO provided according to (i) is an aqueous stream. Regarding the concentration of water of SLO, CLO(W), it is preferred that it is in the range of from 5 to 40 weight-%, more preferably in the range of from 10 to 30 weight-%, more preferably in the range of from 15 to 20 weight-%, based on the weight of the stream SLO. Preferably from 95 to 100 weight-%, more preferably from 98 to 100 weight-%, more preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, more preferably from 99.9 to 100 weight-% of the stream SLO provided according to (i) consist of the one or more compounds X, monomeric E-caprolactam, and water.According to (ii), a non-aqueous stripping gas stream SGO comprising at least one inert gas G is provided. Preferably, the at least one inert gas G comprises one or more of nitrogen and carbon dioxide, more preferably nitrogen, wherein more preferably, at least 99 weight-%, more preferably at least 99.5 weight-%, more preferably at least 99.9 volume - % of the at least one inter gas G consist of nitrogen, wherein preferably from 95 to 100 weight-%, more preferably from 98 to 100 weight-%, more preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, more preferably from 99.8 to 100 weight-%, more preferably from 99.9 to 100 weight-% of the non-aqueous stripping gas stream SGO consist of the at least one inert gas G. Therefore, the term "non-aqueous” as used in this context of the present invention refers to a gas stream SGO which comprises water, if at all, only in very low concentrations such as at most 1 weight-% or at most 0.5 weight-% or at most 0.2 weight-% or at most 0.1 weight-%, based on the total weight of the stream SGO. In each case, the term "weight-%” is based on the total weight of the stream SGO.Preferably, the temperature TGO of the stream SGO provided according to (ii) is at least 250 °C, preferably in the rangeof from 250 to 500 °C, more preferably in the range of from 300 to 450 °C. Therefore, preferred conceivable ranges are from 300 to 350 °C or from 350 to 400 °C or from 400 to 450 °C.According to the present invention, the streams SLO and SGO are passed into the stripping unit Usi according to (iii.1 ). The stream SLO is passed into the stripping unit Usi at a mass flow rate PLO and the stream SGO is passed into the stripping unit Usi at a mass flow rate PGO. The value of PLO / PGO is preferably in the range of from 0.15:1 to 0.5:1, more preferably in the range of from 0.15:1 to 0.4:1, more preferably in the range of from 0.15:1 to 0.35:, more preferably in the range of from 0.15:1 to 0.3:1, more preferably in the range of from 0.15:1 to 0.25:1, such as from 0.15:1 to 0.20:1 or from 0.20:1 to 0.25:1. The stream SLO which is passed into the stripping unit Usi according to (iii.1) exhibits a pressure preferably in the range of from 1 to 4 bar, more preferably in the range of from 1 to 3 bar, more preferably in the range of from 1 to 2 bar. The stream SGO which is passed into the stripping unit Usi according to (iii.1) exhibits a pressure preferably in the range of from 1 to 4 bar, more preferably in the range of from 1 to 3 bar, more preferably in the range of from 1 to 2 bar. In the stripping unit Usi, the stream SLO and the stream SGO are brought into contact with each other so as to provide suitable stripping conditions; preferably, they are brought into contact in countercurrent mode or in co-current mode, more preferably in counter-current mode. While not being restricted to any particular design, it is preferred that the stripping unit Usi comprises one or more of a tray column, a packed column, a spray column, a bubble column and a centrifugal contactor, wherein more preferably, the stripping unit Usi comprises a spray column.From the stripping unit Usi, the stream SLI is obtained which is, compared to the stream SLO, enriched in one or more of the compounds X and, respectively, depleted in monomeric E-caprolactam. The temperature of the stream SLI, TH, is preferably in the range of from 230 to 300 °C, more preferably in the range of from 250 to 300 °C, more preferably in the range of from 250 to 290 °C, more preferably in the range of from 250 to 280 °C. Regarding the concentrations, it is preferred that CLI(X) + CLI(C) is in the range of from 95 to 100 weight-%, more preferably in the range of from 98 to 100 weight-%, more preferably in the range of from 99 to 100 weight-%, based on the weight of the stream SLI . Preferably, in the stream SLI , the weight ratio of the one or more compounds X relative to monomeric E-caprolactam is at least 10:1, more preferably at least 15:1, more preferably at least 20:1, more preferably at least 25:1, more preferably at least 30:1, more preferably at least 35:1, more preferably at least 40:1.Regarding the stripping step of the present invention, the process exhibits a high boiler separation efficiency Q(X), preferably of at least 95 %, more preferably at least 96 %, more preferably at least 97 %, more preferably at least 98 %, more preferably at least 99 %, with Q(X) = |JLI(X) I PLO(X), wherein PLO(X) is the mass flow rate of the at least one compound X in the stream SLO, expressed in kg / h, and |JLI (X) is the mass flow rate of the at least one compound X in the stream SLI, expressed in kg / h.In addition to the stream SLI, a gas stream Svi is obtained from the stripping unit Usi which is, compared to the stream SLO, depleted in the one or more compounds X and, respectively, enriched in monomeric E-caprolactam. The temperature of the stream Svi, Tvi, is preferably in the ranoe of from 200 to 270 °C, more preferably in the range offrom 230 to 270 °C, more preferably in the range of from 250 to 270 °C. The pressure of the stream Svi , pvi , is preferably in the range of from 1 to 4 bar, more preferably in the range of from 1 to 3 bar, more preferably in the range of from 1 to 2 bar. Regarding the concentrations, it is preferred that cvi(C) + Cvi(W) + Cvi(G) is in the range of from 98 to 100 weight-%, more preferably in the range of from 99 to 100 weight-%, more preferably in the range of from 99.8 to 100 weight-%, based on the weight of the stream Svi. Preferably, in the stream Svi , the weight ratio of the one or more compounds X relative to monomeric E-caprolactam is at most 1 :50, more preferably at most 1 :65, more preferably at most 1 :80, more preferably at most 1 :90, more preferably at most 1 :100.According to (iv) of the present invention, the stream Svi is passed to the separation unit Us2. Preferably, the separation unit Us2 is a partial condensation unit, and more preferably, Us2 comprises one or more of a plate heat exchanger and a tube shell heat exchanger. More preferably, the separation unit Us2 according to (iv) is a scrubbing unit, preferably comprising a packed column, and as far as the production of the aqueous gas stream Sv2 and the liquid stream SL2 from the stream Svi in the scrubbing unit Us2 is concerned, it preferably comprises(iv.1 ) passing the stream Svi removed from the stripping unit Usi into the scrubbing unit Us2 and subjecting the stream Svi in the unit Us2 to scrubbing conditions;(iv.2) removing the stream Sv2 from the scrubbing unit Us2, the stream Sv2 having a temperature Tv2 with Tv2 < Tvi and exhibiting a total concentration cv2(X) of one or more compounds X, a concentration cv2(C) of monomeric E-caprolactam, a concentration cv2(W) of water and a concentration cv2(G) of the at least one inert gas G, with cv2(W) < cvi(W);(iv.3) removing the stream SL2 from the scrubbing unit Us2, the stream SL2 having a temperature TL2 with Tv2 < TL2 < Tvi and exhibiting a total concentration CL2(X) of one or more compounds X, a concentration CL2(C) of monomeric E-caprolactam and a concentration CL2(W) of water, with CL2(X) > Cv2(X), CL2(C) > Cv2(C), and CL2(W) < cv2(W);(iv.4) dividing the stream SL2 in at least a stream Si_2i having a temperature TL2I with TL2I = TL2 and a stream Si_22 having a temperature TL22 with TL22 = TL2J subjecting the stream Si_2i to cooling, obtaining a cooled stream SL2IC having a temperature TL2IC < TL2I; and feeding the stream Si_2ic back into the scrubbing unit Us2, wherein the scrubbing conditions according to (iv.1) comprise bringing the gas stream Svi into contact with the liquid stream Si_2ic.From the unit Us2, the stream SL2 is obtained which is, compared to the stream Svi, enriched in monomeric E- caprolactam and depleted in water. Due to the fact that according to the present invention, the aqueous stream SLO is stripped with a non-aqueous gas stream SGO, and further due to the fact that water is efficiently removed from the gas stream Svi, the respectively obtained purified E-caprolactam stream SL2 exhibit such a low concentration of water that it can be passed to a downstream fine purification stage such as fine distillation stage without the need of a further intermediate water separation stage. The temperature of the stream Si_2, TL2, is preferably in the range of from 85 to 110 °C, more preferably in the range of from 85 to 100 °C, more preferably in the range of from 85 to 95 °C. Regarding the concentrations, it is preferred that CL2(X) + CL2(C) + CL2(W) is in the range of from 95 to 100 weight-%, more preferably in the range of from 96 to 100 weight-%, more preferably in the range of from 97 to 100 weight-%,more preferably in the range of from 98 to 100 weight-%, more preferably in the range of from 99 to 100 weight-%, based on the weight of the stream SL2. Preferably, in the stream SL2, the weight ratio of the one or more compounds X to monomeric E-caprolactam is at most 1 :50, more preferably at most 1 :65, more preferably at most 1 :80, more preferably at most 1 :90, more preferably at most 1 : 100. Further preferably, in the stream Si_2, the weight ratio of the one or more compounds X to water is at least 0.01 :1, more preferably at least 0.5:1, more preferably at least 1 :1, more preferably at least 5:1, more preferably at least 10:1.In addition to the stream Si_2, a gas stream Sv2 is obtained from the unit Us2 which is, compared to the stream Svi, depleted in E-caprolactam and, respectively, enriched in the at least one inert gas G. The temperature of the stream Sv2, TV2, is preferably in the range of from 85 to 105 °C, more preferably in the range of from 90 to 100 °C, more preferably in the range of from 95 to 100 °C. The pressure of the stream Sv2, Pv2, is preferably in the range of from 1 to 4 bar, more preferably in the range of from 1 to 3 bar, more preferably in the range of from 1 to 2 bar. Regarding the concentrations, it is preferred that cv2(C) + cv2(W) + cv2(G) is in the range of from 98 to 100 weight-%, more preferably in the range of from 99 to 100 weight-%, more preferably in the range of from 99.5 to 100 weight-%, based on the weight of the stream Sv2. Preferably, in the stream Sv2, the weight ratio of monomeric E-caprolactam to water is at most 1 :1, preferably at most 1:2, more preferably at most 1 :3.According to preferred (iv.4), the stream SL2 is divided in at least a stream Si_2i having a temperature TL2I with TL2I = TL2 and a stream Si_22 having a temperature L22 with L22 = Ti_2i and the stream Si_2i is subjected to cooling, obtaining a cooled stream Si_2ic having a temperature TL2IC < L21; and the stream Si_2ic is fed back into the scrubbing unit Us2, wherein the scrubbing conditions according to (iv.1) comprise bringing the gas stream Svi into contact with the liquid stream Si_2ic. The temperature TL2IC is preferably in the range of from 75 to 95 °C, more preferably in the range of from 75 to 90 °C, more preferably in the range of from 75 to 85 °C. It is preferred that according to (iv.1 ), the stream Svi is passed into the scrubbing unit Us2 at a mass flow rate pvi and the stream Si_2i c is passed the scrubbing unit Us2 at a mass flow rate |JL2IC, wherein pvi I PL2IC is preferably in the range of from 0.2:1 to 0.5:1, more preferably in the range of from 0.2:1 to 0.4:1, more preferably in the range of from 0.2:1 to 0.3:1. In the scrubbing unit Us2, the stream Svi and the stream Si_2i c are brought into contact with each other so as to provide suitable stripping conditions; preferably, they are brought into contact in counter-current mode or in co-current mode or in cross-flow mode, more preferably in counter-current mode.Regarding the stripping step and the subsequent downstream separation step, preferably the subsequent downstream scrubbing step of the present invention, the process exhibits an E-caprolactam separation efficiency Q(C), preferably of at least 94 %, more preferably at least 95 %, more preferably at least 96 %, more preferably at least 97 %, more preferably at least 98 %, with Q(C) = |JL22(C) I PLO(C), wherein |JLO(C) is the mass flow rate of E- caprolactam in the stream SLO, expressed in kg / h, and pi_22(C) is the mass flow rate of E-caprolactam in the stream SL22, expressed in kg / h. Preferred ranges of at least 99.4 %, more preferably at least 99.7 %, more preferably at least 99.9 % are conceivable.According to (i) of the process of the present invention, the stream SLO is provided. Generally, there no particular restrictions how this stream is provided. Preferably, providing the stream SLO according to (I) comprises(1.1) providing a stream SM comprising a solid material M comprising polyamide 6;(1.2) preparing an aqueous depolymerization mixture based on SM;(1.3) subjecting the depolymerization mixture prepared according to (1.2) to polyamide 6 depolymerization conditions in a reaction unit UR, obtaining a liquid aqueous stream S comprising E-caprolactam dissolved in water at a concentration CSR, the stream SR further comprising one or more impurities;(1.4) preferably passing the liquid aqueous stream SR into an evaporation unit UE, obtaining from SR a liquid aqueous stream SL comprising E-caprolactam dissolved in water at a concentration CSL with CSL > CSR, and further obtaining from SR one or more aqueous vapor streams Sv;(1.5) passing the aqueous stream SR, preferably the aqueous stream SL, into a heat-consuming purification unit URI, obtaining from SR, preferably from SL, the stream SLO and further obtaining from SR, preferably from SL, one or more aqueous streams SRW, wherein at least part of the heat consumed in URI is preferably provided by at least one of the one or more streams Sv, thereby obtaining from the at least one stream Sv at least one at least partially condensed aqueous stream Svw;(1.6) preferably recycling at least one stream Svw at least partially to the reaction unit UR and at least one stream SRW at least partially to the reaction unit UR.Also preferably, the stream SLO provided according to (I) is obtainable or obtained by a method comprising(1.1) providing a stream SM comprising a solid material M comprising polyamide 6;(1.2) preparing an aqueous depolymerization mixture based on SM;(1.3) subjecting the depolymerization mixture prepared according to (1.2) to polyamide 6 depolymerization conditions in a reaction unit UR, obtaining a liquid aqueous stream SR comprising E-caprolactam dissolved in water at a concentration CSR, the stream SR further comprising one or more impurities;(1.4) preferably passing the liquid aqueous stream SR into an evaporation unit UE, obtaining from SR a liquid aqueous stream SL comprising E-caprolactam dissolved in water at a concentration CSL with CSL > CSR, and further obtaining from SR one or more aqueous vapor streams Sv;(1.5) passing the aqueous stream SR, preferably the aqueous stream SL, into a heat-consuming purification unit URI, obtaining from SR, preferably from SL, the stream SLO and further obtaining from SR, preferably from SL, one or more aqueous streams SRW, wherein at least part of the heat consumed in URI is preferably provided by at least one of the one or more streams Sv, thereby obtaining from the at least one stream Sv at least one at least partially condensed aqueous stream Svw;(1.6) preferably recycling at least one stream Svw at least partially to the reaction unit UR and at least one stream SRW at least partially to the reaction unit UR.The solid material M according to (1.1) preferably comprises, more preferably consists of, waste material, wherein said waste material more preferably comprises, more preferably consists of, one or more of at least one textile waste material and at least one engineering plastics waste material, more preferably comprises, more preferably consists ofat least one 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 the solid material M consist of the polyamide.Preferably, in addition to polyamide 6, the solid material M comprises one or more further organic polymeric compounds, more preferably including, but not limited to, one or more of at least one elastane; at least one polyamide 6.6; at least one semiaromatic polyamide including one or more of polyamide 6T and polyamide 6I; at least one polyethylene terephthalate; at least one polyurethane; at least one polyester; at least one polyether; at least one polyvinyl chloride; at least one natural fiber material such as wool and cotton; at least one cellulose material; at least one natural elastomer; at least one synthetic elastomer; at least one copolymer of two or more of said polymeric compounds including statistical copolymers, gradient copolymers, alternating copolymers, block copolymers, and graft copolymers; and at least one rubber material comprising one or more of at least one natural rubber material and at least one synthetic rubber material.Prior to being provided to the process of the present invention, the collected textile waste material can be suitably sorted. In this regard, it is possible to spread the collected textile waste material on a conveyor, which spreading can be carried out either manually and / or mechanically. Thereafter, the respectively spread textile waste material is subjected to sorting, either by composition and / or by color. Sorting can be carried out either manually and / or optically. If carried out optically, the sorting preferably comprises an infrared sorting, more preferably a near-infrared sorting and / or a mid-infrared sorting. Optionally, prior to sorting, the textile waste material can be subjected to a suitable metal removing step. If a metal removing step is carried out, ferrous elements are preferably separated, for example by suitable magnetic means, and / or non-ferrous elements are preferably separated, for example by suitable eddy current separating means. After said sorting, the respectively obtained textile waste material can be subjected to a further treatment, such as cutting and / or milling.Generally, the solid material M can be provided according to any suitable method. Preferably according to the present invention, providing the solid material M comprises providing the solid material M in a delivering unit UMD, wherein UMD preferably comprises one or more of at least one big bag station and at least one a bulk container station; passing the provided solid material M via a first connecting line from the unit UMD to a material collecting unit UMC, preferably a collecting drum, wherein the first connecting line preferably comprises one or more of at least one material receiving and discharge unit UMRD, at least one first material feeding unit UFMF, and at least one first particle separation unit UFMPS; passing the solid material M from the unit UMC via a second connecting line to a unit UM as described herein, wherein the second connecting line preferably comprises one or more of at least one second material feeding unit USMF, at least one second particle separation unit USMPS, and at least one metal detector.Preferably, the solid material M is provided in the form of granules, wherein the particle size distribution of said granules is preferably characterized by one or more of the following pairs of values, preferably by two or more of the following pairs of values, more preferably by the following three pairs of values: a D10 value of the particle width in the range of from in the range of from 0.1 to 15 mm and a D10 value of the particle length in the range of from 0.3 to 15 mm; a D50 value of the particle width in the range of from in the range of from 0.2 to 20 mm and a D50 value of the particle length in the range of from 0.5 to 20 mm; a D90 value of the particle width in the range of from in the range of from 0.3 to 30 mm and a D90 value of the particle length in the range of from 0.8 to 30 mm.Generally, the aqueous depolymerisation mixture can be prepared according to any method. Preferably, preparing the aqueous depolymerization mixture according to comprises melting in a melting unit UM the solid material M, obtaining the liquid stream SM having a temperature TSM at a pressure PSM; admixing in a pre-reaction unit UPR the stream SM with an aqueous stream Sw having a temperature Tsw at a pressure psw, obtaining a liquid reaction feed stream SF having a temperature TSF at a pressure PSF; feeding the stream SF obtained according to (i.3.2) as the depolymerization mixture into the chemical reaction unit UR. AS far as this process design is concerned, it is preferred that0.8 < TSF / TD 1 .05 and 0.9 < PSF / PD 1 .05;0.6 < TSM / TSF 1.2 and 0.9 < PSM / PSF 1.05; and0.8 — TSW / TSF — 1.2 and 0.9 — psw / psF — 1 .05.The pre-reaction unit UPR preferably comprises, more preferably consists of, a mixing unit, preferably a static mixing unit, and wherein the melting unit UM comprises, preferably consists of an extruder, preferably a single-screw extruder or a twin-screw extruder. Further, it is preferred that Sw and SM are admixed in UPR at a mixing ratio (mw / kg) I (mp / kg) 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, wherein mw is the amount of water comprised in Sw and mp is the amount of polyamide 6 comprised in SM.As far as the hydrolytic depolymerization according to the present invention is concerned, it is preferred that the depolymerization pressure PD in the unit UR is in the range of from 40 to 140 bar, more preferably in the range of from 40 to 125 bar, more preferably in the range of from 40 to 110 bar; and the depolymerisation temperature TD in the unit UR is in the range of from 230 to 335 °C, more preferably in the range of from 250 to 320 °C, more preferably in the range of from 270 to 310 °C.Preferably, the reaction unit UR 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 1 to 8, more preferably in the range of from 1 to 6, more preferably in the range of from 1 to 5, more preferably in the range of from 1 to 4, more preferably in the range of from 1 to 3. If z > 1, is preferred that at least 2 reactors R, more preferably all z reactors R, are serially coupled, whereinthe stream SF is fed into R, with i = 1 ; an aqueous liquid stream Si containing E-caprolactam dissolved in water is removed from reactor R and fed into the reactor +i, with i < z; the aqueous liquid stream Szcontaining E-caprolactam dissolved in water is removed from the reactor Rzas the stream SR; wherein in every reactor R, a depolymerization temperature TDI at a depolymerization pressure PDI is maintained, wherein, independently of each other, TDI is in the range of from 230 to 330 °C and PDI is in the range of from 40 to 140 bar, preferably wherein TDI is in the range of from 250 to 320 °C and PDI is in the range of from 40 to 125 bar, more preferably wherein TDI is in the range of from 270 to 310 °C and PDI is in the range of from 40 to 110 bar. For z > 1, it is preferred that the z reactors R are vertically arranged, with Ri being the top-most reactor and Rzbeing the bottom-most reactor, wherein Si obtained from Rj is transferred to Rj+i by gravity, preferably by gravity only. More preferably, at least 1, preferably all z reactors R, are continuous stirred tank reactors (CSTR). Preferably, every continuous stirred tank reactor R has, independently from each other, from 2 to 6 compartments, more preferably from 2 to 5 compartments, more preferably from 2 to 4 compartments, said compartments preferably being serially, more preferably being serially and vertically arranged, wherein 2 adjacent compartments are separated by a divider which comprises at least one flow-through opening. Preferably at least one compartment comprised in a reactor R comprises at least one agitator, wherein more preferably every compartment of every reactor R comprises at least one agitator, wherein more preferably, every compartment of every reactor R comprises one agitator, and the process comprises agitating the depolymerization mixture in a given compartment for at least part of the time during subjecting to depolymerization conditions in said compartment. Preferably, the polyamide 6 depolymerization conditions further comprise a total residence time to of the aqueous depolymerization mixture in the unit U , preferably in the z reactors R, more preferably in the z continuous stirred tank reactors, wherein at least 85 weight- %, preferably at least 90 weight-%, more preferably at least 95 weight-% of the aqueous depolymerization mixture have a to in the range of from 30 to 90 min. More preferably, the residence time of an aqueous depolymerization mixture in a reactor R is toi and 0.90 < (toi I bi+i) 1 .10, more preferably 0.95 < (foi I tow) 1 .05.If the solid material M comprises one or more elastanes, the aqueous liquid stream SR obtained from the depolymerization reaction usually contains one or more decomposition products which are formed from the one or more elastanes, for example in the course of the depolymerization reaction in UR. Additionally or alternatively, one or more decomposition products form the one or more elastanes may also be formed in the melting unit UM which is described above. By way of example, said one or more decomposition products from the one or more elastanes preferably include at least one of aniline, butanediol, butanediol oligomers including, for example, butandediol dimer and butanediol trimer, and 4,4’-methylenedi ani line (MDA) and isomers thereof such as 2, 4'-methy lenedianil ine and 2,2'-methylenedianiline.According to the present invention, it is preferred that the purification unit URI according to (i.5) comprises a heatconsuming water separation unit Uwsi, wherein the process further process comprises feeding the stream SL to Uwsi, obtaining from Uwsi the stream SLO. While not being restricted to any specific purification units, it is preferredaccording to the present invention that Uwsi comprises, preferably is an evaporation unit, preferably comprising a film evaporator, more preferably a falling film evaporator, wherein said film evaporator is more preferably equipped with heating means to provide heat for evaporation. Optionally, the unit Uwsi may comprise two or more evaporation subunits, preferably two or more serially coupled evaporation sub-units.Preferably according to the present invention, the gas stream Sv2 obtained from the separation unit Us2 and essentially consisting of water and the at least one inert gas G is passed to a further separation stage where water is separated. According to this additional separation stage, it is possible, for example, to efficiently re-use the at least one inert gas for stripping purposes as described herein. Therefore, the process of the present invention preferably further comprises(v) producing in a separation unit Us3 from the stream Sv2 a gas stream Sv3 and an aqueous liquid stream Si_3, comprising(v.1) passing the stream Sv2 removed from the separation unit Us2 into the separation unit Us3 and subjecting the stream Sv2 in the unit Us3 to separation conditions;(v.2) removing the stream Sv3 from the separation unit Us3, the stream Sv3 exhibiting a concentration cvs(G) of the at least one inert gas G and a concentration cvs(W) of water, with cvs(W) < cv2(W) and cvs(G) > CV2(G);(v.3) removing the stream S from the separation unit Us3, the stream S exhibiting a concentration CL3(W) of water and a concentration cvs(G) of the at least one inert gas G, with CL3(W) > cvs(W) and CL3(G) < Cvs(G).Preferably, the separation unit Us3 is a partial condensation unit, and more preferably, Us3 comprises one or more of a plate heat exchanger and a tube shell heat exchanger. More preferably, the separation unit Us3 according to (v) is a scrubbing unit, preferably comprising a packed column, and as far as the production of the gas stream Sv3 and the aqueous liquid stream SL3 from the stream Sv2 in the scrubbing unit Us3 is concerned, it preferably comprises (v.1) passing the stream Sv2 removed from the scrubbing unit Us2 into the scrubbing unit Us3 and subjecting the stream Sv2 in the unit Us3 to scrubbing conditions;(v.2) removing the stream Sv3 from the scrubbing unit Us3, the stream Sv3 having a temperature Tvs with Tvs < Tv2 and exhibiting a concentration cvs(G) of the at least one inert gas G and a concentration cvs(W) of water, with cv3(W) < cv2(W) and cV3(G) > cV2(G);(v.3) removing the stream Su from the scrubbing unit Us3, the stream Su having a temperature Tu with Tvs < Tu < TV2 and exhibiting a concentration cu(W) of water and a concentration cvs(G) of the at least one inert gas G, with cu(W) > cv3(W) and cu(G) < Cvs(G).The temperature of the stream Su obtained according to (v.3) is preferably in the range of from 55 to 80 °C, more preferably in the range of from 65 to 80 °C, more preferably in the range of from 75 to 80 °C. Regarding the concentrations, it is preferred that cu(W) + cu(G) is in the range of from 95 to 100 weight-%, more preferably in the range of from 98 to 100 weight-%, more preferably in the ranoe of from 99 to 100 weight-%, based on the weight ofthe stream SL3. Preferably, in the stream Si.3, the weight ratio of water to the at least one inert gas is at least 320: 1 , preferably at least 400:1, more preferably at least 500:1.In addition to the stream Si_3, a gas stream Sv3 is obtained from the unit Us3 which is, compared to the stream Sv2, depleted in water and, respectively, enriched in the at least one inert gas G. The temperature of the stream Sv3, Tvs, is preferably in the range of from 25 to 40 °C, more preferably in the range of from 25 to 35 °C, more preferably in the range of from 25 to 30 °C. The pressure of the stream Sv3, Pv3, is preferably in the range of from 1 to 4 bar, more preferably in the range of from 1 to 3 bar, more preferably in the range of from 1 to 2 bar. Regarding the concentrations, it is preferred that cvs(G) + cvs(W) is in the range of from 98 to 100 weight-%, more preferably in the range of from 99 to 100 weight-%, more preferably in the range of from 99.5 to 100 weight-%, more preferably in the range of from 99.6 to 100 weight-%, more preferably in the range of from 99.7 to 100 weight-%, based on the weight of the stream Sv3. Preferably, in the stream Sv3, the weight ratio of the at least one inert gas to water is at least 31 :1, preferably at least 35:1, more preferably at least 40:1.Preferably according to the present invention, (v) further comprises(v.4) dividing the stream SL3 in at least a stream Si_3i having a temperature TLSI with TLSI = Tu and a stream Si_32 having a temperature TL32 with TL32 = TLS; subjecting the stream Si_3i to cooling, obtaining a cooled stream SLSIC having a temperature TLSIC < TLSI ; and feeding the stream Si_3ic back into the scrubbing unit Us3, wherein the scrubbing conditions according to (v.1) comprise bringing the gas stream Sv2 into contact with the liquid stream S 3ic.The temperature TLSI c is preferably in the range of from 25 to 40 °C, more preferably in the range of from 25 to 35 °C, more preferably in the range of from 25 to 30 °C. It is preferred that according to (v.1), the stream Sv2 is passed into the scrubbing unit Us3 at a mass flow rate pv2 and the stream Si_3i c is passed the scrubbing unit Us3 at a mass flow rate |JL3IC, wherein |Jv2 / PLSIC is in the range of from 0.3:1 to 0.6:1, preferably in the range of from 0.4:1 to 0.5:1, more preferably in the range of from 0.45:1 to 0.48:1 . In the scrubbing unit Us3, the stream Sv2 and the stream Si_3ic are brought into contact with each other so as to provide suitable stripping conditions; preferably, they are brought into contact in counter-current mode or in co-current mode or in cross-flow mode, more preferably in counter-current mode.Regarding the stripping step and the subsequent downstream separation steps carried out in Us2 and Us3, preferably the subsequent downstream scrubbing steps of the present invention, the process exhibits a water separation efficiency Q(W) preferably of at least 65 %, more preferably at least70 %, more preferably at least 75 %, with Q(W) = PL32(W) I PLO(W), wherein PLO(W) is the mass flow rate of water in the stream SLO, expressed in kg / h, and |JL32(W) is the mass flow rate of water in the stream Si_32, expressed in kg / h.Thus, preferred designs of the process of the present invention exhibita high boiler separation efficiency Q(X), preferably of at least 95 %, more preferably at least 96 %, more preferably at least 97 %, more preferably at least 98 %, more preferably at least 99 %, with Q(X) = |JLI(X) I LO(X), wherein |JLO(X) is the mass flow rate of the at least one compound X in the stream SLO, expressed in kg / h, and |JLI (X) is the mass flow rate of the at least one compound X in the stream SLI, expressed in kg / h; and an E-caprolactam separation efficiency Q(C) of at least 94 %, preferably at least 96 %, more preferably at least 98 %, with Q(C) = pi_22(C) I PLO(C), wherein |JLO(C) is the mass flow rate of E-caprolactam in the stream SLO, expressed in kg / h, and PL22(C) is the mass flow rate of E-caprolactam in the stream SL22, expressed in kg / h; and a water separation efficiency Q(W) of at least 65 %, preferably at least 70 %, more preferably at least 75 %, with Q(W) = PL32(W) I PLO(W), wherein PLO(W) is the mass flow rate of water in the stream SLO, expressed in kg / h, and PL32(W) is the mass flow rate of water in the stream SL32, expressed in kg / h.As mentioned herein, a preferred process of the present invention advantageously allows for re-using the at least one inert gas G separated in Us2 and Us3. Therefore, the present invention also relates to the process as described herein, further comprising(vi) passing the stream Sv3 having the temperature Tvs, or a part stream thereof, into the stripping unit Usi.Therefore, it is preferred that at least a part of the stream SGO provided according to (II) and passed into the stripping unit Usi according to (ill.1 ) consists of the stream Sv3 or the part stream thereof. According to the present invention, it is conceivable to discharge a part of the stream Sv3 from the system as a purge stream, which part is therefore not fed back to Usi ■ Depending on the specific process design, such a purge stream may turn out to be desirable to avoid an accumulation of any impurities in the system, including, for example, water.Generally, when starting-up the process of the present invention, an external stream SGO, for example taken from a suitable grid, is passed, after optionally heating to the desired temperature TGO, into Usi ■ In the course of the process, the stream Sv3 is then preferably produced, and at least a part of the stream SGO can be provided by Sv3 or a part stream thereof. During the process, the stream Sv3 or the part stream thereof can be supplemented by a suitable make-up stream comprising the at least inert gas, wherein the make-up stream is preferably combined with Sv3 of the part stream thereof prior to the heating in UHI as described herein.When the stream Sv3 or a part stream thereof is fed back to Usi, the process of the present invention further allows for an advantageous heat integration method. In particular, it is preferred that prior to being passed into the stripping unit Usi, the stream Sv3 or the part stream thereof is passed through a heating unit UHI , the process comprising heating the stream Sv3 or the part stream thereof from the temperature Tvs to the temperature TGO. Preferably, said heating unit UHI comprises a heat exchange sub-unit UHEI, and the process preferably comprises passing the stream Svi through UHEI and heating the stream Sv3 from the temperature Tvs to a temperature T*v3 in UHEI with Tvs < T*v3 TGO, wherein at least a part of the heat for heating the stream Sv3 in UHEI to the temperature T*v3 is provided by thestream Svi. According to the present invention, it is further conceivable that prior to heating the stream Sv3 via Svi in UHI, the stream Sv3 is pre-heated wherein said pre-heating may be carried out in a pre-heating unit UPHI in which at least a part of the heat for pre-heating the stream Sv3 is provided by the stream Sv2 from Us2.Yet further according to the present invention, in particular in case T*v3 < TGO, the heating unit UHI further preferably comprises a heating sub-unit UHSI arranged downstream of the heat exchange sub-unit UHEI , and the process preferably comprises passing the stream Sv3 obtained from the heat exchange sub-unit UHEI and having the temperature T*v3 through the heating sub-unit UHSI and heating the stream Sv3 from the temperature T*v3 to the temperature TGO in UHSI.Preferably, T*v3 is in the range of from 40 to 95 °C, more preferably in the range of from 50 to 85 °C, more preferably in the range of from 65 to 75 °C.As already mentioned, the process of the present invention allows for passing the stream SL2 obtained from Us2 directly to a fine purification stage, more preferably comprising a fine distillation stage, without the need of an intermediate water separation stage. Therefore, the process preferably further comprises(vii) passing the stream SL2 obtained according to (iv.3), or the stream Si_22 obtained according to (iv.4), into a purification unit UP, obtaining from SL2 or Si_22 a stream SCPL exhibiting a concentration CCPL(C) of monomeric E- caprolactam with CCPL(C) > CL2 (C) or CCPL(C) > CL22(C); wherein the purification unit UP comprises a distillation unit UDI, the process comprising feeding the stream SL2 or the stream Si_22 to UDI, obtaining from UDI a stream SDI exhibiting a concentration CDI(C) of monomeric E-caprolactam with CCPL(C) S CDI(C) > cL2(C) or CCPL(C) S CDI(C) > Ci_22(C), wherein the purification unit UP preferably further comprises, downstream of the unit UDI, one or more of a crystallization unit UCR and a chemical treatment unit UOD, the process comprising obtaining the stream SCPL from UCR or from UOD.In case the purification unit UP further comprises a crystallization unit UCR located downstream of UDI, the process preferably comprises feeding the stream SDI to the crystallization unit UCR, obtaining from UCR a stream SCR being the stream SCPL comprising E-caprolactam at a concentration CCR(C) = CCPL(C).In case the purification unit UP further comprises a chemical treatment unit UOD located downstream of UDI, the process preferably comprises feeding the stream SDI to the chemical treatment unit UOD, obtaining from UOD a stream SOD being the stream SCPL comprising E-caprolactam at a concentration COD(C) = CCPL(C).In case the purification unit UP further comprises a chemical treatment unit UOD and a crystallization unit UCR, wherein the crystallization unit UCR is located downstream of the distillation unit UDI and the chemical treatment unit UOD is located downstream of the crystallization unit UCR, the process preferably comprises feeding the stream SDI to the crystallization unit UCR, obtaining from the crystallization UCR a stream SCR comprising E-caprolactam at aconcentration CCR(C) with CCR(C) > CDI(C), and feeding the stream SCR to the chemical treatment unit UOD, obtaining from UOD a stream SOD being the stream SCPL comprising E-caprolactam at a concentration COD(C) = CCPL(C).In case the purification unit UP further comprises a chemical treatment unit UOD and a crystallization unit UCR, wherein the chemical treatment unit UOD is located downstream of the distillation unit UDI and the crystallization unit UCR is located downstream of the unit UOD, the process preferably comprises feeding the stream SDI to the chemical treatment unit UOD, obtaining from the chemical treatment unit UOD a stream SOD comprising E-caprolactam at a concentration COD(C) with COD(C) > CDI(C), and feeding the stream SOD to the crystallization unit UCR, obtaining from UCR a stream SCR being the stream SCPL comprising E-caprolactam at a concentration CCR(C) = CCPL(C).While not being restricted to any specific method, it is preferred that the chemical treatment in the unit UOD comprises(a) providing a preferably liquid stream SDI comprising E-caprolactam from the distillation unit UDI or a preferably liquid stream SCR comprising E-caprolactam from the crystallization unit UCR, said stream SDI or said stream SCR further comprising one or more oxidizable organic impurity compounds Y, wherein the stream SDI or the stream SCR exhibits a weight ratio rye of the one or more organic compounds Y relative to E-caprolactam;(b) providing a stream SPM comprising at least one permanganate;(c) preparing an oxidation reaction educt mixture MOE from the stream SDI and the stream SPM, or from the stream SCR and the stream SPM, and subjecting the mixture MOE to oxidation reaction conditions, obtaining an oxidation reaction product stream SP comprising E-caprolactam, further comprising one or more oxidation products Z obtained from the oxidation of at least a part of the one or more compounds Y, and optionally further comprising a part of the one or more organic compounds Y, wherein the stream SP exhibits a weight ratio ryep of organic compound Y relative to E-caprolactam with 0 < ryep < rye and further exhibits a weight ratio rzep of the one or more products Z relative to E-caprolactam with rzep > 0;(d) separating at least a part of the one or more oxidation products Z and optionally at least a part of organic compound Y from the stream SP, obtaining the stream SOD; wherein the process optionally further comprises providing a stream SOH comprising at least one hydroxide, wherein the oxidation reaction educt mixture MOE according to (c) is prepared from the stream SOD or the stream SCR, and from the stream SPM and the stream SOH; wherein separating at least a part of the one or more oxidation products Z and optionally at least a part of organic compound Y from the stream SP according to (d) preferably comprises subjecting the stream SP obtained according to (c) to distillation in a distillation unit UDI, comprised in the chemical treatment unit UOD, obtaining from the distillation unit UDI a stream SDT comprising E-caprolactam as the stream SOD, wherein the unit UDI comprises one or more distillation columns, preferably one or two distillation columns, wherein at least one column is optionally configured as side stream column or as divided wall column.Depending on the chemical composition of the stream SLI obtained from the stripping unit Usi, it is possible according to the present invention that at least a part thereof is passed to a further separation stage. In this respect, it is preferred that the process of the present invention further comprises passing at least a part of the stream SLIremoved from the unit Usi into a separation unit Us4, obtaining from the unit Us4 a vapor stream Sv4 and a liquid stream SL4, wherein the vapor stream Sv4 exhibits a total concentration cv4(X) of one or more compounds X and a concentration cv4(C) of monomeric E-caprolactam and wherein the liquid stream SL4 exhibits a total concentration cL4(X) of one or more compounds X and a concentration CL4(C) of monomeric E-caprolactam, with CL4(X) > cv4(X) and CL4(C) < Cv4(C). In case at least one of the one or more compounds X comprised in the stream SL4 is an organic polymeric compound, the process may preferably further comprise passing at least a part of the stream SL4 to a suitable depolymerization unit. With regard to the stream Sv4, it may be preferred to pass at least a part thereof as educt stream in addition to the stream Svi into the separation unit Us2. While there are no specific restrictions with regard to the design of the separation unit Us4, it may be preferred that it comprises or consists of a thin film evaporator. Yet further according to the present invention, it is conceivable that a certain part of the stream SLI is fed back to Usi as part of the educt stream. Due to the temperature TLI of this part of the stream SM , a lesser amount of the stream SGO may be necessary for heating purposes.According to the present invention, it is conceivable that downstream of the separation unit Usi or, if realized, downstream of the separation unit Us4, a part of the stream SLI and / or at least a part of the stream SL4 is subjected to suitable cooling, for example in a belt cooler like a steel belt cooler. After cooling, it may be preferred either to discard the cooled material and / or to subject it to a suitable further use.Yet further, the present invention relates to a stream SCPL comprising highly purified E-caprolactam, the stream SCPL being obtainable or obtained by a process as describe herein. Yet further, the present invention relates to the use of said stream SCPL as an educt material for a chemical process, preferably for a polymerization reaction, more preferably for preparing polyamide 6. Yet further, the present invention relates to a method for preparing polyamide 6, comprising(A) preparing a stream SCPL according to a process as described herein;(B) subjecting the stream SCPL, optionally after storing, to polyamide 6 polymerization conditions.Yet further, the present invention relates to polyamide 6, obtainable or obtained by said method.Still further, the present invention relates to the process described herein from which the stream SCPL is obtained, wherein the process further comprises providing at least part of the stream SCPL to a polyamide 6 production unit UPP, wherein the polyamide 6 produced in UPP is preferably provided as a feedstock to a textile material producing unit UTP, from which unit UTP(A) a textile material MTE is obtained which is brought onto the market, wherein, after the lifetime TMTE of said textile material MTE, it is at least partially collected as textile waste material in a textile material collecting unit UTC;(B) remaining material MRE is obtained as textile waste material;wherein at least part of the textile waste material according to (A), or at least part of the textile waste material according to (B), or at least part of the textile waste material according to (A) and at least part of the textile waste material according to (B) is suitably provided as material M according to (1.1) as defined herein.Still further, the present invention relates to the process described herein from which the stream SCPL is obtained, wherein the process further comprises providing at least part of the stream SCPL to a polyamide 6 production unit UPP, wherein the polyamide 6 produced in UPP is preferably provided as a feedstock to an engineering plastics material producing unit UEP, from which unit UEP(A) an engineering plastics material MEP is obtained which is brought onto the market, wherein, after the lifetime TMEP of said engineering plastics material MEP, it is at least partially collected as engineering plastics waste material in an engineering plastics material collecting unit UEC;(B) remaining material MRE is obtained as engineering plastics waste material; wherein at least part of the engineering plastics waste material according to (A), or at least part of the engineering plastics waste material according to (B), or at least part of the engineering plastics waste material according to (A) and at least part of the engineering plastics waste material according to (B) is suitably provided as material M according to (1.1) as defined herein.Still further, the present invention relates to the use of the stream SCPL as described herein for preparing polyamide 6, said use preferably further comprising employing said polyamide 6 as a feedstock for preparing one or more of a textile material and an engineering plastics material, more preferably for preparing a textile material.Still further, the present invention relates to a method for preparing polyamide 6, said method comprising employing the stream SCPL as described herein as a starting material, wherein said method preferably further comprises employing said polyamide 6 as a feedstock for preparing one or more of a textile material and an engineering plastics material, more preferably for preparing a textile material.According to a further aspect, the present invention relates to an integrated process for preparing polyamide 6, comprising(a) preparing a stream SCPL according to a process as described herein, said stream SCPL comprising purified E- caprolactam;(p) passing the stream SCPL to a polyamide 6 production unit UPA;(y) subjecting the stream SCPL in UPA to c-caprolactam polymerization conditions, obtaining from UPA a polyamide 6 material MP and a stream comprising water and one or more c-caprolactam oligomers;(5) optionally subjecting the stream comprising water and one or more c-caprolactam oligomers to concentration with respect to the one or more c-caprolactam oligomers in at least one concentration stage, obtaining a concentrated stream comprising water and one or more c-caprolactam oligomers;(E) passing the optionally concentrated stream comprising water and one or moreE-caprolactam oligomers into the melting unit UM.Preferably, the optionally concentrated stream comprising water and one or more E-caprolactam oligomers according to (E) further comprises E-caprolactam, i.e. monomeric E-caprolactam. Further preferably, said integrated process comprises(y) subjecting the stream SCPL in UPA to E-caprolactam polymerization conditions, obtaining from UPA a polyamide 6 material MP and a stream SEW comprising water at a concentration CEW(W), E-caprolactam at a concentration CEW(C), and one or more E-caprolactam oligomers at a total concentration CEW(O);(5) subjecting the stream SEW to concentration, comprising subjecting the stream SEW to concentration in a first concentration unit Uci, obtaining from Uci a concentrated stream Sci comprising water at a concentration Cci(W), E-caprolactam at a concentration cci (C), and one or more E-caprolactam oligomers at a total concentration Cci(O), with Cci(W) < CEW(W), CCI (C) > CEW(C) and Cci(O) > CEW(O), and further obtaining from Uci an aqueous stream Swi comprising water at a concentration Cwi(W) > CEW(W);(E) passing the stream Sci to the sub-unit UM.More preferably according to the present invention, (y) comprises(y.1 ) passing the stream SCPL and preferably an aqueous stream SAQO to a polymerization stage STo, obtaining from STo a polyamide 6 crude product stream SPAI and an aqueous stream SWAI;(y.2) passing the stream SPAI and preferably an aqueous stream SAQI to a granulation stage ST 1, obtaining from STi a crude granulated polyamide 6 material MPA2 and an aqueous stream SWA?;(y.3) passing the material MPA2 and preferably an aqueous stream SAQ2 to an extraction stage ST2, obtaining from ST2 a purified granulated polyamide 6 material MPA3 and an aqueous stream SWAS;(y.4) passing the material MPA3 to a drying stage ST3, obtaining from ST3 the polyamide 6 material MP and an aqueous stream SWA4.In particular regarding the process of the present invention comprising (y.1) to (y.4) above, it is preferred that the stream Swi obtained from Uci according to (5 is passed back to the polyamide 6 production unit UPA. More preferably, the stream Swi is passed back to UPA as at least part of one or more of the streams SAQO, SAQI and SAQ2.Assuming that some of the polyamide 6 material obtained from the production unit UPA does not meet the specifications, the process may preferably further comprise passing at least some of said material MPR to the unit UM.According to another aspect, the present invention relates to a process, preferably to the process as described above, which comprises the step of converting the stream SLI obtainable or obtained by the process as described herein and / or the stream SCPL obtainable or obtained by the process as described herein and / or a chemical material obtainable by or obtained by the process as described herein to obtain a product Q.Preferably, the product Q is selected from:building block or monomer; or polymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; or cleaning polymer, cleaning surfactant, descaling compound, cleaning biocide or composition or formulation thereof; or agrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; or active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, human food additive, dietary supplements, aroma chemical or aroma composition; or aqueous polymer dispersion, preferably polyurethane or polyurethane - poly(meth)acrylate hybrid polymer dispersion, emulsion, binder for paper and fiber coatings, UV-curable acrylic polymer for hot melts and coatings polyisocyanates, hyperbranched polyester polyol, polymeric dispersant for inorganic binder compositions, unsaturated polyester polyol or 100% curable composition; or cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or composition or formulation thereof; or polymer B, polymer composition B, coating composition, other functional composition, foil, molded body, coating or coated substrate.Regarding this process from which the product Q, is obtained, it is preferred: that the content of SLI and / or SCPL and / or the chemical material in the product Q is 1 weight-% or more, preferably 2 weight-% or more, more preferably 5 weight-% or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and / or that the content of SLI and / or SCPL and / or the chemical material in the product Q is 100 weight-% or less, preferably 95 weight-% or less, more preferably 90 weight-% or less, more preferably 50 weight-% or less, more preferably 25 weight-% or less, more preferably 10 weight-% or less; and preferably wherein the content is determined based on identity preservation and / or segregation and / or mass balance and / or book and claim chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard.The publication Prior Art Disclosure; Issue 684; paragraphs

[1000] to

[8005] ; ISSN: 2198-4786; published: February 12, 2024 will be regarded as Reference RF1, which is incorporated herein by reference in its entirety. Preferably, the product Q is a product as described in Reference RF1; paragraphs

[1000] to

[8005] , Preferably, the process described herein is further a process for the production of a product.The converting step to obtain the product Q preferably comprises one or more step(s) as described below and can be performed by conventional methods well known to a person skilled in the art. The converting step preferably comprises one or more step(s) selected from: recycling, preferably depolymerizing, gasifying, pyrolyzino. and / or steam cracking; and / orpurifying, preferably crystallizing, (solvent) extracting, distilling, evaporating, hydrotreating, absorbing, adsorbing and / or subjecting to ion exchanger; and / or assembling, preferably foaming, synthesizing, chemical conversion, chemically transforming, polymerizing and / or compounding; and / or forming, preferably foaming, extruding and / or molding; and / or finishing, preferably coating and / or smoothing.In addition, the one or more step(s) are described in detail in Reference RF1; paragraphs

[1000] to

[8005] ,The term "building block”, as used in the context of the product Q herein, comprises compounds, which are in a gaseous or liquid state under standard conditions of 0°C and 0.1 MPa. Building blocks are typically used in chemical industry to form secondary products, which provide a higher structural complexity and / or higher molecular weight than the building block on which the secondary product is based. The building block is preferably selected from the group consisting of hydrogen, carbon monoxide, carbon dioxide, ethylene oxide, ethylene glycols, syngas comprising a mixture of hydrogen and carbon monoxide, alkanes, alkenes, alkynes and aromatic compounds. The alkanes, alkenes, alkynes and aromatic compounds comprise in particular 1 to 12 carbon atoms, respectively.The term "monomer”, as used in the context of the product Q herein, comprises molecules, which can react with each other to form polymer chains by polymerization. The monomer is preferably selected from the group consisting of (meth)acrylic acid, salts of (meth)acrylic acid; in particular sodium, potassium and zinc salts; (meth)acrolein and (meth)acrylates. (Meth)acrylates comprising 1 to 22 carbon atoms are preferred, in particular comprising 1 to 8 carbon atoms. The terms (meth)acry lie acid, (meth)acrolein or (meth)acrylate relate to acrylic acid, acrolein or acrylate and also to methacrylic acid, methacrolein or methacrylate, where applicable. Further, the monomer can be selected from hexamethylenediamine (HMD) and adipic acid.The building block can further be an intermediate compound. The term "intermediate compound”, as used in the context of the product Q herein, comprises organic reagents, which are applied for formation of compounds with higher molecular complexity. The intermediate compound can be selected for example from the group consisting of phosgene, polyisocyanates and propylene oxide. The polyisocyanates are in particular aromatic di- and polyisocyanates, preferably toluene diisocyanate (TDI) and / or diphenylmethane diisocyanate (MDI).The building block and the monomer and typical converting step(s) to obtain the building block or monomer are described in more detail in paragraphs

[1000] to

[1012] of Reference RF1.The term "polymer A”, as used in the context of the product Q herein, comprises thermoplastic, e.g., polyamide or thermoplastic polyurethane, thermoset, e.g., polyurethane, elastomer, e.g., polybutadiene, or a copolymer or a mixture thereof and is defined in more detail in paragraphs

[2001] to

[2007] of Reference RF1. The term "polymer composition A”, as used in the context of the product Q herein, comprises all compositions comprising a polymer as described above and one or more additive(s), e.g. reinforcement, colorant, modifier and / or flame retardant, and isdefined in more detail in paragraph

[2008] of Reference RF1 . The term "polymer product A”, as used in the context of the product Q herein, comprises any product comprising the polymer A and / or polymer composition A as described above and is defined in more detail in paragraphs

[2009] and

[2010] of Reference RF1 . The step(s) to obtain the polymer, preferably polymer A, polymer composition, preferably polymer composition A or polymer product, preferably polymer product A is / are described in more detail in paragraph

[2011] of Reference RF1 .The term "industrial use polymer”, as used in the context of the product Q herein, comprises rheology, polycarboxylate, alkoxylated polyalkylenamine, alkoxylated polyalkylenimine, polyether-based, dye inhibition and soil release cleaning polymers defined in more detail in paragraphs

[3035] to

[3044] of Reference RF1. The term "industrial use surfactant”, as used in the context of the product Q herein, comprises non-ionic, anionic and amphoteric industrial use surfactants defined in more detail in paragraphs

[3008] to

[3034] of Reference RF1. The term "industrial use descaling compound”, as used in the context of the product Q herein, comprises non-phosphate based builders (NPB) and phosphonates (CoP) described in more detail in paragraphs

[3001] to

[3005] of Reference RF1 . The term "industrial use biocide”, as used in the context of the product Q herein, refers to a chemical compound that kills microorganisms or inhibits their growth or reproduction defined in more detail in paragraphs

[3006] to

[3007] of Reference RF1 . The term "industrial use solvent”, as used in the context of the product Q herein, comprises alkyl amides, alkyl lactamides, alkyl esters, lactate esters, alkyl diester, cyclic alkyl diester, cyclic carbonates, aromatic aldehydes and aromatic esters defined in more detail in paragraphs

[3045] to

[3055] of Reference RF1 . The term "industrial use dispersant”, as used in the context of the product Q herein, comprises anionic and non-ionic industrial use dispersants defined in more detail in paragraphs

[3056] to

[3058] of Reference RF1. The term "composition and / or formulation thereof' with reference to the industrial use polymers, industrial use surfactants, descaling compounds and / or industrial use biocides refers to industrial use compositions and / or institutional use products and / or fabric and home care products and / or personal care products defined in more detail in paragraph

[3059] of Reference RF1. The converting step(s) to obtain the industrial use polymer, industrial use surfactant, descaling compound and / or industrial use biocide are defined in more detail in paragraph

[3060] of Reference RF1. The converting steps to obtain the industrial use composition or formulation of the industrial use polymer, industrial use surfactant, descaling compound and / or industrial use biocide are defined in more detail in paragraph

[3061] of Reference RF1.The term "agrochemical composition”, as used in the context of the product Q herein, typically relates to a composition comprising an agrochemically active ingredient and at least one agrochemical formulation auxiliary. Examples of agrochemical compositions, active ingredients and auxiliaries are described in more detail in Reference RF1, paragraph

[4001] , The agrochemical composition may take the form of any customary formulation. The agrochemical compositions are prepared in a known manner, e.g. described by Mollet and Grubemann, Formulation technology, Wiley VCH, Weinheim, 2001; or Knowles, New developments in crop protection product formulation, Agrow Reports DS243, T&F Informa, London, 2005. The converting step(s) to obtain the agrochemically active ingredients and auxiliaries may be conducted in analogy to the production step(s) of their analogues that are based on petrochemicals or other precursors that are not gained bv recycling processes. In addition, conversion tocompounds mentioned in sections "Polymer” and "Cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or compositions or formulations thereof' may be performed as described in these sections as well as the respective paragraphs in Reference RF1.The term active pharmaceutical ingredients and / or intermediates thereof, as used in the context of the product Q herein, comprises substances that provide pharmacological activity or other direct effect in the diagnosis, cure, mitigation, treatment, or prevention of disease, or to affect the structure or any function of the body. Intermediates thereof are isolated products that are generated during a multi-step route of synthesis of an active pharmaceutical ingredient. The term pharmaceutical excipients, as used in the context of the product Q herein, comprises compounds or compound mixtures used in compositions for various pharmaceutical applications, which are not substantially pharmaceutically active on itself. Active pharmaceutical ingredients and / or intermediates thereof and pharmaceutical excipients are defined in more detail in paragraph

[5001] of Reference RF1. The converting step(s) to obtain the active pharmaceutical ingredients and / or intermediates thereof and pharmaceutical excipients may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.The terms animal feed additives, human food additives, dietary supplements, as used in the context of the product Q herein, comprises Vitamins, Pro-Vitamins and active metabolites thereof including intermediates and precursors, especially Vitamin A, B, E, D, K and esters thereof, like acetate, propionate, palmitate esters or alcohols thereof like retinol or salts thereof and any combinations thereof; Tetraterpenes, especially isoprenoids like carotenoids and xanthophylls including their intermediates and precursors as well as mixtures and derivates thereof, especially beta carotene, Canthaxanthin, Citranaxanthin, Astaxanthin, Zeaxanthin, Lutein, Lycopene, Apo-carotenoids, and any combinations thereof; organic acids, especially formic acid, propionic acid and salts thereof, such as sodium, calcium or ammonium salts, and any combinations thereof, such as but not limited to mixtures of formic acid and sodium formiate, propionic acid and ammonium propionate, formic acid and propionic acid, formic acid and sodium formiate and propionic acid, propionic acid and sodium propionate and formic acid and sodium formiate; glycerides of carboxylic acids and short and medium chain fatty acids, conjugated linoleic acids, such as omega-6 fatty acid (C18:2) methyl ester and 1 ,2-propandiol and beverage stabilizers, such as polyvinylpyrrolidone-polymer or polyvinylimidazole I polyvinylpyrrolidone-copolymer. Animal feed additives, human food additives and dietary supplements are defined in more detail in paragraph

[5002] of Reference RF1. The converting step(s) to obtain the animal feed additives, human food additives, dietary supplements may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.The terms aroma chemical and aroma composition as used in the context of the product Q herein, comprise a volatile organic substance with a molecular weight between 70-250 g / mol comprising a functional group with a carbon skeleton of C5-C16 carbon atoms comprising linear, branched, cyclic, for example with a ring size of C5-C18, bicyclic or tricyclic aliphatic chains and but not necessarily one or more unsaturated structural elements like double bonds, triple bonds, aromatics or heteroaromatics and preferably the one or more additional functional groups are selectedfrom alcohol, ether, ester, ketone, aldehyde, acetal, carboxylic acid, nitrile, thiol, amine. In one aspect, the aroma chemical is a terpene-based aroma chemical, for example selected from monoterpenes and monoterpenoids, sesquiterpenes and sesquiterpenoids, diterpenes, triterpenes or tetraterpenes. Aroma chemicals can be combined with further aroma chemicals to give an aroma composition. Aroma chemicals and aroma compositions are defined in more detail in paragraph

[5003] of Reference RF1 . The converting step(s) to obtain the aroma chemical and aroma composition may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.The term "aqueous polymer dispersion”, as used in the context of the product Q herein, comprises aqueous composition(s) comprising dispersed polymer(s) and is defined in more detail in the section

[6001] entitled "aqueous polymer dispersion” of Reference RF1 . The dispersed polymer(s) may be selected from acrylic emulsion polymer(s), styrene acrylic emulsion polymer(s), styrene butadiene dispersion(s), aqueous dispersion(s) comprising composite particles, acrylate alkyd hybrid dispersion(s), polyurethane(s) (including UV-curable polyurethanes) and polyurethane - poly(meth)acrylate hybrid polymer(s). The term "emulsion polymer”, as used in the context of the product Q herein, comprises polymer(s) made by free-radical emulsion polymerization. Aqueous polyurethane dispersion(s) are defined in more detail in the section

[6002] entitled "Polyurethane dispersions” of Reference RF1. UV-curable polyurethane(s) is / are defined in more detail in the section

[6017] of Reference RF1. Polyurethane - poly(meth)acrylate hybrid polymer(s) is / are defined in more detail in the section

[6016] of Reference RF1.The term "polymeric dispersant”, as used in the context of the product Q herein, comprises preferably polymer(s) comprising polyether side chain, in particular polycarboxylate ether polymer(s) and polycondensation product(s) defined in more detail in paragraph

[6020] entitled "Polymeric dispersant” of Reference RF1.The converting (polymerization) step(s) to obtain the aqueous polymer dispersion(s) comprising emulsion polymer(s) is / are defined in more detail in the section

[6003] entitled "Emulsion polymerization” of Reference RF1.The converting (polymerization) step(s) to obtain the aqueous polyurethane dispersion(s) is / are defined in more detail in the section

[6014] entitled "Process for the preparation of aqueous polyurethane dispersions” and section [6017)] entitled "Aqueous UV-curable polyurethane dispersions, their preparation and use and compositions containing them” of Reference RF1.Composition(s) and uses of aqueous polymer dispersion(s) and of polymeric dispersant(s) are defined in more detail in the following sections of Reference RF1 : section

[6004] entitled "Uses of aqueous polymer dispersions”, section

[6005] entitled "Binders for architectural and construction coatings” section

[6006] entitled "Binders for paper coating” section

[6007] entitled "Binders for fiber bonding” section

[6008] entitled "Adhesive polymers and adhesive compositions” section

[6015] entitled "Aqueous polyurethane dispersions suitable for use in coating compositions”section

[6016] entitled "Aqueous polyurethane - poly(meth)acrylate hybride polymer dispersions suitable for use in coating compositions” section

[6017] entitled "Aqueous UV-curable polyurethane dispersions, their preparation and use and compositions containing them” section

[6018] entitled "Inorganic binder compositions comprising polymeric dispersants and their use”

[6019] 100% curable coating compositionsUV-crosslinkable poly(meth)acrylate(s) and its / their uses are defined in more detail in section

[6009] entitled "UV- crosslinkable poly(meth)acrylates for use in UV-curable solvent-free hotmelt adhesives and their use for making pressure-sensitive self-adhesive articles” of Reference RF1.Polyisocyanate(s), composition(s) comprising them and their uses are defined in more detail in section

[6010] entitled "Polyisocyanates” of Reference RF1.Hyperbranched polyester polyol (s) and its / their uses are defined in more detail in section

[6011] entitled "Organic solvent based hyperbranched polyester polyols suitable for use in coating compositions” of Reference RF1. The converting step(s) to obtain the hyperbranched polyester polyols is / are defined in more detail in the section

[6012] entitled "Preparation of organic solvent based hyperbranched polyester polyols” of Reference RF1 . Coating composition(s) comprising hyperbranched polyester polyol(s), polyisocyanate(s) and additive(s) and substrate(s) coated therewith are defined in more detail in section

[6013] entitled "Organic solvent based two component coating compositions comprising hyperbranched polyester polyols and polyisocyanates” of Reference RF1.Unsaturated polyester polyol(s), solvent-based coating composition(s) comprising said unsaturated polyester polyol(s) and substrate(s) for coating with said coating composition(s) are defined in more detail in section

[6018] entitled "Organic solvent based coating composition comprising unsaturated polyester polyols” of Reference RF1. 100% curable coating composition(s) is / are defined in more detail in section

[6019] of Reference RF1.Polymeric dispersant(s) for inorganic binder compositions is / are defined in more detail in section

[6020] of Reference RF1. The inorganic binder composition(s) comprising the polymeric dispersants and their use are defined in more detail in section

[6021] of Reference RF1. The converting step(s) to obtain the polymeric dispersant(s) are defined in more detail in section

[6020] of Reference RF1 . The term "inorganic binder composition” comprising the polymeric dispersant(s), as used in the context of the product Q herein, comprises preferably in particular hydraulically setting compositions and compositions comprising calcium sulfate and is defined in more detail in section

[6021] of Reference RF1 entitled "Inorganic binder compositions comprising the polymeric dispersant and their use”. Specific building material formulation(s) comprising polymeric dispersant(s) or building product(s) produced by a building material formulation comprising a polymeric dispersant are disclosed in more detail in section

[6021] of Reference RF1.The term "cosmetic surfactant”, as used in the context of the product Q herein, comprises non-ionic, anionic, cationic and amphoteric surfactants and is defined in more detail in paragraph

[7002] of Reference RF1. The term "emollient”, as used in the context of the product Q herein, refers to a chemical compound used for protecting, moisturizing, and / or lubricating the skin and is defined in more detail in paragraph

[7003] of Reference RF1. The term "wax”, as used in the context of the product Q herein, comprises pearlizers and opacifiers and is defined in more detail in paragraph

[7004] of Reference RF1 . The term "cosmetic polymer”, as used in the context of the product Q herein, comprises any polymer that can be used as an ingredient in a cosmetic formulation and is defined in more detail in paragraph

[7005] of Reference RF1 . The term "UV filter”, as used in the context of the product Q herein, refers to a chemical compound that blocks or absorbs ultraviolet light and is defined in more detail in paragraph

[7006] of Reference RF1 . The term "further cosmetic ingredient”, as used in the context of the product Q herein, comprises any ingredient suitable for making a cosmetic formulation. Several sources disclose cosmetically acceptable ingredients. E. g. the database Cosing on the internet pages of the European Commission discloses cosmetic ingredients and the International Cosmetic Ingredient Dictionary and Handbook, edited by the Personal Care Products Council (PCPC), discloses cosmetic ingredients. The term "composition and / or formulation thereof” with reference to the cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter and / or further cosmetic ingredient refers to personal care and / or cosmetic compositions or formulations defined in more detail in paragraph

[7007] of Reference RF1 . The converting step(s) to obtain the cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter or further cosmetic ingredient is / are defined in more detail in paragraph

[7008] of Reference RF1 .The terms "polymer B”, "polymer composition B”, "coating composition”, "other functional composition”, "foil”, "molded body”, "coating” and "coated substrate” are well known to the person skilled in the art and are defined in more detail from paragraph

[8000] to

[8005] of Reference RF1.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 continuous process for separating one or more organic compounds X from an aqueous liquid stream SLO comprising monomeric E-caprolactam and said one or more compounds X, the process comprising(I) providing the stream SLO having a temperature TLO and exhibiting a total concentration CLO(X) of the one or more compounds X, a concentration CLO(C) of monomeric E-caprolactam, and a concentration CLO(W) of water;(ii) providing a non-aqueous stripping gas stream SGO comprising at least one inert gas G and having a temperature TGO with TGO > TLO;(iii) producing in a stripping unit Usi from the stream SLO an aqueous gas stream Svi and a liquid stream511, comprising(iii.1 ) passing the stream SLO and the stream SGO into the stripping unit Usi;(111.2) bringing the stream SLO and the stream SGO in the stripping unit Usi at stripping conditions into contact with each other, wherein the stripping conditions comprise a stripping pressure ps and wherein at the stripping pressure ps, the one or more one organic compounds X comprised in the stream SLO have a boiling point TBX and monomeric E-caprolactam has a boiling point TBC with TBX>T BC|(111.3) removing the stream Svi from the stripping unit Usi, the stream Svi having a temperature Tvi with TLO < Tvi < TGO and exhibiting a total concentration cvi(X) of one or more compounds X, a concentration cvi(C) of monomeric E-caprolactam, a concentration Cvi(W) of water and a concentration Cvi(G) of the at least one inert gas G, with cvi(C) > CLO(C) and cvi(X) < CLO(X);(111.4) removing the stream SLI from the stripping unit Usi, the stream SLI having a temperature TLI with TLO < TLI < TGO and exhibiting a total concentration CLI(X) of one or more compounds X and a concentration CLI(C) of monomeric E-caprolactam, with CLI(X) > Cvi(X) and CLI(C) < Cvi(C);(iv) producing in a separation unit Us2 from the stream Svi an aqueous gas stream Sv2 and a liquid stream512, comprising(iv.1 ) passing the stream Svi removed from the stripping unit Usi into the separation unit Us2 and subjecting the stream Svi in the unit Us2 to separation conditions;(iv.2) removing the stream Sv2 from the separation unit Us2, the stream Sv2 exhibiting a total concentration cv2(X) of one or more compounds X, a concentration cv2(C) of monomeric E- caprolactam, a concentration cv2(W) of water and a concentration cv2(G) of the at least one inert gas G, with cv2(W) < Cvi(W);(iv.3) removing the stream SL2 from the separation unit Us2, the stream SL2 exhibiting a total concentration CL2(X) of one or more compounds X, a concentration CL2(C) of monomeric E- caprolactam and a concentration CL2(W) of water, with CL2(X) > Cv2(X), CL2(C) > Cv2(C), and CL2(W) < CV2(W). The process of embodiment 1, wherein TLO is in the range of from 75 to 120 °C, preferably in the range of from 80 to 110 °C, more preferably in the range of from 85 to 100 °C. The process of embodiment 1 or 2, wherein CLO(C) + CLO(X) is in the range of from 60 to 95 weight-%, preferably in the range of from 70 to 90 weight-%, more preferably in the range of from 80 to 85 weight-%, based on the weight of the stream SLO.The process of any one of embodiments 1 to 3, wherein in the stream SLO, the weight ratio of the one or more compounds X to monomeric E-caprolactam is in the range of from 50:50 to 5:95. The process of any one of embodiments 1 to 4, wherein the one or more compounds X comprised in the stream SLO comprise at least one of at least one aromatic amine which includes at least one of an aromatic monoamine, an aromatic diamine, an aromatic triamine and an aromatic tetramine; at least one aliphatic amine which includes at least one of an aliphatic monoamine, an aliphatic diamine and an aliphatic triamine; at least one aliphatic amide; at least one aromatic alcohol which includes at least one of an aromatic monool and an aromatic diol; at least one aliphatic alcohol which includes at least one of an aliphatic monool and an aliphatic diol; at least one aromatic acid; at least one and aliphatic acid; at least one E-caprolactam oligomer; at least other compound selected from the group consisting of one or more cleavage products of dyes such as optionally chlorinated aromatic diamines, one or more water-soluble oligomeric cellulose cleavage products, and one or more water-soluble oligomers of terephthalic acid and hexamethylenediamine. The process of embodiment 5, wherein the at least one aromatic amine includes one or more of 4, 4'-methylenedianil ine (MDA), isomers thereof such as 2,4’-methylenedianiline and 2,2’-methylenedianiline, and polymethylen polyphenylen polyamines (pMDA); the at least one aliphatic amine and the at least one aliphatic amide include one or more of hexamethylenediamine adipate, 6-aminocaproic acid and oligomers thereof, including 6-aminocaproic acid dimer and higher oligomers such as 6-aminocaproic acid trimer, 6-aminocaproic acid tetramer, 6- aminocaproic acid pentamer, 6-aminocaproic acid hexamer, N'-(6-aminohexyl)hexane-1,6-diamine, N- methyl-hexane-1,6-diamine, 6-aminohexanamide, derivatives of E-caprolactam other than E-caprolactam oligomers and having a boiling point higher than E-caprolactam such as 1-(6- aminohexyl)azepan-2-one; the at least one aliphatic alcohol includes one or more of butanediol and oligomers thereof, including butanediol dimer and higher oligomers such as butanediol trimer, including polytetrahydrofuran; the at least one aromatic acid and the at least one aliphatic acid include one or more of terephthalic acid and adipic acid; the at least one E-caprolactam oligomer includes one or more of E-caprolactam dimer E-caprolactam trimer, E-caprolactam tetramer, E-caprolactam pentamer, andE-caprolactam hexamer.7. The process of any one of embodiments 1 to 6, wherein CLO(W) is in the range of from 5 to 40 weight-%, preferably in the range of from 10 to 30 weight-%, more preferably in the range of from 15 to 20 weight-%, based on the weight of the stream SLO.8. The process of any one of embodiments 1 to 7, wherein from 95 to 100 weight-%, preferably from 98 to 100 weight-%, more preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, more preferably from 99.9 to 100 weight-% of SLO consist of the one or more compounds X, monomeric E- caprolactam, and water.9. The process of any one of embodiments 1 to 8, wherein the at least one inert gas G comprises one or more of nitrogen and carbon dioxide, preferably nitrogen, wherein more preferably, at least 99 weight-%, more preferably at least 99.5 weight-%, more preferably at least 99.9 volume -% of the at least one inter gas G consist of nitrogen, wherein preferably from 95 to 100 weight-%, more preferably from 98 to 100 weight-%, more preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, more preferably from 99.8 to 100 weight-%, more preferably from 99.9 to 100 weight-% of the non-aqueous stripping gas stream SGO consist of the at least one inert gas G.10. The process of any one of embodiments 1 to 9, wherein TGO is at least 250 °C, preferably in the range of from 250 to 500 °C, more preferably in the range of from 300 to 450 °C.11. The process of any one of embodiments 1 to 10, wherein according to (ill.1), the stream SLO is passed into the stripping unit Usi at a mass flow rate PLO and the stream SGO is passed into the stripping unit Usi at a mass flow rate PGO, wherein PLO I PGO is in the range of from 0.15:1 to 0.4:1, preferably in the range of from 0.15:1 to 0.3:1, more preferably in the range of from 0.15:1 to 0.25:1.12. The process of any one of embodiments 1 to 11, wherein the stream SLO which is passed into the stripping unit Usi according to (iii.1) exhibits a pressure in the range of from 1 to 4 bar, preferably in the range of from 1 to 3 bar, more preferably in the range of from 1 to 2 bar.13. The process of any one of embodiments 1 to 12, wherein the stream SGO which is passed into the stripping unit Usi according to (iii.1) exhibits a pressure in the range of from 1 to 4 bar, preferably in the range of from 1 to 3 bar, more preferably in the range of from 1 to 2 bar.14. The process of any one of embodiments 1 to 13, wherein in the stripping unit Usi, the stream SLO and the stream SGO are brought into contact in counter-current mode or in co-current mode, preferably in countercurrent mode.15. The process of any one of embodiments 1 to 14, wherein the stripping unit Usi comprises one or more of a tray column, a packed column, a spray column, a bubble column and a centrifugal contactor, wherein more preferably, the stripping unit Usi comprises a spray column.16. The process of any one of embodiments 1 to 15, wherein TLI is in the range of from 230 to 300 °C, preferably in the range of from 250 to 300 °C, more preferably in the range of from 250 to 280 °C.17. The process of any one of embodiments 1 to 16, wherein CLI(X) + CLI(C) is in the range of from 95 to 100 weight-%, preferably in the range of from 98 to 100 weight-%, more preferably in the range of from 99 to 100 weight-%, based on the weight of the stream SLI .18. The process of any one of embodiments 1 to 17, wherein in the stream SLI, the weight ratio of the one or more compounds X to monomeric E-caprolactam is at least 10:1, preferably at least 20:1, more preferably at least 40:1.19. The process of any one of embodiments 1 to 18, exhibiting a high boiler separation efficiency Q(X) of at least 95 %, preferably at least 97 %, more preferably at least 99 %, with Q(X) = |JLI(X) I PLO(X), wherein |JLO(X) is the mass flow rate of the at least one compound X in the stream SLO, expressed in kg / h, and |JLI (X) is the mass flow rate of the at least one compound X in the stream SLI, expressed in kg / h.20. The process of any one of embodiments 1 to 19, wherein Tvi is in the range of from 200 to 270 °C, preferably in the range of from 230 to 270 °C, more preferably in the range of from 250 to 270 °C.21 . The process of any one of embodiments 1 to 20, wherein the stream Svi exhibits a pressure pvi, wherein pvi is in the range of from 1 to 4 bar, preferably in the range of from 1 to 3 bar, more preferably in the range of from 1 to 2 bar.22. The process of any one of embodiments 1 to 21 , wherein cvi(C) + Cvi(W) + Cvi(G) is in the range of from 98 to 100 weight-%, more preferably in the range of from 99 to 100 weight-%, more preferably in the range of from 99.8 to 100 weight-%, based on the weight of the stream Svi.23. The process of any one of embodiments 1 to 22, wherein in the stream Svi, the weight ratio of the one or more compounds X to monomeric E-caprolactam is at most 1 :50, preferably at most 1 :65, more preferably at most 1 :100.24. The process of any one of embodiments 1 to 23, wherein the separation unit Us2 according to (iv) is a partial condensation unit, preferably comprising one or more of a plate heat exchanger and a tube shell heat exchanger.The process of any one of embodiments 1 to 24, wherein the separation unit Us2 according to (iv) is a scrubbing unit, the producing in the scrubbing unit Us2 from the stream Svi an aqueous gas stream Sv2 and a liquid stream SL2 comprising(iv.1 ) passing the stream Svi removed from the stripping unit Usi into the scrubbing unit Us2 and subjecting the stream Svi in the unit Us2 to scrubbing conditions;(iv.2) removing the stream Sv2 from the scrubbing unit Us2, the stream Sv2 having a temperature Tv2 with Tv2 < Tvi and exhibiting a total concentration cv2(X) of one or more compounds X, a concentration cv2(C) of monomeric E-caprolactam, a concentration cv2(W) of water and a concentration cv2(G) of the at least one inert gas G, with cv2(W) < Cvi(W);(iv.3) removing the stream SL2 from the scrubbing unit Us2, the stream SL2 having a temperature TL2 with Tv2 < TL2 < Tvi and exhibiting a total concentration CL2(X) of one or more compounds X, a concentration MO) of monomeric E-caprolactam and a concentration CL2(W) of water, with CL2(X) > Cv2(X), Ci_2(C) > Cv2(C), and cL2(W) < W);(iv.4) dividing the stream SL2 in at least a stream Si_2i having a temperature TL2I with TL2I = TL2 and a stream SL22 having a temperature TL22 with TL22 = M; subjecting the stream Si_2i to cooling, obtaining a cooled stream Si_2ic having a temperature TL2IC < L21; and feeding the stream Si_2ic back into the scrubbing unit Us2, wherein the scrubbing conditions according to (iv.1 ) comprise bringing the gas stream Svi into contact with the liquid stream Si_2ic. The process of embodiment 25, wherein the scrubbing unit Us2 comprises a packed column. The process of embodiment 25 or 26, wherein TL2 is in the range of from 85 to 110 °C, preferably in the range of from 85 to 100 °C, more preferably in the range of from 85 to 95 °C. The process of any one of embodiments 25 to 27, wherein X) + Ci_2(C) + W) is in the range of from 95 to 100 weight-%, preferably in the range of from 98 to 100 weight-%, more preferably in the range of from 99 to 100 weight-%, based on the weight of the stream SL2. The process of any one of embodiments 25 to 28, wherein in the stream Si_2, the weight ratio of the one or more compounds X to monomeric E-caprolactam is at most 1 :50, preferably at most 1 :65, more preferably at most 1 :100. The process of any one of embodiments 25 to 29, wherein in the stream Si_2, the weight ratio of the one or more compounds X to water is at least 0.01 :1 , preferably at least 1 :1 , more preferably at least 10:1. The process of any one of embodiments 25 to 30, wherein Tv2 is in the range of from 85 to 105 °C, preferably in the range of from 90 to 100 °C, more preferably in the range of from 95 to 100 °C.32. The process of any one of embodiments 25 to 31 , wherein the stream Sv2 exhibits a pressure pv2, wherein pv2 is in the range of from 1 to 4 bar, preferably in the range of from 1 to 3 bar, more preferably in the range of from 1 to 2 bar.33. The process of any one of embodiments 25 to 32, wherein cv2(C) + cv2(W) + cv2(G) is in the range of from 98 to 100 weight-%, preferably in the range of from 99 to 100 weight-%, more preferably in the range of from 99.5 to 100 weight-%, based on the weight of the stream Sv2.34. The process of any one of embodiments 25 to 33, wherein in the stream Sv2, the weight ratio of monomeric E- caprolactam to water is at most 1 :1 , preferably at most 1 :2, more preferably at most 1 :3.35. The process of any one of embodiments 25 to 34, wherein TL2C is in the range of from 75 to 95 °C, preferably in the range of from 75 to 90 °C, more preferably in the range of from 75 to 85 °C.36. The process of any one of embodiments 25 to 35, wherein according to (iv.1 ), the stream Svi is passed into the scrubbing unit Us2 at a mass flow rate pvi and the stream Si_2i c is passed the scrubbing unit Us2 at a mass flow rate |JL2IC, wherein pvi I PL2IC is in the range of from 0.2: 1 to 0.5:1 , preferably in the range of from 0.2: 1 to 0.4:1 , more preferably in the range of from 0.2: 1 to 0.3:1.37. The process of any one of embodiments 25 to 36, wherein in the scrubbing unit Us2, the stream Svi and the stream Si_2ic are brought into contact in counter-current mode or in co-current mode or in cross-flow mode, preferably in counter-current mode.38. The process of any one of embodiments 25 to 37, exhibiting an E-caprolactam separation efficiency Q(C) of at least 94 %, preferably at least 96 %, more preferably at least 98 %, with Q(C) = pi_22(C) I PLO(C), wherein PLO(C) is the mass flow rate of E-caprolactam in the stream SLO, expressed in kg / h, and pi_22(C) is the mass flow rate of E-caprolactam in the stream Si_22, expressed in kg / h.39. The process of any one of embodiments 1 to 38, wherein providing the stream SLO according to (I) comprises, and / or wherein the stream SLO is obtainable or obtained by a method comprising(1.1) providing a stream SM comprising a solid material M comprising polyamide 6;(1.2) preparing an aqueous depolymerization mixture based on SM;(1.3) subjecting the depolymerization mixture prepared according to (1.2) to polyamide 6 depolymerization conditions in a reaction unit UR, obtaining a liquid aqueous stream S comprising E-caprolactam dissolved in water at a concentration CSR, the stream SR further comprising one or more impurities;(1.4) preferably passing the liquid aqueous stream SR into an evaporation unit UE, obtaining from S a liquid aqueous stream SL comprising E-caprolactam dissolved in water at a concentration CSL with CSL > CSR, and further obtaining from SR one or more aqueous vapor streams Sv;(1.5) passing the aqueous stream SR, preferably the aqueous stream SL, into a heat-consuming purification unit URI, obtaining from SR, preferably from SL, the stream SLO and further obtaining from SR, preferably from SL, one or more aqueous streams SRW, wherein at least part of the heat consumed in URI is preferably provided by at least one of the one or more streams Sv, thereby obtaining from the at least one stream Sv at least one at least partially condensed aqueous stream Svw;(1.6) preferably recycling at least one stream Svw at least partially to the reaction unit UR and at least one stream SRW at least partially to the reaction unit UR; wherein the solid material M preferably comprises, more preferably consists of, waste material, wherein said waste material more preferably comprises, more preferably consists of, one or more of at least one textile waste material and at least one engineering plastics waste material, more preferably comprises, more preferably consists of at least one textile waste material; wherein 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 the solid material M consist of the polyamide; wherein preferably, in addition to polyamide 6, the solid material M comprises one or more further organic polymeric compounds, more preferably including, but not limited to, one or more of at least one elastane; at least one polyamide 6.6; at least one polyethylene terephthalate; at least one polyurethane; at least one polyester; at least one polyether; at least one polyvinyl chloride; at least one natural fiber material such as wool and cotton; at least one cellulose material; at least one natural elastomer; at least one synthetic elastomer; at least one copolymer of two or more of said polymeric compounds including statistical copolymers, gradient copolymers, alternating copolymers, block copolymers, and graft copolymers; and at least one rubber material comprising one or more of at least one natural rubber material and at least one synthetic rubber material. The process of any one of embodiments 1 to 39, further comprising(v) producing in a separation unit Us3 from the stream Sv2 a gas stream Sv3 and an aqueous liquid stream SL3, comprising(v.1) passing the stream Sv2 removed from the separation unit Us2 into the separation unit Us3 and subjecting the stream Sv2 in the unit Us3 to separation conditions;(v.2) removing the stream Sv3 from the separation unit Us3, the stream Sv3 exhibiting a concentration MG) of the at least one inert gas G and a concentration cvs(W) of water, with cvs(W) < cv2(W) and CV3(G) > G);(v.3) removing the stream SL3 from the separation unit Us3, the stream SL3 exhibiting a concentration cL3(W) of water and a concentration G) of the at least one inert gas G, with W) > MW) and MG) < cv3(G).41 . The process of embodiment 40, wherein the separation unit Us3 is a partial condensation unit, preferably comprising one or more of a plate heat exchanger and a tube shell heat exchanger.42. The process of embodiment 40 or 41 , wherein the separation unit Us3 is a scrubbing unit, the producing in the scrubbing unit Us3 from the stream Sv2 a gas stream Sv3 and an aqueous liquid stream S comprising(v.1) passing the stream Sv2 removed from the scrubbing unit Us2 into the scrubbing unit Us3 and subjecting the stream Sv2 in the unit Us3 to scrubbing conditions;(v.2) removing the stream Sv3 from the scrubbing unit Us3, the stream Sv3 having a temperature Tvs with Tvs < TV2 and exhibiting a concentration cvs(G) of the at least one inert gas G and a concentration cvs(W) of water, with cvs(W) < cv2(W) and cvs(G) > cv2(G);(v.3) removing the stream Su from the scrubbing unit Us3, the stream Su having a temperature T with Tvs < Tu < TV2 and exhibiting a concentration cu(W) of water and a concentration cvs(G) of the at least one inert gas G, with cu(W) > cvs(W) and cu(G) < Cvs(G).43. The process of embodiment 42, wherein the scrubbing unit Us3 comprises a packed column.44. The process of embodiment 42 or 43, wherein Tu is in the range of from 55 to 80 °C, preferably in the range of from 65 to 80 °C, more preferably in the range of from 75 to 80 °C.45. The process of any one of embodiments 42 to 44, wherein cu(W) + cu(G) is in the range of from 95 to 100 weight-%, preferably in the range of from 98 to 100 weight-%, more preferably in the range of from 99 to 100 weight-%, based on the weight of the stream Su.46. The process of any one of embodiments 42 to 45, wherein in the stream Si_3, the weight ratio of water to the at least one inert gas is at least 320: 1 , preferably at least 400: 1 , more preferably at least 500: 1 .47. The process of any one of embodiments 42 to 46, wherein Tvs is in the range of from 25 to 40 °C, preferably in the range of from 25 to 35 °C, more preferably in the range of from 25 to 30 °C.48. The process of any one of embodiments 42 to 47, wherein the stream Sv3 exhibits a pressure pv3, wherein pv3 is in the range of from 1 to 4 bar, preferably in the range of from 1 to 3 bar, more preferably in the range of from 1 to 2 bar.49. The process of any one of embodiments 42 to 48, wherein cvs(G) + cvs(W) is in the range of from 98 to 100 weight-%, more preferably in the range of from 99 to 100 weight-%, more preferably in the range of from 99.5 to 100 weight-%, based on the weight of the stream Sv3.The process of any one of embodiments 42 to 49, wherein in the stream Sv3, the weight ratio of the at least one inert gas to water is at least 31 :1 , preferably at least 35: 1 , more preferably at least 40: 1 . The process of any one of embodiments 42 to 50, further comprising(v.4) dividing the stream SL3 in at least a stream Si_3i having a temperature TLSI with TLSI = Tu and a stream SL32 having a temperature TL32 with TL32 = Ti_3i subjecting the stream Si_3i to cooling, obtaining a cooled stream Si_3ic having a temperature TLSIC < TLSI; and feeding the stream Si_3ic back into the scrubbing unit Us3, wherein the scrubbing conditions according to (v.1 ) comprise bringing the gas stream Sv2 into contact with the liquid stream Si_3ic. The process of embodiment 51 , wherein TLSI c is in the range of from 25 to 40 °C, preferably in the range of from 25 to 35 °C, more preferably in the range of from 25 to 30 °C. The process of embodiment 51 or 52, wherein according to (v.1), the stream Sv2 is passed into the scrubbing unit Us3 at a mass flow rate pv2 and the stream Si_3i c is passed the scrubbing unit Us3 at a mass flow rate PLSIC, wherein pv2 1 PLSIC is in the range of from 0.3: 1 to 0.6:1 , preferably in the range of from 0.4: 1 to 0.5:1 , more preferably in the range of from 0.45: 1 to 0.48: 1. The process of any one of embodiments 51 to 53, wherein in the scrubbing unit Us3, the stream Sv2 and the stream Si_3i c are brought into contact in counter-current mode or in co-current mode or in cross-flow mode, preferably in counter-current mode. The process of any one of embodiments 51 to 54, exhibiting a water separation efficiency Q(W) of at least 65 %, preferably at least 70 %, more preferably at least 75 %, with Q(W) = |JL32(W) I PLO(W), wherein PLO(W) is the mass flow rate of water in the stream SLO, expressed in kg / h, and pi_32(W) is the mass flow rate of water in the stream Si_32, expressed in kg / h. The process of any one of embodiments 40 to 55, further comprising(vi) passing the stream Sv3 having the temperature Tvs, or a part stream thereof, into the stripping unit Usi. The process of embodiment 56, wherein at least a part of the stream SGO provided according to (ii) and passed into the stripping unit Usi according to (ill.1) consists of the stream Sv3 or the part stream thereof. The process of embodiment 56 or 57, wherein prior to being passed into the stripping unit Usi , the stream Sv3 or the part stream thereof is passed through a heating unit UHI, the process comprising heating the stream Sv3 or the part stream thereof from the temperature Tvs to the temperature TGO.59. The process of embodiment 58, wherein the heating unit UHI comprises a heat exchange sub-unit UHEI, wherein the process comprises passing the stream Svi through UHEI and heating the stream Sv3 from the temperature Tv3 to a temperature T*v3 in UHEI with Tvs < T*v3 TGO, wherein at least a part of the heat for heating the stream Sv3 in UHEI to the temperature T*v3 is provided by the stream Svi.60. The process of embodiment 59, wherein T*v3 < TGO, the heating unit UHI further comprising a heating sub-unit UHSI arranged downstream of the heat exchange sub-unit UHEI, wherein the process comprises passing the stream Sv3 obtained from the heat exchange sub-unit UHEI and having the temperature T*v3 through the heating sub-unit UHSI and heating the stream Sv3 from the temperature T*v3 to the temperature TGO in UHSI.61 . The process of embodiment 59 or 60, wherein T*v3 is in the range of from 40 to 95 °C, preferably in the range of from 50 to 85 °C, more preferably in the range of from 65 to 75 °C.62. The process of any one of embodiments 1 to 56, or of any one of embodiments 24 to 56, further comprising (vii) passing the stream SL2 obtained according to (iv.3), or the stream Si_22 obtained according to (iv.4), into a purification unit UP, obtaining from SL2 or Si_22 a stream SCPL exhibiting a concentration CCPL(C) of monomeric E-caprolactam with CCPL(C) > CL22(C); wherein the purification unit UP comprises a distillation unit UDI, the process comprising feeding the stream SL2 or the stream Si_22 to UDI, obtaining from UDI a stream SDI exhibiting a concentration CDI(C) of monomeric E- caprolactam with CCPL(C) > CDI(C) > Ci_2(C) or CCPL(C) > CDI(C) > Ci_22(C), wherein the purification unit UP preferably further comprises, downstream of the unit UDI, one or more of a crystallization unit UCR and a chemical treatment unit UOD, the process comprising obtaining the stream SCPL from UCR or from UOD.63. The process of embodiment 62, wherein the purification unit UP further comprises a crystallization unit UCR located downstream of UDI, the process comprising feeding the stream SDI to the crystallization unit UCR, obtaining from UCR a stream SCR being the stream SCPL comprising E-caprolactam at a concentration CCR(C) = CCPL(C).64. The process of embodiment 62, wherein the purification unit UP further comprises a chemical treatment unit UOD located downstream of UDI, the process comprising feeding the stream SDI to the chemical treatment unit UOD, obtaining from UOD a stream SOD being the stream SCPL comprising E-caprolactam at a concentration COD(C) = CCPL(C).65. The process of embodiment 62, wherein the purification unit UP further comprises a chemical treatment unit UOD and a crystallization unit UCR, wherein the crystallization unit UCR is located downstream of the distillation unit UDI and the chemical treatment unit UOD is located downstream of the crystallization unit UCR, the process comprising feeding the stream SDI to the crystallization unit UCR, obtaining from the crystallization UCR astream SCR comprising E-caprolactam at a concentration CC (C) with CC (C) > CDI(C), and feeding the stream SC to the chemical treatment unit UOD, obtaining from UOD a stream SOD being the stream SCPL comprising E- caprolactam at a concentration COD(C) = CCPL(C).66. The process of embodiment 62, wherein the purification unit UP further comprises a chemical treatment unit UOD and a crystallization unit UCR, wherein the chemical treatment unit UOD is located downstream of the distillation unit UDI and the crystallization unit UCR is located downstream of the unit UOD the process comprising feeding the stream SDI to the chemical treatment unit UOD, obtaining from the chemical treatment unit UOD a stream SOD comprising E-caprolactam at a concentration COD(C) with COD(C) > CDI(C), and feeding the stream SOD to the crystallization unit UCR, obtaining from UCR a stream SCR being the stream SCPL comprising E-caprolactam at a concentration CCR(C) = CCPL(C).67. The process of any one of embodiments 62 to 66, wherein the chemical treatment in the unit UOD comprises(a) providing a preferably liquid stream SDI comprising E-caprolactam from the distillation unit UDI or a preferably liquid stream SCR comprising E-caprolactam from the crystallization unit UCR, said stream SDI or said stream SCR further comprising one or more oxidizable organic impurity compounds Y, wherein the stream SDI or the stream SCR exhibits a weight ratio rye of the one or more organic compounds Y relative to E-caprolactam;(b) providing a stream SPM comprising at least one permanganate;(c) preparing an oxidation reaction educt mixture MOE from the stream SDI and the stream SPM, or from the stream SCR and the stream SPM, and subjecting the mixture MOE to oxidation reaction conditions, obtaining an oxidation reaction product stream SP comprising E-caprolactam, further comprising one or more oxidation products Z obtained from the oxidation of at least a part of the one or more compounds Y, and optionally further comprising a part of the one or more organic compounds Y, wherein the stream SP exhibits a weight ratio ryep of organic compound Y relative to E-caprolactam with 0 < ryep < rye and further exhibits a weight ratio rzep of the one or more products Z relative to E-caprolactam with TZCP > 0;(d) separating at least a part of the one or more oxidation products Z and optionally at least a part of organic compound Y from the stream SP, obtaining the stream SOD; wherein the process optionally further comprises providing a stream SOH comprising at least one hydroxide, wherein the oxidation reaction educt mixture MOE according to (c) is prepared from the stream SOD or the stream SCR, and from the stream SPM and the stream SOH; wherein separating at least a part of the one or more oxidation products Z and optionally at least a part of organic compound Y from the stream SP according to (d) preferably comprises subjecting the stream SP obtained according to (c) to distillation in a distillation unit UDI, comprised in the chemical treatment unit UOD, obtaining from the distillation unit UDI a stream SDT comprising E-caprolactam as the stream SOD, wherein the unit UDI comprises one or more distillation columns, preferably one or two distillation columns, wherein at least one column is optionally configured as side stream column or as divided wall column.68. A stream SCPL comprising highly purified E-caprolactam, the stream SCPL being obtainable or obtained by a process according to any one of embodiments 62 to 67.69. Use of the stream SCPL according to embodiment 68 as an educt material for a chemical process, preferably for a polymerization reaction, more preferably for preparing polyamide 6.70. A method for preparing polyamide 6, comprising(A) preparing a stream SCPL according to a process according to any one of embodiments 62 to 67;(B) subjecting the stream SCPL, optionally after storing, to polyamide 6 polymerization conditions.71. Polyamide 6, obtainable or obtained by a method according to embodiment 70.72. The process of any one of embodiments 62 to 67, further comprising providing at least part of the stream SCPL to a polyamide 6 production unit UPP, wherein the polyamide 6 produced in UPP is preferably provided as a feedstock to a textile material producing unit UTP, from which unit UTP(A) a textile material MTE is obtained which is brought onto the market, wherein, after the lifetime TMTE of said textile material MTE, it is at least partially collected as textile waste material in a textile material collecting unit UTC;(B) remaining material MRE is obtained as textile waste material; wherein at least part of the textile waste material according to (A), or at least part of the textile waste material according to (B), or at least part of the textile waste material according to (A) and at least part of the textile waste material according to (B) is suitably provided as material M according to (1.1) as defined in embodiment 39.73. The process of any one of embodiments 62 to 67, further comprising providing at least part of the stream SCPL to a polyamide 6 production unit UPP, wherein the polyamide 6 produced in UPP is preferably provided as a feedstock to an engineering plastics material producing unit UEP, from which unit UEP(A) an engineering plastics material MEP is obtained which is brought onto the market, wherein, after the lifetime TMEP of said engineering plastics material MEP, it is at least partially collected as engineering plastics waste material in an engineering plastics material collecting unit UEC;(B) remaining material MRE is obtained as engineering plastics waste material; wherein at least part of the engineering plastics waste material according to (A), or at least part of the engineering plastics waste material according to (B), or at least part of the engineering plastics waste material according to (A) and at least part of the engineering plastics waste material according to (B) is suitably provided as material M according to (1.1) as defined in embodiment 39.74. Use of the stream SCPL according to embodiment 68 for preparing polyamide 6, said use preferably further comprising employing said polyamide 6 as a feedstock for preparing one or more of a textile material and an engineering plastics material, more preferably for preparing a textile material.75. A method for preparing polyamide 6, said method comprising employing the stream SCPL according to embodiment 68 as a starting material, wherein said method preferably further comprises employing said polyamide 6 as a feedstock for preparing one or more of a textile material and an engineering plastics material, more preferably for preparing a textile material.76. A process, preferably according to any one of embodiments 1 to 67, comprising the step of converting the stream SLI obtainable or obtained by the process according to any one of embodiments 1 to 67 and / or the stream SCPL obtainable or obtained by the process according to any one of embodiments 62 to 67 and / or a chemical material obtainable or obtained by the process according to any one of embodiments 1 to 67 to obtain a product Q.77. The process of embodiment 76, wherein the product Q is selected from: building block or monomer; or polymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; or cleaning polymer, cleaning surfactant, descaling compound, cleaning biocide or composition or formulation thereof; or agrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; or active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, human food additive, dietary supplements, aroma chemical or aroma composition; or aqueous polymer dispersion, preferably polyurethane or polyurethane - poly(meth)acrylate hybrid polymer dispersion, emulsion, binder for paper and fiber coatings, UV-curable acrylic polymer for hot melts and coatings polyisocyanates, hyperbranched polyester polyol, polymeric dispersant for inorganic binder compositions, unsaturated polyester polyol or 100% curable composition; or cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or composition or formulation thereof; or polymer B, polymer composition B, coating composition, other functional composition, foil, molded body, coating or coated substrate.78. The process of embodiment 76 or 77, wherein the content of SLI and / or SCPL and / or the chemical material in the product Q is 1 weight-% or more, preferably 2 weight-% or more, more preferably 5 weight-% or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight-% ormore, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and / or wherein the content of SLI and / or SCPL and / or the chemical material in the product Q is 100 weight-% or less, preferably 95 weight-% or less, more preferably 90 weight-% or less, more preferably 50 weight-% or less, more preferably 25 weight-% or less, more preferably 10 weight-% or less; and preferably wherein the content is determined based on identity preservation and / or segregation and / or mass balance and / or book and claim chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard.The term „bar" as used in the context of the present invention refers to the absolute pressure, also referred to as „bar(abs)“ or as "bara”.The term "textile material” as used herein 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” as used herein 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.The term "engineering plastics” as used herein refers to high-performance plastics grades which possess physical properties enabling them to perform for prolonged use in structural applications, over a wide temperature range, under mechanical stress, and in difficult chemical and physical environments used for example to fabricate plastic parts replacing traditional engineering materials like metals and ceramics. Engineering plastics specifically apply in the fabrication of mechanical parts across several industries such as automotive, medical, electrical and electronics, aerospace, construction and consumer products. The term "engineering plastics waste material” as used herein covers an engineering plastics 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.The present invention is further illustrated by the Figures 1 to 6 as described hereinbelow.Short description of the FiguresFigure 1 shows a process according to present invention. According to this process, an aqueous liquid stream SLO comprising monomeric E-caprolactam and one or more organic compounds X is passed into a stripping unit Usi, together with a non-aqueous stripping gas stream SGO comorising at least one inert gas G. In the stripping unit Usi,the stream SLO and the stream SGO are brought into contact with each other at stripping conditions. At these stripping conditions, the one or more one organic compounds X comprised in the stream SLO have a boiling point TBX and the monomeric E-caprolactam has a boiling point TBC with TBX > TBC. By said stripping in Usi, an aqueous gas stream Svi and a liquid stream SLI, are obtained, and removed from Usi ■ The stream SLI exhibits a total concentration CLI(X) of one or more compounds X and a concentration CLI(C) of monomeric E-caprolactam with CLI(X) > Cvi(X) and CLI(C) < Cvi(C), whereas the stream Svi exhibits a total concentration cvi(X) of one or more compounds X, a concentration Cvi(C) of monomeric E-caprolactam, a concentration Cvi(W) of water and a concentration Cvi(G) of the at least one inert gas G, with cvi(C) > CLO(C) and cvi(X) < CLO(X). The stream Svi is then passed to a separation unit Us2 where it is subjected to separation conditions allowing for producing an aqueous gas stream Sv2 and a liquid stream SL2, wherein the stream SL2 exhibits a total concentration CL2(X) of one or more compounds X, a concentration CL2(C) of monomeric E-caprolactam and a concentration CL2(W) of water, with CL2(X) > Cv2(X), CL2(C) > Cv2(C), and CL2(W) < Cv2(W), and the stream Sv2 exhibits a total concentration cv2(X) of one or more compounds X, a concentration cv2(C) of monomeric E-caprolactam, a concentration cv2(W) of water and a concentration cv2(G) of the at least one inert gas G, with cv2(W) < Cvi(W). Thus, in the unit Usi, the main separation task is the separation of the one or more organic compounds X from monomeric E-caprolactam, and the main separation task in the downstream unit Us2 is the separation of water from monomeric E-caprolactam.Figure 2 shows a process according to present invention. Further according to the process as shown in Figure 1, the Figure 2 illustrates an especially design separation stage carried out in Us2 according to which the separation unit Us2 is configured as a scrubbing unit. According to this process, the stream SL2 having a temperature TL2 obtained from the scrubber Us2 is divided into a stream SL2I having a temperature TL2I with TL2I = TL2 and a stream SL22 having a temperature L22 with L22 = TL2. This stream SL21 is subjected to cooling in a cooling unit Uc2 from which a cooled stream SL2IC is obtained which has a temperature TL2IC < L21. This cooled stream SL2IC is then sent back into the scrubbing unit Us2.Figure 3 shows a process according to present invention. Further according to the processes as shown in Figure 1 and Figure 2, the Figure 3 illustrates a preferred way how the feed stream SLO passed into the stripping unit is provided. According this preferred process, a stream SM is provided which comprises a solid material M comprising polyamide 6, wherein the solid material M preferably comprises, more preferably consists of, waste material, wherein said waste material more preferably comprises, more preferably consists of, one or more of at least one textile waste material and at least one engineering plastics waste material, more preferably comprises, more preferably consists of at least one textile waste material. Based on the stream SM, an aqueous depolymerization mixture is suitably prepared (not shown) and subjected to polyamide 6 depolymerization conditions in a reaction unit UR, from which a liquid aqueous stream S is obtained which comprises monomeric E-caprolactam dissolved in water at a concentration CSR, Further, the stream SR comprises one or more impurities which are either already contained in SM and / or formed from impurities in SM at the depolymerization conditions in UR. Typically, these impurities contain one or more of the organic compounds X comprised in the stream SLO. According to the present invention, it may be preferred that downstream of UR, the liquid aqueous stream SR is passed into an evaporation unit UE from which aliquid aqueous stream SL is obtained which comprises monomeric E-caprolactam dissolved in water at a concentration CSL with CSL > CSR. Further from SR in UE, one or more aqueous vapor streams Sv are obtained which may serve as suitable heat source for one or more process stages in the overall process as described herein. The aqueous stream SL is then passed into a heat-consuming purification unit URI from which the stream SLO is obtained which is passed as feed stream into the stripping unit Usi ■Figure 4 shows a process according to present invention. Further according to the processes as shown in Figure 1, Figure 2 and Figure 3, the Figure 4 illustrates a preferred way how the stream Sv2 obtained from the separation unit Us2, preferably the scrubbing unit Us2, is further treated. According this preferred process, the aqueous gas stream Sv2 is passed to a separation unit Us3 where it is subjected to separation conditions allowing for producing a gas stream Sv3 and an aqueous liquid stream SL3, wherein the stream Sv3 exhibits a concentration cvs(G) of the at least one inert gas G and a concentration cvs(W) of water, with cvs(W) < cv2(W) and cvs(G) > Cv2(G), and wherein the stream SL3 exhibits a concentration CL3(W) of water and a concentration cvs(G) of the at least one inert gas G, with cL3(W) > cv3(W) and CL3(G) < Cvs(G). Preferably, the separation unit Us3 is configured as a scrubbing unit, and the stream SL3 having a temperature TL3 obtained from the scrubber Us3 is divided into a stream SLSI having a temperature TLSI with TLSI = TL3 and a stream SL32 having a temperature TL32 with TL32 = TL3. This stream SLSI is subjected to cooling in a cooling unit Uc3 from which a cooled stream SLSIC is obtained which has a temperature TLSIC < TL2I . This cooled stream SLSIC is then sent back into the scrubbing unit Us3. Thus, in the unit Us3, the main separation task is the separation of the at least one inert gas from water.Figure 5 shows a process according to present invention. Further according to the processes as shown in Figure 4, the Figure 5 illustrates a preferred way how the stream Sv3 is re-used in the process, in particular including a heatintegrating way of re-using the stream Sv3. According to this preferred process, the stream Sv3 having the temperature Tvs, is passed back into the stripping unit Usi, and it is especially preferred that at least a part of the stream SGO consists of the stream Sv3. Further preferably, as shown in Figure 5, the stream Sv3 is passed through a heating unit UHI in which it is heated from the temperature Tvs to the temperature TGO, in a heat exchange sub-unit UHEI. According to this process, the stream Svi is passed through said sub-unit UHEI and heats up the stream Sv3 from the temperature Tvs to a temperature T*v3 with Tvs < T*v3 TGO. Yet further preferably, also shown in Figure 5, in particular in case T*v3 < TGO, the heating unit UHI further comprises a heating sub-unit UHSI arranged downstream of the heat exchange sub-unit UHEI, wherein the stream Sv3 obtained from the heat exchange sub-unit UHEI is passed through UHSI in which it is heated from the temperature T*v3 to the temperature TGO.Figure 6 shows a process according to present invention. Further according to the processes as shown in Figure 5, the Figure 6 illustrates a preferred way how the stream SL22 comprising purified monomeric E-caprolactam is still further purified in process stages carried out in a purification unit UP located downstream of the first separation, preferably scrubbing unit Us2. According to this preferred process as shown in Figure 6, the stream SL22 is sent to said purification unit UP from which a stream SCPL is obtained as ultimately purified monomeric E-caprolactam stream which exhibits a concentration CCPL(C) of monomeric E-caorolactam with CCPL(C) > CL22(C). Preferably, as shown inFigure 6, the purification unit UP comprises a distillation unit UDI, and the stream Si_22 is first fed to UDI, obtaining from UDI a stream SDI (not shown) exhibiting a concentration CDI(C) of monomeric E-caprolactam with CCPL(C) > CDI(C) > CL22(C). Further preferably, also shown in Figure 6, the purification unit UP further comprises, downstream of the unit UDI, one or more of a crystallization unit UCR and a chemical treatment unit UOD, and the stream SCPL is obtained either from UCR or from UOD.Further, the Figure 6 shows a stream SGM which is suitably combined with the stream Sv3 obtained from Us3. While, for example at the start-up of the continuous process of the present invention, an external stream SGO, for example taken from a suitable grid, is passed into the stripping unit Usi, the stream SGO is provided during the process in the form of Sv3, as described above. In order to deal with any unavoidable losses during the process, a make-up gas stream SGM, for example taken from said grid, is passed into the process, preferably as shown in Figure 6, i.e. it is combined with the stream Sv3 before the (combined) stream is passed through the heating unit UHI as described.

Claims

Claims1 . A continuous process for separating one or more organic compounds X from an aqueous liquid stream SLO comprising monomeric E-caprolactam and said one or more compounds X, the process comprising(i) providing the stream SLO having a temperature TLO and exhibiting a total concentration CLO(X) of the one or more compounds X, a concentration CLO(C) of monomeric E-caprolactam, and a concentration CLO(W) of water;(ii) providing a non-aqueous stripping gas stream SGO comprising at least one inert gas G and having a temperature TGO with TGO > TLO;(ill) producing in a stripping unit Usi from the stream SLO an aqueous gas stream Svi and a liquid stream511, comprising(ill.1 ) passing the stream SLO and the stream SGO into the stripping unit Usi;(111.2) bringing the stream SLO and the stream SGO in the stripping unit Usi at stripping conditions into contact with each other, wherein the stripping conditions comprise a stripping pressure ps and wherein at the stripping pressure ps, the one or more one organic compounds X comprised in the stream SLO have a boiling point TBX and monomeric E-caprolactam has a boiling point TBC with TBX>T BC;(111.3) removing the stream Svi from the stripping unit Usi, the stream Svi having a temperature Tvi with TLO < Tvi < TGO and exhibiting a total concentration cvi(X) of one or more compounds X, a concentration cvi(C) of monomeric E-caprolactam, a concentration Cvi(W) of water and a concentration Cvi(G) of the at least one inert gas G, with cvi(C) > CLO(C) and cvi(X) < CLO(X);(111.4) removing the stream SLI from the stripping unit Usi, the stream SLI having a temperature TLI with TLO < TLI < TGO and exhibiting a total concentration CLI(X) of one or more compounds X and a concentration CLI(C) of monomeric E-caprolactam, with CLI(X) > Cvi(X) and CLI(C) < Cvi(C);(iv) producing in a separation unit Us2 from the stream Svi an aqueous gas stream Sv2 and a liquid stream512, comprising(iv.1 ) passing the stream Svi removed from the stripping unit Usi into the separation unit Us2 and subjecting the stream Svi in the unit Us2 to separation conditions;(iv.2) removing the stream Sv2 from the separation unit Us2, the stream Sv2 exhibiting a total concentration cv2(X) of one or more compounds X, a concentration cv2(C) of monomeric E- caprolactam, a concentration cv2(W) of water and a concentration cv2(G) of the at least one inert gas G, with cv2(W) < Cvi(W);(iv.3) removing the stream SL2 from the separation unit Us2, the stream SL2 exhibiting a total concentration CL2(X) of one or more compounds X, a concentration CL2(C) of monomeric E- caprolactam and a concentration CL2(W) of water, with CL2(X) > Cv2(X), CL2(C) > Cv2(C), and CL2(W) < CV2(W).

2. The process of claim 1 , wherein TLO is in the range of from 75 to 120 °C, preferably in the range of from 80 to 110 °C, more preferably in the range of from 85 to 100 °C, and wherein TGO is at least 250 °C, preferably in the range of from 250 to 500 °C, more preferably in the range of from 300 to 450 °C.

3. The process of claim 1 or 2, wherein according to (ill.1), the stream SLO is passed into the stripping unit Usi at a mass flow rate PLO and the stream SGO is passed into the stripping unit Usi at a mass flow rate PGO, wherein PLO / PGO is in the range of from 0.15: 1 to 0.4:1 , more preferably in the range of from 0.15:1 to 0.3:1 , more preferably in the range of from 0.15:1 to 0.25:1.

4. The process of any one of claims 1 to 3, wherein from 95 to 100 weight-%, preferably from 98 to 100 weight- %, more preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, more preferably from 99.9 to 100 weight-% of SLO consist of the one or more compounds X, monomeric E-caprolactam, and water.

5. The process of any one of claims 1 to 4, wherein the at least one inert gas G comprises one or more of nitrogen and carbon dioxide, preferably nitrogen, wherein more preferably, at least 99 weight-%, more preferably at least 99.5 weight-%, more preferably at least 99.9 volume -% of the at least one inter gas G consist of nitrogen, wherein more preferably from 95 to 100 weight-%, more preferably from 99 to 100 weight- %, more preferably from 99.9 to 100 weight-% of the non-aqueous stripping gas stream SGO consist of the at least one inert gas G.

6. The process of any one of claims 1 to 5, exhibiting a high boiler separation efficiency Q(X) of at least 95 %, preferably at least 97 %, more preferably at least 99 %, with Q(X) = |JLI(X) I PLO(X), wherein PLO(X) is the mass flow rate of the at least one compound X in the stream SLO, expressed in kg / h, and PLI(X) is the mass flow rate of the at least one compound X in the stream SLI , expressed in kg / h.

7. The process of any one of claims 1 to 6, wherein the separation unit Us2 according to (iv) is a scrubbing unit, the producing in the scrubbing unit Us2 from the stream Svi an aqueous gas stream Sv2 and a liquid stream SL2 comprising(iv.1 ) passing the stream Svi removed from the stripping unit Usi into the scrubbing unit Us2 and subjecting the stream Svi in the unit Us2 to scrubbing conditions;(iv.2) removing the stream Sv2 from the scrubbing unit Us2, the stream Sv2 having a temperature Tv2 with Tv2 < Tvi and exhibiting a total concentration cv2(X) of one or more compounds X, a concentration cv2(C) of monomeric E-caprolactam, a concentration cv2(W) of water and a concentration cv2(G) of the at least one inert gas G, with cv2(W) < Cvi(W);(iv.3) removing the stream SL2 from the scrubbing unit Us2, the stream SL2 having a temperature TL2 with Tv2 < TL2 < Tvi and exhibiting a total concentration CL2(X) of one or more compounds X, a concentrationcL2(C) of monomeric E-caprolactam and a concentration CL2(W) of water, with CL2(X) > Cv2(X), CL2(C) > CV2(C), and cL2(W) < W);(iv.4) dividing the stream SL2 in at least a stream Si_2i having a temperature TL2I with TL2I = TL2 and a stream SL22 having a temperature TL22 with TL22 = M; subjecting the stream Si_2i to cooling, obtaining a cooled stream Si_2ic having a temperature TL2IC < L21; and feeding the stream Si_2ic back into the scrubbing unit Us2, wherein the scrubbing conditions according to (iv.1 ) comprise bringing the gas stream Svi into contact with the liquid stream Si_2ic.

8. The process of any one of claims 1 to 7, further comprising(v) producing in a separation unit Us3 from the stream Sv2 a gas stream Sv3 and an aqueous liquid stream SL3, comprising(v.1) passing the stream Sv2 removed from the separation unit Us2 into the separation unit Us3 and subjecting the stream Sv2 in the unit Us3 to separation conditions;(v.2) removing the stream Sv3 from the separation unit Us3, the stream Sv3 exhibiting a concentration CV3(G) of the at least one inert gas G and a concentration W) of water, with MW) < MW) and MG) > MG);(v.3) removing the stream SL3 from the separation unit Us3, the stream SL3 exhibiting a concentration cL3(W) of water and a concentration MG) of the at least one inert gas G, with W) > MW) and G) < MG); wherein the separation unit Us3 is preferably a scrubbing unit, the producing in the scrubbing unit Us3 from the stream Sv2 a gas stream Sv3 and an aqueous liquid stream SL3 comprising(v.1) passing the stream Sv2 removed from the separation unit Us2 into the scrubbing unit Us3 and subjecting the stream Sv2 in the unit Us3 to scrubbing conditions;(v.2) removing the stream Sv3 from the scrubbing unit Us3, the stream Sv3 having a temperature M with M < M and exhibiting a concentration MG) of the at least one inert gas G and a concentration MW) of water, with MW) < MW) and MG) > MG);(v.3) removing the stream SL3 from the scrubbing unit Us3, the stream SL3 having a temperature Tu with M < M < TV2 and exhibiting a concentration MW) of water and a concentration MG) of the at least one inert gas G, with MW) > MW) and MG) < MG); the process preferably further comprising(v.4) dividing the stream SL3 in at least a stream Si_3i having a temperature TLSI with TLSI = M and a stream SL32 having a temperature T1.32 with TL32 = M; subjecting the stream Si_3i to cooling, obtaining a cooled stream Si_3ic having a temperature TLSIC < TLSI; and feeding the stream Si_3ic back into the scrubbing unit Us3, wherein the scrubbing conditions according to (v.1 ) comprise bringing the gas stream Sv2 into contact with the liquid stream Si_3ic.

9. The process of claim 8, exhibiting a water separation efficiency Q(W) of at least 65 %, preferably at least 70 %, more preferably at least 75 %, with Q(W) = pi 3?fW) I ULO(W), wherein LO(W) is the mass flow rate of waterin the stream SLO, expressed in kg / h, and pi_32(W) is the mass flow rate of water in the stream SL32, expressed in kg / h.

10. The process of claim 8 or 9, further comprising(vi) passing the stream Sv3 having the temperature Tvs, or a part stream thereof, into the stripping unit Usi; preferably wherein at least a part of the stream SGO provided according to (ii) and passed into the stripping unit Usi according to (ill.1 ) consists of the stream Sv3 or the part stream thereof.

11. The process of claim 10, wherein prior to being passed into the stripping unit Usi, the stream Sv3 or the part stream thereof is passed through a heating unit UHI, the process comprising heating the stream Sv3 or the part stream thereof from the temperature Tvs to the temperature TGO, wherein the heating unit UHI preferably comprises a heat exchange sub-unit UHEI, wherein the process preferably comprises passing the stream Svi through UHEI and heating the stream Sv3 from the temperature Tvs to a temperature T*v3 in UHEI with Tvs < T*V3 TGO, at least a part of the heat for heating the stream Sv3 in UHEI to the temperature T*v3 being provided by the stream Svi.

12. The process of claim 11 , wherein T*v3 < T GO, the heating unit UHI further comprising a heating sub-unit UHSI arranged downstream of the heat exchange sub-unit UHEI , wherein the process comprises passing the stream Sv3 obtained from the heat exchange sub-unit UHEI and having the temperature T*v3 through the heating subunit UHSI and heating the stream Sv3 from the temperature T*v3 to the temperature TGO in UHSI.

13. The process of any one of claims 1 to 12, further comprising(vii) passing the stream SL2 obtained according to (iv.3), or the stream Si_22 obtained according to (iv.4) as defined in claim 7, into a purification unit UP, obtaining from SL2 or Si_22 a stream SCPL exhibiting a concentration CCPL(C) of monomeric E-caprolactam with CCPL(C) > CL22(C); wherein the purification unit UP comprises a distillation unit UDI, the process comprising feeding the stream SL2 or the stream Si_22 to UDI, obtaining from UDI a stream SDI exhibiting a concentration CDI(C) of monomeric E- caprolactam with CCPL(C) > CDI(C) > Ci_2(C) or CCPL(C) > CDI(C) > Ci_22(C), wherein the purification unit UP preferably further comprises, downstream of the unit UDI, one or more of a crystallization unit UCR and a chemical treatment unit UOD, the process comprising obtaining the stream SCPL from UCR or from UOD.

14. The process of any one of claims 1 to 13, wherein providing the stream SLO according to (i) comprises, and / or wherein the stream SLO is obtainable or obtained by a method comprising(1.1) providing a stream SM comprising a solid material M comprising polyamide 6;(1.2) preparing an aqueous depolymerization mixture based on SM;(1.3) subjecting the depolymerization mixture prepared according to (i.2) to polyamide 6 depolymerization conditions in a reaction unit UR, obtaining a liquid aqueous stream S comprising E-caprolactam dissolved in water at a concentration CSR, the stream SR further comprising one or more impurities;(1.4) preferably passing the liquid aqueous stream SR into an evaporation unit UE, obtaining from SR a liquid aqueous stream SL comprising E-caprolactam dissolved in water at a concentration CSL with CSL > CSR, and further obtaining from SR one or more aqueous vapor streams Sv;(1.5) passing the aqueous stream SR, preferably the aqueous stream SL, into a heat-consuming purification unit URI, obtaining from SR, preferably from SL, the stream SLO and further obtaining from SR, preferably from SL, one or more aqueous streams SRW, wherein at least part of the heat consumed in URI is preferably provided by at least one of the one or more streams Sv, thereby obtaining from the at least one stream Sv at least one at least partially condensed aqueous stream Svw;(1.6) preferably recycling at least one stream Svw at least partially to the reaction unit UR and at least one stream SRW at least partially to the reaction unit UR; wherein the solid material M preferably comprises, more preferably consists of, waste material, wherein said waste material more preferably comprises, more preferably consists of, one or more of at least one textile waste material and at least one engineering plastics waste material, more preferably comprises, more preferably consists of at least one textile waste material.

15. A process, preferably according to any one of claims 1 to 14, comprising the step of converting the stream SLI obtainable or obtained by the process according to any one of claims 1 to 14 and / or the stream SCPL obtainable or obtained by the process according to claim 14 and / or a chemical material obtainable by or obtained by the process according to any one of claims 1 to 14 to obtain a product Q.

Images