Process for hydrolytic depolymerization of polyamides

Abstract

A process for hydrolytic depolymerization of polyamide 6 contained in a solid material M, the process comprising providing the solid material M; melting the solid material M in a melting unit UM, thereby obtaining a liquid stream SM having a temperature TSM at a pressure pSM; providing a liquid aqueous stream SW having a temperature TSW at a pressure pSW; mixing the stream SM with the stream SW in a pre-reaction unit UPR, thereby obtaining a liquid reaction feed stream SF having a temperature TSF at a pressure pSF; feeding the stream SF into a chemical reaction unit UR; subjecting the stream SF to polyamide 6 depolymerization conditions comprising a polyamide 6 depolymerization temperature TD at a polyamide 6 depolymerization pressure pD in the reaction unit UR, thereby obtaining in the UR an aqueous depolymerization mixture comprising epsilon-caprolactam dissolved in water; removing an aqueous liquid reactor outlet stream SR from the UR, the stream SR comprising epsilon-caprolactam dissolved in water; wherein 0.8 < = TSF / TD < = 1.05 and 0.9 < = pSF / pD < = 1.05.

Description

[0001] The present invention relates to a method for hydrolyzing and depolymerizing a polyamide prepared from ε-caprolactam and an apparatus for performing the method for hydrolyzing and depolymerizing a polyamide prepared from ε-caprolactam, preferably for performing the above-described method.

[0002] Polyamides, and especially those of the formula (-NH-(CH2)5-CO-) n Polyamide 6, as characterized, is found in many materials, such as packaging, engineering plastics from automobiles, and textile filaments. The latter accounts for approximately 40% of the global polyamide 6 market. Currently, only a very small percentage of textile filaments are recycled, yet this accounts for a large percentage of global CO2 emissions. Therefore, there is a need to recycle polyamide 6 from such materials. Methods for alkaline depolymerization of polyamides exist. Therefore, there is a need to provide improved methods for depolymerizing polyamides that can overcome these problems.

[0003] According to the present invention, it has been found that an efficient depolymerization reaction in which polyamide 6 is hydrolyzed can be achieved by implementing a specific sequence of melting and pre-reaction units upstream of the chemical reaction unit in which the actual depolymerization reaction occurs. Furthermore, it has been found that the method can be made even more efficient if a specific design of the chemical reaction unit is implemented. Based on this, and in combination with the specific sequence of upstream and, particularly downstream, stages of the chemical reaction unit that allows for water recycling and very efficient use of internal process heat, the present invention can provide an advantageous overall method for recycling materials containing polyamide 6.

[0004] Therefore, the present invention relates to a method for hydrolyzing polyamide 6 contained in a polypolymer solid material M, the method comprising:

[0005] (i) Provide the solid material M;

[0006] (ii) In the melting unit U M The general will melt the solid material M provided by (i) to obtain a solution under pressure p. SM Below has temperature T SM Liquid flow S M ;

[0007] (iii) Provided under pressure p SW Below has temperature T SW Liquid water flow S W ;

[0008] (iv) In the pre-reaction unit U PR The lieutenant general obtained the stream S according to (ii). M According to (iii), the stream S is provided W Mixing, thereby obtaining at pressure p SF Below has temperature TSF a liquid reaction feed stream S F ;

[0009] (v) feeding the stream S F obtained according to (iv) to a chemical reaction unit U R ;

[0010] (vi) subjecting the stream S R in the reaction unit U F to polyamide 6 depolymerization conditions comprising a polyamide 6 depolymerization temperature T D at a polyamide 6 depolymerization pressure p D , thereby obtaining in U R an aqueous depolymerization mixture comprising epsilon-caprolactam dissolved in water;

[0011] (vii) removing from U R an aqueous liquid reactor outlet stream S R comprising epsilon-caprolactam dissolved in water; R

[0012] wherein 0.8 ≤ T SF / T D ≤ 1.05 and 0.9 ≤ p SF / p D ≤ 1.05.

[0013] Preferably, according to the present application, no polyamide 6 depolymerization catalyst such as a mineral acid, such as one or more of hydrochloric acid, nitric acid, sulfuric acid and phosphoric acid, and / or a zinc salt such as zinc chloride, zinc acetate or zinc triflate is added for preparing the stream S F subjected to hydrolytic polyamide 6 depolymerization conditions according to (vi).

[0014] Preferably, 0.6 ≤ T SM / T SF ≤ 1.05 and 0.9 ≤ p SM / p SF ≤ 1.05. According to the present application, one or more of the following ranges can be preferred: 0.6 ≤ T SM / T SF ≤ 0.7; 0.7 ≤ T SM / T SF ≤ 0.8;

[0015] 0.8 ≤ T SM / T SF ≤ 0.9; 0.9 ≤ T SM / T SF ≤ 1.0; 1.0 ≤ T SM / T​SF ≤ 1.05.

[0016] Further preferably, 0.8 ≤ T SW / T SF ≤ 1.3 and 0.9 ≤ p SW / p SF ≤ 1.05. Further according to the present application, one or more of the following ranges can be preferred: 0.8 ≤ T SW / T SF ≤ 0.9;

[0017] 0.9 ≤ T SW / T SF ≤ 1.0; 1.0 ≤ T SW / T SF ≤ 1.1; 1.1 ≤ T SW / T SF ≤ 1.2; 1.2 ≤ T SW / T SF ≤ 1.3.

[0018] With regard to the pre-reaction unit U PR according to (iv), there is no specific restriction, provided that a liquid reaction feed stream S SF with a temperature T SF at a pressure p F can be obtained. Preferably, the pre-reaction unit U PR according to (iv) comprises, more preferably consists of, a mixing unit, wherein more preferably the mixing unit is a static mixing unit. As used herein, the term “static mixing unit” refers to an arrangement of mixing elements which are installed in a pipe or tube and which operate essentially without moving parts, preferably completely without moving parts. According to the present application, it can be preferred that the mixing unit is configured as a suitable pipe joint of a pipe for stream S M and a pipe for stream S W , wherein there are no specific mixing elements.

[0019] According to the present application, it is preferred that, according to (iv), S W and S M are mixed in U W in a mixing ratio (m P / kg) / (m PR / kg) in the range of 1 : 1 to 20 : 1, more preferably in the range of 2 : 1 to 15 : 1, more preferably in the range of 5 : 1 to 10 : 1, wherein m W is S WThe amount of water contained therein, and m P It is S M The amount of polyamide 6 contained therein. Preferred ranges are, for example, 5:1 to 6:1 or 6:1 to 7:1 or 7:1 to 8:1, 8:1 to 9:1 or 9:1 to 10:1.

[0020] Regarding the melting unit U according to (ii) M There are no specific restrictions, provided that it is possible to obtain pressure p. SM Below has temperature T SM Liquid flow S M Preferably, according to (ii) the melting unit U M Including a kneader or extruder, more preferably an extruder, wherein more preferably, according to (ii) the melting unit U M Composed of an extruder, wherein more preferably, the extruder is a single-screw extruder or a twin-screw extruder, more preferably a twin-screw extruder. More preferably, the material provided according to (i) and having a value lower than T... SM A solid material M is fed into the extruder at a temperature that melts therein while being conveyed through the extruder. Preferably, the temperature of the solid material fed into the extruder is in the range of 10 to 50°C, more preferably in the range of 15 to 40°C, and even more preferably in the range of 20 to 30°C. More preferably, the solid material is fed into the extruder at a pressure in the range of 0.75 to 5 bar, more preferably in the range of 0.85 to 3 bar, and even more preferably in the range of 0.95 to 1.5 bar. To melt the material M, the extruder is preferably equipped with a suitable heating device to heat the material M separately, wherein the liquid flow S exits the extruder. M With temperature T SM The suitable heating device can be arranged such that the extruder exhibits one or more heating zones. It is conceivable that the extruder has more than one feeding zone for feeding solid material M. Furthermore, according to the invention, the extruder can operate with either a short-feed or full-feed configuration.

[0021] Preferably, the melting unit U M The extruder is preferably equipped with a degassing system for removing one or more gases during the melting process within the extruder. While it is generally conceivable for an extruder to have more than one degassing zone, it is preferred to have only one. Preferably, the degassing zone is located directly before pressure buildup in the extruder's discharge zone. If the melting unit U M If the extruder is preferably equipped with a degassing system, then the method preferably includes, during the melting process according to (ii), extracting gas from U... M Middle removed gas flow S GMPreferably, the gas flow S GM Under pressure p GM Below has temperature T GM Where 0.95 ≤ T GM / T SM ≤1.05, preferably 0.95 ≤ T GM / T SM ≤ 1.0. Preferably, according to the present invention, the melt from unit U... M The obtained stream S GM In the washing unit U S The gas stream S is subjected to washing, preferably wet washing and dry washing, more preferably wet washing, wherein the wet washing preferably includes the process of passing a gas stream S through a gas stream S. GM The material is introduced into a washing tower, preferably a filled washing tower. Before undergoing washing, it is preferable to allow the material to pass through the molten unit U... M The obtained stream S GM The fluid is cooled, preferably in a vacuum system, through which the flow S is preferably cooled. GM From the melting unit U M Move out of the middle.

[0022] According to the present invention, flow S M With pressure p SM The pressure p SM Preferably in the range 0.9 ≤ p SM / p SF Within ≤1.05, and where p SF In the range 0.9 ≤ p SF / p D ≤ 1.05. As discussed below, the depolymerization pressure p of polyamide 6... D Preferably, the pressure is in the range of 40 to 140 bar. Therefore, according to the present invention, a pressure p is preferred. SM Higher than, and more preferably significantly higher than, solid material M fed into the melting unit U M The pressure at which the feed is introduced into the extruder is moderately, preferably, moderate. According to the invention, it is conceivable that this pressure increase is achieved within the extruder itself. However, it is particularly preferred that, in order to achieve said pressure increase, it is achieved by including the feed into the melting unit U... M This is achieved using a suitable compression device, such as a compression device arranged downstream of the extruder. According to this preferred arrangement, it is preferable that the liquid flow leaving the extruder is at substantially the same pressure as the solid material fed into the extruder, wherein the liquid flow is then appropriately compressed in the compression device to produce a liquid at pressure p. SM Below has temperature T SM The flow S MPreferably, according to the invention, the compression device comprises at least one suitable gear pump, more preferably consisting of at least one suitable gear pump, wherein more than one gear pump is installed, preferably at least two gear pumps are arranged in series.

[0023] Further according to the invention, it is preferable that, according to (iv), the material leaving the melting unit U... M Liquid flow S M With liquid water flow S W Before mixing, allow the melt unit U to exit. M Liquid flow S M Passing through filter unit U F Preferably, in the melting unit U M Downstream and reaction unit U R Upstream, filter unit U is arranged F Preferred filter unit U F Used to draw liquid from S M The method involves separating particles with a particle size in the range of 100 to 500 micrometers, preferably in the range of 200 to 400 micrometers, wherein the method includes allowing the liquid stream S to flow before mixing according to (iv). M Passing through U F Furthermore, if the molten unit U M Including the compression device as described above, it is preferable to pass the liquid flow, preferably the liquid flow obtained from the extruder, through the filter device U before passing the compression device. F .

[0024] Further according to the present invention, it is possible that the melting unit U M It includes more than one melting device, preferably more than one extruder, wherein, for example, two or more extruders may be arranged in parallel.

[0025] Regarding the depolymerization conditions of polyamide 6 according to (vi), T is preferred. D Within the range of 230 to 330°C and p D Within the range of 40 to 140 bar, T is more preferred. D Within the range of 250 to 320°C and p D Within the range of 40 to 125 bar, T is more preferred. D Within the range of 270 to 310°C and p D The range is between 40 and 110 bar.

[0026] Therefore, T D The preferred range is, for example, 270 to 280°C, 280 to 290°C, 290 to 300°C, or 300 to 310°C, and p DThe preferred range is for example 40 to 55 bar or 55 to 70 bar or 70 to 85 bar or 85 to 100 bar or 100 to 110 bar.

[0027] According to the present application, the reaction unit U according to (v) R comprises at least one reactor in which a liquid stream S F is subjected to depolymerization conditions according to (vi). Preferably, the reaction unit U according to (v) R comprises z chemical reactors R i , i = 1...z, wherein z is in the range of 1 to 10, preferably in the range of 1 to 8, more preferably in the range of 1 to 6, more preferably in the range of 1 to 5, more preferably in the range of 1 to 4, more preferably in the range of 1 to 3. More preferably, the reaction unit U according to (v) R comprises 3 reactors R1, R2 and R3.

[0028] If the reaction unit U according to (v) R comprises more than one reactor R i , i.e. if z > 1, it is preferred that at least 2 reactors R i , preferably all z reactors R i are coupled in series, wherein

[0029] - according to (v), the stream S F is fed into R i , wherein i = 1;

[0030] - the aqueous liquid stream S i containing ε-caprolactam dissolved in water is removed from reactor R i and fed into reactor R i+1 , wherein i < z;

[0031] - according to (vii), the aqueous liquid stream S z containing ε-caprolactam dissolved in water is removed as stream S R from reactor R z ;

[0032] wherein in each reactor R i , the depolymerization temperature T Di is maintained at a depolymerization pressure p Di , wherein independently from each other, T Di is in the range of 230 to 330 °C and p Di is in the range of 40 to 140 bar, preferably wherein T Di is in the range of 250 to 320 °C and p Diin the range of 40 to 125 bar, more preferably wherein T Di in the range of 270 to 310 °C and p Di in the range of 40 to 110 bar. With regard to the preferred arrangement of the three reactors R1, R2 and R3, it is preferred that these three reactors are coupled in series, wherein

[0033] - according to (v), the stream S F is fed to R1 ;

[0034] - the aqueous liquid stream S1 containing ε-caprolactam dissolved in water is removed from reactor R1 and fed to reactor R2;

[0035] - the aqueous liquid stream S2 containing ε-caprolactam dissolved in water is removed from reactor R2 and fed to reactor R3;

[0036] - according to (vii), the aqueous liquid stream S3 containing ε-caprolactam dissolved in water is removed from reactor R3 as stream S R ;

[0037] wherein in reactor R1, the depolymerization temperature T D1 is maintained at a depolymerization pressure p D1 , wherein T D1 is in the range of 230 to 330 °C and p D1 is in the range of 40 to 140 bar, preferably wherein T D1 is in the range of 250 to 320 °C and p D1 is in the range of 40 to 125 bar, more preferably wherein T D1 is in the range of 270 to 310 °C and p D1 is in the range of 40 to 110 bar; wherein T D1 is preferably in the range of e.g. 270 to 280 °C or 280 to 290 °C or 290 to 300 °C or 300 to 310 °C and p D1 is preferably in the range of e.g. 40 to 55 bar or 55 to 70 bar or 70 to 85 bar or 85 to 100 bar or 100 to 110 bar;

[0038] wherein in reactor R2, the depolymerization temperature T D2 is maintained at a depolymerization pressure p D2 , wherein T D2 is in the range of 230 to 330 °C and p D2 is in the range of 40 to 140 bar, preferably wherein T D2 is in the range of 250 to 320 °C and p D2 is in the range of 40 to 125 bar, more preferably wherein T D2Within the range of 270 to 310°C and p D2 Within the range of 40 to 110 bar; where T D2 The preferred range is, for example, 270 to 280°C, 280 to 290°C, 290 to 300°C, or 300 to 310°C, and p D2 The preferred range is, for example, 40 to 55 bar, 55 to 70 bar, 70 to 85 bar, 85 to 100 bar, or 100 to 110 bar;

[0039] In reactor R3, at depolymerization pressure p D3 Maintain depolymerization temperature T D3 T D3 Within the range of 230 to 330°C and p D3 Within the range of 40 to 140 bar, preferably where T D3 Within the range of 250 to 320°C and p D3 In the range of 40 to 125 bar, more preferably, T D3 Within the range of 270 to 310°C and p D3 Within the range of 40 to 110 bar; where T D3 The preferred range is, for example, 270 to 280°C, 280 to 290°C, 290 to 300°C, or 300 to 310°C, and p D3 The preferred range is, for example, 40 to 55 bar, 55 to 70 bar, 70 to 85 bar, 85 to 100 bar, or 100 to 110 bar.

[0040] According to the present invention, preferably, for z > 1, z reactors R i Arranged vertically, with R1 being the topmost reactor and R... z It is the bottom reactor, from which R i S obtained i Transferred to R by gravity, preferably solely by gravity. i+1 Regarding the preferred arrangement of the three reactors R1, R2, and R3, it is preferred that the reactors R1, R2, and R3 are arranged vertically, with R1 being the topmost reactor and R3 being the bottommost reactor, wherein S1 obtained from R1 is transferred to R2 by gravity, preferably only by gravity, and wherein S2 obtained from R2 is transferred to R3 by gravity, preferably only by gravity.

[0041] Regarding one or more reactors R i The specific design preferably includes at least one reactor R. iis a stirred tank reactor, and more preferably all z reactors are stirred tank reactors. With regard to the preferred arrangement of the three reactors R1, R2 and R3, it is preferred that the reactors R1, R2 and R3 are stirred tank reactors.

[0042] While there are no general limitations with regard to the specific design of the stirred tank reactors, it is in particular preferred according to the present application that at least one stirred tank reactor R i , preferably each stirred tank reactor R i , independently from each other, preferably has 2 to 6 compartments, more preferably 2 to 5 compartments, more preferably 2 to 4 compartments, which are preferably arranged in series, more preferably in series and vertically, wherein 2 adjacent compartments are separated by a partition comprising at least one flow-through opening. Preferably, the at least one compartment comprised in the reactor R i comprises at least one stirrer, wherein more preferably each compartment of each reactor R i comprises at least one stirrer, wherein more preferably each compartment of each reactor R i comprises one stirrer, wherein the process comprises stirring the depolymerization mixture in a given compartment for at least a portion of the time during which the compartment is subjected to depolymerization conditions. With regard to the preferred arrangement of the three reactors R1, R2 and R3, it is more preferred that the stirred tank reactor R1 has 3 compartments arranged vertically and in series, wherein each compartment comprises a stirrer, the stirred tank reactor R2 has 3 compartments arranged vertically and in series, wherein each compartment comprises a stirrer, and the stirred tank reactor R3 has 3 compartments arranged vertically and in series, wherein each compartment comprises a stirrer. Reference is in particular made to the preferred arrangement of the three reactors R1, R2 and R3 as described above and the respective description. Figure 5

[0043] Alternatively, with regard to the specific design of the stirred tank reactors, it is in particular preferred according to the present application that at least one stirred tank reactor R i , preferably each stirred tank reactor R i , independently from each other, preferably has 2 to 6 compartments, more preferably 2 to 5 compartments, more preferably 2 to 4 compartments, which are preferably arranged in series, more preferably in series and vertically, wherein the reactor R i ​comprises at least one stirrer, and wherein 2 adjacent compartments are formed and separated by one or more suitable components of said stirrer, such as blades comprised in the stirrer, wherein the process comprises stirring the depolymerization mixture in a given compartment for at least a part of the time during which the depolymerization mixture is subjected to the depolymerization conditions in the reactor compartment. In this respect, and further with regard to the preferred arrangement of three reactors R1, R2 and R3, it is more preferred that the stirred tank reactor R1 has 2 vertically and serially arranged compartments which are formed and separated by said suitable components of the stirrer comprised in R1, that the stirred tank reactor R2 has 2 vertically and serially arranged compartments which are formed and separated by said suitable components of the stirrer comprised in R2, and that the stirred tank reactor R3 has 2 vertically and serially arranged compartments which are formed and separated by said suitable components of the stirrer comprised in R3.

[0044] Preferably according to the present application, the polyamide 6 depolymerization conditions according to (vi) further comprise that the aqueous depolymerization mixture has a total residence time t R in the unit U i , preferably in the z reactors R D , more preferably in the z stirred tank reactors, D wherein at least 85 wt-%, preferably at least 90 wt-%, more preferably at least 95 wt-% of the aqueous depolymerization mixture has a t i in the range of 30 to 90 min. The term “total residence time” as used in this context of the present application refers to the sum of the residence times in all chemical reactors R i . In particular, for z > 1, it is preferred that the residence time of the aqueous depolymerization mixture in the reactors R Di is t Di , and wherein 0.90 ≤ (t Di+1 / t Di ) ≤ 1.10, preferably 0.95 ≤ (t Di+1 / t D1 . Thus, according to the present application, it is preferred to achieve a narrow residence time distribution. With regard to the preferred arrangement of three reactors R1, R2 and R3, it is more preferred that the residence time of the aqueous depolymerization mixture in the reactor R1 is t D2 , the residence time of the aqueous depolymerization mixture in the reactor R2 is t D3 , and the residence time of the aqueous depolymerization mixture in the reactor R3 is t D1 , and wherein 0.90 ≤ (t D2 / t D1 ) ≤ 1.10, preferably 0.95 ≤ (t D2) ≤ 1.05, and where 0.90 ≤ (t D2 / t D3 ) ≤ 1.10, preferably 0.95 ≤ (t) D2 / t D3 ) ≤ 1.05.

[0045] Preferably, according to the present invention, reactor R i At least one of them, preferably all of the reactors R i Having one or more for the corresponding reactor R i The outlet device for removing the gas flow, i.e., used to make the corresponding reactor R i A degassing outlet device. Therefore, the method of the present invention preferably includes degassing from at least one reactor R. i The middle and preferred options are from all z reactors R i Remove the corresponding gas flow S Gi (at pressure p) Gi Below has temperature T Gi Given gas flow S Gi ), where 0.95 ≤ T Gi / T Di ≤ 1.05. Regarding the preferred arrangement of the three reactors R1, R2, and R3, the method more preferably includes removing the gas stream S from R1. G1 S G1 Under pressure p G1 Below has temperature T G1 Where 0.95 ≤ T G1 / T D1 ≤ 1.05, gas stream S removed from R2 G2 S G2 Under pressure p G2 Below has temperature T G2 Where 0.95 ≤ T G2 / T D2 ≤ 1.05, and the gas stream S removed from R3 G3 S G3 Under pressure p G3 Below has temperature T G3 Where 0.95 ≤ T G3 / T D3 ≤ 1.05. According to the present invention, it is preferable that the method further includes directing the gas stream S... Gi At least one of them, more preferably all streams S Gi More preferably, gas flow S G1 S G2 and S G3 With the gas flow S described above GM Combining, preferably in making the gas flow SGM are combined prior to being subjected to washing as described above.

[0046] Generally, there is no particular restriction as to how the solid material M is provided according to (i). Preferably, providing the solid material M according to (i) comprises

[0047] (i.1 ) providing the solid material M in a delivery unit U MD , wherein U MD preferably comprises one or more of at least one big bag station and at least one bulk container station;

[0048] (i.2) transferring the solid material M provided according to (i.1 ) from the unit U MD to a material collection unit U MC , preferably a collection drum, via a first connecting pipeline, wherein the first connecting pipeline preferably comprises one or more of at least one material receiving and discharge unit U MRD , at least one first material feeding unit U FMF and at least one first particle separation unit U FMPS .

[0049] (i.3) transferring the solid material M from the unit U MC to a unit U M via a second connecting pipeline, wherein the second connecting pipeline preferably comprises one or more of at least one second material feeding unit U SMF , at least one second particle separation unit U SMPS and at least one metal detector.

[0050] Preferably, the first connecting pipeline according to (i.2) comprises at least one unit U MRD , preferably at least one hopper, more preferably at least one single-zone hopper, and further comprises at least one unit U FMF , preferably at least one rotary feeder, and preferably further comprises at least a particle separation unit U FMPS , more preferably at least one filter, more preferably at least one screen filter.

[0051] Further preferably, for transferring the solid material M from the unit U MD to the unit U MC via the first connecting pipeline, at least one gas stream S G is passed through the first connecting pipeline, said at least one gas stream preferably comprising or more preferably consisting of air or lean air, wherein the at least one gas stream is preferably pre-treated by at least one of filtering, compressing and cooling, more preferably filtering, compressing and cooling, prior to passing through the first connecting pipeline.

[0052] Further preferably, the second connecting line according to (i.3) comprises at least two units U SMF , preferably a rotary feeder and a loss-in-weight feeder, wherein more preferably the rotary feeder is arranged upstream of the loss-in-weight feeder, and further comprising a unit U SMPS , preferably a vibrating screen.

[0053] Preferably according to (i), the solid material M is provided in the form of particles, preferably to U M , wherein the particle size distribution of said particles is preferably characterized by one or more, preferably by two or more, more preferably by three pairs of values:

[0054] - a D10 value of the particle width in the range of 0.3 to 15 mm and a D10 value of the particle length in the range of 0.3 to 15 mm;

[0055] - a D50 value of the particle width in the range of 0.5 to 20 mm and a D50 value of the particle length in the range of 0.5 to 20 mm;

[0056] - a D90 value of the particle width in the range of 0.8 to 30 mm and a D90 value of the particle length in the range of 0.8 to 30 mm.

[0057] More preferred pairs of values are for example:

[0058] - a D10 value of the particle width in the range of 2 to 4 mm and a D10 value of the particle length in the range of 3.5 to 5.5 mm;

[0059] - a D50 value of the particle width in the range of 2.5 to 4.5 mm and a D50 value of the particle length in the range of 4 to 7 mm;

[0060] - a D90 value of the particle width in the range of 3 to 5 mm and a D90 value of the particle length in the range of 4.5 to 8.5 mm.

[0061] The term“particle” as used in this context of the present application includes optionally preformed particles and also includes comminuted fragments.

[0062] Preferably, the solid material M provided according to (i) comprises polyamide 6, ranging from 10 to 100 wt%, more preferably 30 to 100 wt%, more preferably 50 to 100 wt%, more preferably 60 to 100 wt%, more preferably 70 to 100 wt%, and more preferably 80 to 100 wt%. If the polyamide 6 content of the solid material M is less than 100 wt%, it is preferable that the solid material M further comprises one or more elastic fibers. Typically, in addition to polyamide 6, solid material M may also contain at least one other polymer compound, wherein the at least one other polymer compound preferably contains one or more of the following: at least one polyamide 6.6; at least one semi-aromatic 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 the polymer compounds, including statistical copolymers, gradient copolymers, alternating copolymers, block copolymers and graft copolymers; and at least one rubber material, including one or more of at least one natural rubber material and at least one synthetic rubber material. Furthermore, in addition to polyamide 6, solid material M may further contain one or more of at least one pigment material and at least one glass fiber material.

[0063] Preferably, the solid material M provided according to (i) comprises, more preferably, one or more of the following: waste, more preferably textile waste and engineering plastic waste, more preferably textile waste. Generally, the solid material M provided according to (i) can be composed of a single material or several different materials, i.e., it is composed of w chemical materials M. j The composition, wherein j = 1..w and w ≥ 1. Further according to the invention, the preferred chemical material M... j At least one of the following, more preferably each chemical material M j The material contains waste, preferably composed of waste, and the waste preferably contains at least one type of textile waste, more preferably composed of at least one type of textile waste. If w > 1, the corresponding two or more materials can have different chemical compositions, which are not subject to any particular limitation, provided that the solid material M exhibits the composition discussed above.

[0064] According to the present invention, preferably 90 to 100 wt%, more preferably 91 to 100 wt%, more preferably 92 to 100 wt%, more preferably 93 to 100 wt%, more preferably 94 to 100 wt%, more preferably 95 to 100 wt%, of the liquid aqueous flow S provided according to (iii) is preferred. WComposed of water. A more preferred range may be 96 to 100 wt%, 97 to 100 wt%, 99 to 100 wt%, or 99 to 100 wt%.

[0065] Preferably, according to the present invention, according to (iii) providing a liquid aqueous flow S W Including the generation of stream S R The water contained in the water flow, and the water flow generated in the water flow as at least a portion of the water flow S. W Or as part of its feed back to the chemical reaction unit U R .

[0066] Regarding the recycling of the water, it is possible, for example, that the method includes optionally recycling the water from the chemical reaction unit U. R The obtained stream S R After being filtered, S R After undergoing hot water separation, a water-based flow S is obtained. X ; and the water flow S X At least a portion of it is used as a water-borne flow S W Part of the feed is returned to the chemical reaction unit U R The hot water separation preferably includes one or more of distillation and falling film evaporation. Preferably, an aqueous flow S is generated. X This may optionally include making the reaction unit U R The obtained stream S R S is distilled after filtration R Thus obtaining flow S X The distillation is preferably carried out in a distillation column at a bottom temperature preferably in the range of 70 to 140°C, more preferably in the range of 80 to 120°C, and even more preferably in the range of 90 to 110°C, and a top pressure preferably in the range of 0.5 to 1.5 bar, more preferably in the range of 0.7 to 1.2 bar, and even more preferably in the range of 0.8 to 1.1 bar, wherein the flow rate S X Obtained at the top of a distillation column. Further, the distillation may preferably include subjecting the top vapor stream to condensation to obtain a liquid stream S. X The liquid flow S X At least a portion of it is used as a water-borne flow S W Part of the feed is returned to the chemical reaction unit U R The liquid flow S obtained by condensation X It can be preferably divided into two flows, wherein the first flow obtained by splitting is taken as the water flow S. W Part of the feed is returned to the chemical reaction unit U RThe second stream is fed back to the top of the distillation column, wherein the volume ratio of the first stream to the second stream is preferably in the range of 10:1 to 0.5:1, more preferably in the range of 7:1 to 1:1, and even more preferably in the range of 5:1 to 2:1.

[0067] Regarding the recirculation of the water, according to the method of the invention, wherein according to (vii), the flow S R Includes concentration c SR ε-caprolactam dissolved in water, flow S R The method further includes one or more impurities, preferably including...

[0068] (viii) The liquid water flow S R Transferred to evaporation unit U E In, thus from S R Obtain the concentration c SL Liquid aqueous flow S of ε-caprolactam dissolved in water L , where c SL > c SR And further from S R Obtain one or more water vapor streams S V ;

[0069] (ix) will flow water S L Transferred to the heat-consuming purification unit U P In, thus from S L Obtain the concentration c SCPL The flow of ε-caprolactam S CPL , where c SCPL >> c SL And further from S L Obtain one or more water-borne flows S RW U P At least a portion of the heat consumed is generated by one or more streams S V At least one of them is provided, thereby from at least one stream S V Obtain at least one at least partially condensed aqueous flow S VW ;

[0070] (x) will have at least one stream S VW At least partially recycled to reaction unit U R And at least one stream S RW At least partially recycled to reaction unit U R .

[0071] The recycling of (x) preferably includes

[0072] (x.1) at least one stream SVW and at least one stream S RW is fed to a water treatment unit U W , thereby obtaining at least one aqueous recycle stream S W from U W .

[0073] (x.2) at least one aqueous stream S W is at least partially recycled to a reaction unit U R .

[0074] The water treatment unit U W preferably comprises a water recovery unit U WR and a wastewater unit U WW , wherein (x.1) preferably further comprises

[0075] (x.1.1) at least one stream S VW and at least one stream S RW is fed to a water recovery unit U WR , thereby obtaining at least one aqueous recycle stream S WR from U W and at least one aqueous stream S SW ;

[0076] (x.1.2) at least one stream S SW is fed to a wastewater unit U WW , thereby obtaining at least one wastewater stream S WW from U WW .

[0077] The purification unit U P preferably comprises one or more of a heat-consuming water separation unit U WS , a heat-consuming distillation unit U D and a heat-consuming crystallization unit U C , more preferably two or more of a heat-consuming water separation unit U WS , a heat-consuming distillation unit U D and a heat-consuming crystallization unit U C , more preferably all of a heat-consuming water separation unit U WS , a heat-consuming distillation unit U D and a heat-consuming crystallization unit U C , wherein at least a part of the heat consumed in one or more of U WS , U D and U C is provided by at least one of the one or more streams S V .

[0078] For such purification unit U PThe process preferably comprises one or more of (a-1), (a-2) and (a-3); more preferably at least two or more of (a-1), (a-2) and (a-3); more preferably (a-1), (a-2) and (a-3):

[0079] (a-1) obtaining at least one at least partially condensed aqueous stream S WS from U VW1 ;

[0080] (a-2) obtaining at least one at least partially condensed aqueous stream S D from U VW2 ;

[0081] (a-3) obtaining at least one at least partially condensed aqueous stream S C from U VW3 ;

[0082] wherein the process further comprises feeding one or more of S VW1 , S VW2 and S VW3 ; preferably two or more of S VW1 , S VW2 and S VW3 ; more preferably S VW1 , S VW2 and S VW3 to a water treatment unit U W as defined in embodiment 29.

[0083] Preferably, at least one of the streams S RW is obtained from U WS .

[0084] Preferably, the purification unit U P comprises a heat-consuming water separation unit U WS , a heat-consuming distillation unit U D and a heat-consuming crystallization unit U C , wherein the process comprises feeding a stream S SL comprising ε-caprolactam in a concentration c L to U WS , obtaining a stream U WS comprising ε-caprolactam in a concentration c UWS from U WS , feeding stream S UWS to a distillation unit U D , obtaining a stream S D comprising ε-caprolactam in a concentration c UD from U UD , and feeding stream S UD to a crystallization unit UC from U C containing ε-caprolactam in a concentration c SCPL , wherein CPL c

[0085] c SL < c UWS < c UD < c SCPL .

[0086] Preferably, the water separation unit U WS comprises at least two heat-consuming water separation sub-units U WS1 and U WS2 , more preferably two heat-consuming water separation sub-units U WS1 and U WS2 coupled in series, wherein stream S L is fed to U WS1 and wherein at least part of the heat consumed in one or more of U WS1 and U WS2 is preferably provided by at least one of the one or more streams S V .

[0087] For such a water separation unit U WS , the process preferably comprises one or more of (b-1) and (b-2), preferably (b-1) and (b-2):

[0088] (b-1) obtaining at least one at least partially condensed aqueous stream S WS1 from U VW11 ;

[0089] (b-2) obtaining at least one at least partially condensed aqueous stream S WS2 from U VW12 .

[0090] Further, for such a water separation unit U WS , it is preferred that at least one aqueous stream S RW1 is obtained from U WS1 and at least one aqueous stream S RW2 is obtained from U WS2 , and wherein at least one of S RW1 and S RW2 , preferably S RW1 and S RW2 , is fed to U W .

[0091] Still further, for such a water separation unit U WS , it is preferred that downstream of U WS1 and upstream of UWS2 Upstream, there is a separation unit U. I The method preferably includes extracting from U WS1 Obtaining water flow S UWS1 , will flow S UWS1 Feed to separation unit U I In the middle, from U I Obtaining water flow S UI and the flow S UI Feeding to unit U WS2 In, among them in U I In the process, one or more impurities are removed from S UWS1 Separate from U I Obtain impurity flow S I The impurities preferably contain S according to (vii). R It contains at least one impurity.

[0092] Preferably, the evaporation unit U E The method comprises two or more evaporation sub-units, wherein the method preferably includes obtaining at least two vapor streams S. V1 and S V2 , will the steam flow S V1 Transferred to at least one heat-consuming unit, and the steam flow S V 2 is transferred to at least one heat-consuming unit, wherein the steam flow S V1 and S V2 They differ from each other in terms of pressure and / or temperature.

[0093] Preferably, in U R Downstream, at least one solid-liquid separation unit is arranged, wherein a flow S is preferred. L and S R At least one of them passes through at least one solid-liquid separation unit before being passed to the next downstream unit.

[0094] According to the present invention, preferably, the solid material M provided according to (i) comprises, and preferably consists of, waste, preferably one or more of textile waste and engineering plastic waste, more preferably textile waste.

[0095] Regarding the above flow S CPL That is, purified ε-caprolactam stream, preferably the stream S CPL Transferred to polyamide 6 production unit U PP In this unit, the flow S CPL Used as starting material. One or more additional streams S can be added if needed. NCPL Additionally, it is transmitted to U. PP, which stream comprises non-recycled epsilon-caprolactam, i.e. epsilon-caprolactam from a conventional source. The correspondingly produced polyamide 6 material can then preferably be passed to unit U TP , in which unit the polyamide 6 material is used as starting material for producing a material comprising polyamide 6, preferably a textile material comprising polyamide 6. If desired, one or more further streams S NPA6 may be passed to U TP , which stream comprises non-recycled polyamide 6, i.e. polyamide 6 from a conventional source. Depending on the type of material produced in U TP , further streams comprising one or more starting materials other than polyamide 6 can also be passed to U TP . This material, preferably the textile material M TP obtained from U T then preferably goes onto the market and remains there for a given service life T MT . Thereafter, the corresponding scrap material is suitably collected in a collection unit U TC , preferably a textile material collection unit, from which collection unit the scrap material, optionally after sorting as described herein, is suitably passed as a solid material M or as a part of a solid material M to the process as described above.

[0096] According to the application, the process can therefore preferably further comprise the provision of a stream S CPL to a polyamide 6 production unit U PP , in which polyamide 6 produced in U PP is preferably provided as a raw material to a textile material production unit U TP , from which unit U TP

[0097] (A) obtaining a textile material M T , which, after a service life T T of said textile material M MT , is at least partially collected as textile waste in a textile material collection unit U TC ;

[0098] (B) obtaining a remaining material M R as textile waste;

[0099] wherein at least a part of the textile waste according to (A) or at least a part of the textile waste according to (B) or at least a part of the textile waste according to (A) and at least a part of the textile waste according to (B) is suitably provided via U M to U R .

[0100] ​The present application therefore also relates to a use of S CPL for the production of polyamide 6, which use preferably further comprises the use of the polyamide 6 as a raw material for the production of textile materials.

[0101] Further, the present application also relates to a method for the production of polyamide 6, which method comprises the use of S CPL as a starting material, wherein the method preferably further comprises the use of the polyamide 6 as a raw material for the production of textile materials.

[0102] Further, according to the present application, the method can preferably further comprise the provision of a stream S CPL to a polyamide 6 production unit U PP , wherein the polyamide 6 produced in U PP is preferably provided as a raw material to an engineering plastics material production unit U EP from which unit U EP ,

[0103] (A) obtaining a marketable engineering plastics material M E , wherein after a lifetime T E of said engineering plastics material M ME , it is at least partially collected as engineering plastics waste in an engineering plastics material collection unit U EC ;

[0104] (B) obtaining a remaining material M R as engineering plastics waste;

[0105] wherein at least a portion of the engineering plastics waste according to (A), or at least a portion of the engineering plastics waste according to (B), or at least a portion of the engineering plastics waste according to (A) and at least a portion of the engineering plastics waste according to (B) is provided as S M to U R , preferably via U M to U R .

[0106] The present application therefore also relates to a use of S CPL for the production of polyamide 6, which use preferably further comprises the use of the polyamide 6 as a raw material for the production of engineering plastics materials.

[0107] Further, the present application also relates to a method for the production of polyamide 6, which method comprises the use of S CPLAs a starting material, the method preferably further includes using the polyamide 6 as a raw material for preparing engineering plastic materials.

[0108] According to another aspect, the present invention relates to an integrated method for preparing polyamide 6, the method comprising:

[0109] (α) Prepare flow S according to the method described herein CPL The flow S CPL Contains purified ε-caprolactam;

[0110] (β) This stream S CPL Transferred to polyamide 6 production unit U PA ;

[0111] (γ) in U PA The middle makes this flow S CPL Subjected to ε-caprolactam polymerization conditions, thereby from U PA Obtaining polyamide 6 material M P And streams containing water and one or more ε-caprolactam oligomers;

[0112] (δ) Optionally, a stream containing water and one or more ε-caprolactam oligomers is subjected to concentration with respect to one or more ε-caprolactam oligomers in at least one concentration stage to obtain a concentrated stream containing water and one or more ε-caprolactam oligomers;

[0113] (ε) The optionally concentrated stream containing water and one or more ε-caprolactam oligomers is transferred to the melting unit U described herein. M and water ion unit U WS2 At least one of them.

[0114] Preferably, the optionally concentrated stream of (ε) comprising water and one or more ε-caprolactam oligomers further comprises ε-caprolactam, i.e., monomeric ε-caprolactam. More preferably, the integration method includes...

[0115] (γ) in U PA S CPL Subjected to ε-caprolactam polymerization conditions, thereby from U PA Obtaining polyamide 6 material M P He Liu S EW The S stream EW Contains concentration c EW (W) water, concentration c EW (C) ε-caprolactam and total concentration c EW One or more ε-caprolactam oligomers of (O);

[0116] (δ) makes the flow SEW Concentrated, including

[0117] (δ.1) Make the flow S EW First Concentration Unit U C1 It undergoes concentration, thus from U C1 Obtain concentrated stream S C1 The concentrated stream S C1 Contains concentration c C1 (W) water,

[0118] Concentration c C1 (C) ε-caprolactam and total concentration c C1 (O) one or more ε-caprolactam oligomers, wherein c C1 (W) < c EW (W), c C1 (C) > c EW (C), and

[0119] c C1 (O) > c EW (O), and further from U C1 Obtain the concentration c W1 (W) > c EW (W) water's water flow S W1 ;

[0120] (δ.2) Make the flow S C1 Second Concentration Unit U C2 It undergoes concentration, thus from U C2 Obtain concentrated stream S C2 The concentrated stream S C2 Including total concentration c C2 (O) one or more ε-caprolactam oligomers, wherein c C2 (O) > c C1 (O), and further from U C2 Obtaining water flow S W2 The water flow S W2 Contains concentration c W2 (W) water and

[0121] Concentration c W2 (C) ε-caprolactam, where c W2 (W) > c W1 (W) and c W2 (C) > c W1 (C);

[0122] (ε) will flow S C2 Passed to subunit U M And will flow S W2is passed to the subunit U WS2 .

[0123] As described above, the stream S PA obtained from the polyamide 6 polymerization unit U EW comprises water, monomeric ε-caprolactam and one or more ε-caprolactam oligomers. Typically, the aqueous stream S EW further comprises one or more additional organic compounds other than monomeric ε-caprolactam and one or more ε-caprolactam oligomers. It is therefore preferred that the stream S EW further comprises a total concentration c EW of one or more organic compounds X other than ε-caprolactam and its oligomers, according to (δ) a process comprising

[0124] (δ.1 ) subjecting the stream S EW to concentration in a first concentration unit U C1 , thereby obtaining a concentrated stream S C1 from U C1 , which concentrated stream S C1 comprises water in a concentration c C1 (W),

[0125] ε-caprolactam in a concentration c C1 (C), one or more ε-caprolactam oligomers in a total concentration c C1 (O) and one or more organic compounds X in a total concentration c C1 (X), wherein c C1 (W) < c EW (W), c C1 (C) > c EW (C), c C1 (O) > c EW (O) and c C1 (X) > c EW (X), and further obtaining from U C1 an aqueous stream S W1 comprising water in a concentration c EW (W) > c W1 (W) ;

[0126] (δ.2) subjecting the stream S C1 to concentration in a second concentration unit U C2 , thereby obtaining a concentrated stream S C2 from U C2 , which concentrated stream S C2 comprises one or more ε-caprolactam oligomers in a total concentration c C2 (O) and one or more organic compounds X in a total concentration c C2 (X), wherein cC2 (O) > c C1 (O) and c C2 (X) > c C1 (X), and further from U C2 an aqueous stream S W2 comprising water and epsilon-caprolactam in a concentration c W2 (W) and epsilon-caprolactam in a concentration c W2 (C) wherein c W2 (W) > c W2 (W) and c W1 (W) and c W2 (C) > c W1 (C).

[0127] More preferably, according to the present application, (γ) comprises

[0128] (γ.1) passing stream S CPL and preferably aqueous stream S AQ0 to a polymerization stage ST0, thereby obtaining from ST0 a crude polyamide 6 product stream S PA1 and an aqueous stream S WA1 ;

[0129] (γ.2) passing stream S PA1 and preferably aqueous stream S AQ1 to a granulation stage ST1, thereby obtaining from ST1 a crude granulated polyamide 6 material M PA2 and an aqueous stream S WA2 ;

[0130] (γ.3) passing material M PA2 and preferably aqueous stream S AQ2 to an extraction stage ST2, thereby obtaining from ST2 a purified granulated polyamide 6 material M PA3 and an aqueous stream S WA3 ;

[0131] (γ.4) passing material M PA3 to a drying stage ST3, thereby obtaining from ST3 a polyamide 6 material M P and an aqueous stream S WA4 .

[0132] In case some of the polyamide 6 material obtained from production unit U PA do not meet the specifications, the method can preferably further comprise passing at least some of said material M PR to unit U M .

[0133] The process of the application as described above can preferably be a continuous process. However, one or more process steps can be carried out in a batch type mode and one or more steps can be carried out in a semi-continuous mode.

[0134] The present application is further illustrated by the following groups of examples and combinations of examples resulting from the dependencies and cross-references as indicated. In particular, it should be noted that in each case where a series of examples is mentioned, for example in the context of the term "a process as described in any one of examples 1 to 4", each example of this series is intended to be explicitly disclosed to the skilled person, i.e. the wording of this term is to be understood by the skilled person as synonymous to "a process as described in any one of examples 1, 2, 3 and 4". Further, it should be explicitly noted that the following groups of examples represent appropriate structural parts of the general description for preferred aspects of the present application and thus appropriately support but do not represent the claims of the present application.

[0135] 1. A process for hydrolytic depolymerization of polyamide 6 comprised in a solid material M, the process comprising

[0136] (i) providing the solid material M;

[0137] (ii) melting the solid material M provided according to (i) in a melting unit U M , thereby obtaining a liquid stream S SM having a temperature T SM at a pressure p M ;

[0138] (iii) providing a liquid aqueous stream S SW having a temperature T SW at a pressure p W ;

[0139] (iv) mixing the stream S PR obtained according to (ii) with the stream S M provided according to (iii) in a pre-reaction unit U W , thereby obtaining a liquid reaction feed stream S SF having a temperature T SF at a pressure p F ;

[0140] (v) feeding the stream S F obtained according to (iv) to a chemical reaction unit U R ;

[0141] (vi) subjecting the stream S R to a polyamide 6 depolymerization temperature T D at a polyamide 6 depolymerization pressure p F in the reaction unit U D .D polyamide 6 under depolymerization conditions, thereby obtaining in U R an aqueous depolymerization mixture comprising epsilon-caprolactam dissolved in water;

[0142] (vii) removing the aqueous liquid reactor outlet stream S R from U R , which stream S R comprises epsilon-caprolactam dissolved in water;

[0143] wherein 0.8 < T SF / T D < 1.05 and 0.9 < p SF / p D < 1.05.

[0144] 2. The process according to embodiment 1, wherein 0.6 < T SM / T SF < 1.05 and 0.9 < p SM / p SF < 1.05.

[0145] 3. The process according to embodiment 1, wherein 0.8 < T SW / T SF < 1.3 and 0.9 < p SW / p SF < 1.05.

[0146] 4. The process according to any one of embodiments 1 to 3, wherein the pre- reaction unit U PR according to (iv) comprises, preferably consists of, a mixing unit, preferably a static mixing unit.

[0147] 5. The process according to any one of embodiments 1 to 4, wherein according to (iv), S W and S M are mixed in U W with a mixing ratio (m P / kg) / (m PR / kg) in the range of 1 : 1 to 20 : 1, preferably in the range of 2 : 1 to 15 : 1, more preferably in the range of 5 : 1 to 10 : 1, wherein m W is the amount of water comprised in S W and m P is the amount of polyamide 6 comprised in S M .

[0148] 6. The process according to any one of embodiments 1 to 5, wherein the melting unit UM It includes an extruder, preferably a single-screw extruder or a twin-screw extruder, and is preferably composed of an extruder, preferably a single-screw extruder or a twin-screw extruder.

[0149] 7. The method as described in any one of Examples 1 to 6, preferably as described in Example 6, wherein the melting unit U M Equipped with a degassing system, wherein the method includes, during the melting process according to (ii), removing gas from U M Middle removed gas flow S GM The gas flow S GM Under pressure p GM Below has temperature T GM Where 0.95 ≤ T GM / T SM ≤ 1.05.

[0150] 8. The method as described in Example 7, wherein the U M The gas stream S removed from the middle GM In the washing unit U S The gas stream S is subjected to washing, preferably wet washing and dry washing, more preferably wet washing, wherein the wet washing preferably includes the gas stream S being washed. GM It is transferred to the scrubbing tower, preferably filling the scrubbing tower.

[0151] 9. The method as described in any one of Examples 1 to 8, wherein in the melting unit U M The downstream and the reaction unit U R Upstream, filter unit U is arranged F Preferred filter unit U F For use from the liquid flow S M The method involves separating particles with a particle size in the range of 100 to 500 micrometers, preferably in the range of 200 to 400 micrometers, wherein the method includes allowing the liquid stream S to flow before mixing according to (iv). M Passing through U F .

[0152] 10. The method as described in any one of Examples 1 to 9, wherein according to (vi), T D Within the range of 230 to 330°C and p D Within the range of 40 to 140 bar, preferably where T D Within the range of 250 to 320°C and p D In the range of 40 to 125 bar, more preferably, T D Within the range of 270 to 310°C and p D The range is between 40 and 110 bar.

[0153] 11. The process according to any one of embodiments 1 to 10, wherein the reaction unit U according to (v) is R comprising z chemical reactors R i , i = 1...z, wherein z is in the range of 1 to 10, preferably in the range of 1 to 8, more preferably in the range of 1 to 6, more preferably in the range of 1 to 5, more preferably in the range of 1 to 4, more preferably in the range of 1 to 3.

[0154] 12. The process according to embodiment 11, wherein if z > 1, at least 2 reactors R i , preferably z reactors R i are coupled in series, wherein

[0155] - the stream S F is fed to R i according to (v), wherein i = 1;

[0156] - the aqueous liquid stream S i containing epsilon-caprolactam dissolved in water is removed from reactor R i and fed to reactor R i+1 , wherein i < z;

[0157] - the aqueous liquid stream S z containing epsilon-caprolactam dissolved in water is removed from reactor R R as stream S z according to (vii);

[0158] wherein in each reactor R i , the depolymerization temperature T Di is maintained at a depolymerization pressure p Di , wherein independently from each other, T Di is in the range of 230 to 330 °C and p Di is in the range of 40 to 140 bar, preferably wherein T Di is in the range of 250 to 320 °C and p Di is in the range of 40 to 125 bar, more preferably wherein T Di is in the range of 270 to 310 °C and p Di is in the range of 40 to 110 bar.

[0159] 13. The process according to embodiment 12, wherein for z > 1, the z reactors R i are arranged vertically, wherein R1 is the topmost reactor and R z is the bottommost reactor, wherein S i is obtained from R iby gravity, preferably only by gravity to R i+1 .

[0160] 14. The process of any one of embodiments 11 to 13, wherein at least 1, preferably z reactors R i are stirred tank reactors.

[0161] 15. The process of embodiment 14, wherein each stirred tank reactor R i has 2 to 6 compartments, preferably 2 to 5 compartments, more preferably 2 to 4 compartments, independently from each other, which compartments are preferably arranged in series, more preferably in series and vertically, wherein 2 adjacent compartments are separated by a partition comprising at least one flow-through opening.

[0162] 16. The process of embodiment 15, wherein the at least one compartment comprised in the reactor R i comprises at least one stirrer, wherein preferably each compartment of each reactor R i comprises at least one stirrer, wherein more preferably each compartment of each reactor R i comprises one stirrer, wherein the process comprises stirring the depolymerization mixture in a given compartment for at least a portion of the time during which said compartment is subjected to depolymerization conditions.

[0163] 17. The process of any one of embodiments 1 to 16, preferably of any one of embodiments 11 to 16, more preferably of embodiment 15 or 16, wherein the polyamide 6 depolymerization conditions according to (vi) further comprise a total residence time t R of the aqueous depolymerization mixture in the unit U i , preferably in the z reactors R D , more preferably in the z stirred tank reactors, wherein at least 85 wt-%, preferably at least 90 wt-%, more preferably at least 95 wt-% of the aqueous depolymerization mixture has a t D in the range of 30 to 90 min.

[0164] 18. The process of embodiment 17, with regard to any one of embodiments 11 to 16 according to which z > 1, preferably of embodiment 17 according to embodiment 15 or 16 according to which z > 1, wherein the residence time of the aqueous depolymerization mixture in the reactor R i is t Di , and wherein 0.90 < (t Di / t Di+1 ) < 1.10, preferably 0.95 < (t Di / t Di+1 ) < 1.05.

[0165] 19. The method as described in any one of Examples 11 to 18, the method comprising: from at least one reactor R i Preferred from all z reactors R i The corresponding gas flow S is removed from the middle. Gi (at pressure p) Gi Below has temperature T Gi Given gas flow S Gi ), where 0.95 ≤ T Gi / T Di ≤ 1.05.

[0166] 20. The method as described in Example 19, further comprising causing the gas flow S as defined in Example 7 to... GM Before undergoing the washing process as defined in Example 8, the gas stream S Gi At least one of them, preferably all of the streams S Gi With the gas flow S GM merge.

[0167] 21. The method as described in any one of Examples 1 to 20, wherein providing the solid material M according to (i) includes

[0168] (i.1) In delivery unit U MD The solid material M is provided in the middle, wherein U MD Preferably, it includes one or more of at least one bulk bag station and at least one bulk container station;

[0169] (i.2) The solid material M provided according to (i.1) is transferred from the unit U via the first connecting pipe. MD Transferred to material collection unit U MC A preferred collecting drum, wherein the first connecting pipeline preferably includes at least one material receiving and discharging unit U. MRD At least one first material feeding unit U FMF and at least one first particle separation unit U FMPS One or more of them;

[0170] (i.3) Remove the solid material M from the unit U MC Transmitted to unit U via the second connecting pipeline M The second connecting pipeline preferably includes at least one second material feeding unit U. SMF At least one second particle separation unit U SMPS and one or more of at least one metal detector.

[0171] 22. The method as described in embodiment 21, wherein the first connecting line according to (i.2) includes at least one unit U. MRD, preferably at least one hopper, more preferably at least one single-zone hopper, and further comprising at least one unit U FMF , preferably at least one rotary feeder, and preferably further comprising at least a particle separation unit U FMPS , more preferably at least one filter, more preferably at least one screen filter.

[0172] 23. The method of embodiment 21 or 22, wherein for transferring the solid material M from the unit U MD to the unit U MC at least one gas stream S G is passed through the first connection line, said at least one gas stream preferably comprising or more preferably consisting of air or lean air, wherein the at least one gas stream is preferably pretreated by at least one of filtering, compressing and cooling, more preferably by filtering, compressing and cooling, prior to passing through the first connection line.

[0173] 24. The method of any one of embodiments 21 to 23, wherein the second connection line according to (i.3) comprises at least two units U SMF , preferably a rotary feeder and a loss-in-weight feeder, wherein more preferably the rotary feeder is arranged upstream of the loss-in-weight feeder, and further comprising a unit U SMPS , preferably a vibrating screen.

[0174] 25. The method of any one of embodiments 1 to 24, wherein according to (i), the solid material M is provided in the form of particles, preferably to U M , wherein the particle size distribution of said particles is preferably characterized by one or more, preferably by two or more, more preferably by three pairs of values:

[0175] - a D10 value of the particle width in the range of 0.3 to 15 mm and a D10 value of the particle length in the range of 0.3 to 15 mm;

[0176] - a D50 value of the particle width in the range of 0.5 to 20 mm and a D50 value of the particle length in the range of 0.5 to 20 mm;

[0177] - a D90 value of the particle width in the range of 0.8 to 30 mm and a D90 value of the particle length in the range of 0.8 to 30 mm.

[0178] 26. The process of any one of embodiments 1 to 25, wherein 10 to 100 wt-%, more preferably 30 to 100 wt-%, more preferably 50 to 100 wt-%, more preferably 60 to 100 wt-%, more preferably 70 to 100 wt-%, more preferably 80 to 100 wt-% of the solid material M consists of polyamide 6.

[0179] 27. The process of any one of embodiments 1 to 26, wherein the liquid aqueous stream S is provided according to (iii) W comprising water contained in the stream S R , and at least a part of said produced aqueous stream is fed back to the chemical reaction unit U W or as a part thereof R .

[0180] 28. The process of any one of embodiments 1 to 27, wherein according to (vii), the stream S R comprises ε-caprolactam dissolved in water in a concentration c SR , the stream S R further comprises one or more impurities, the process further comprises

[0181] (viii) passing the liquid aqueous stream S R to an evaporation unit U E , thereby obtaining from S R a liquid aqueous stream S SL comprising ε-caprolactam dissolved in water in a concentration c L , wherein c SL > c SR , and further obtaining from S R one or more aqueous vapor streams S V ;

[0182] (ix) passing the aqueous stream S L to a heat-consuming purification unit U P , thereby obtaining from S L a stream S SCPL comprising ε-caprolactam in a concentration c CPL , wherein c SCPL >> c SL , and further obtaining from S L one or more aqueous streams S RW , wherein at least a part of the heat consumed in U P is provided by at least one of the one or more streams S V , thereby obtaining from the at least one stream S V at least one at least partially condensed aqueous stream S VW;

[0183] (x) recycling at least one stream S VW at least partially to the reaction unit U R and at least one stream S RW at least partially to the reaction unit U R .

[0184] 29. The method of embodiment 28, wherein the recycling according to (x) comprises

[0185] (x.1 ) feeding the at least one stream S VW and the at least one stream S RW to a water treatment unit U W , thereby obtaining at least one aqueous recycle stream S W from U W ;

[0186] (x.2) recycling at least one aqueous stream S W at least partially to the reaction unit U R .

[0187] 30. The method of embodiment 29, wherein the water treatment unit U W comprises a water recovery unit U WR and a wastewater unit U WW , wherein (x.1 ) further comprises

[0188] (x.1.1 ) feeding the at least one stream S VW and the at least one stream S RW to the water recovery unit U WR , thereby obtaining at least one aqueous recycle stream S WR and at least one aqueous stream S W from U SW ;

[0189] (x.1.2) feeding at least one stream S SW to the wastewater unit U WW , thereby obtaining at least one wastewater stream S WW from U WW .

[0190] 31. The method of any one of embodiments 28 to 30, wherein the purification unit U P comprises one or more of an energy intensive water separation unit U WS , an energy intensive distillation unit U D , and an energy intensive crystallization unit U C , preferably an energy intensive water separation unit U WS , an energy intensive distillation unit U Dand a heat-consuming crystallization unit U C , more preferably a heat-consuming water separation unit U WS , a heat-consuming distillation unit U D , and a heat-consuming crystallization unit U C , wherein U WS , U D , and U C one or more of the heat consumed in U V is provided by at least one of the streams S WS .

[0191] 32. The method according to embodiment 31, comprising one or more of (i-1), (i-2), and (i-3); preferably at least two or more of (i-1), (i-2), and (i-3); more preferably (i-1), (i-2), and (i-3):

[0192] (i-1) obtaining at least one at least partially condensed aqueous stream S WS from U VW1 ;

[0193] (i-2) obtaining at least one at least partially condensed aqueous stream S D from U VW2 ;

[0194] (i-3) obtaining at least one at least partially condensed aqueous stream S C from U VW3 ;

[0195] The method further comprises feeding one or more S VW1 , S VW2 , and S VW3 ; preferably two or more S VW1 , S VW2 , and S VW3 ; more preferably S VW1 , S VW2 , and S VW3 to a water treatment unit U W as defined in embodiment 29.

[0196] 33. The method according to embodiment 31 or 32, wherein at least one of the streams S RW is obtained from U WS .

[0197] 34. The method according to any one of embodiments 28 to 33, wherein the purification unit U P comprises a heat-consuming water separation unit U WS , a heat-consuming distillation unit U D , and a heat-consuming crystallization unit UC The process comprises feeding the stream S SL comprising epsilon-caprolactam in a concentration c L to a U WS , obtaining from U WS a stream U UWS comprising epsilon-caprolactam in a concentration c WS , feeding the stream S UWS to the distillation unit U D , obtaining from U D a stream S UD comprising epsilon-caprolactam in a concentration c UD , and feeding the stream S UD to the crystallization unit U C , and obtaining from U C a stream S SCPL comprising epsilon-caprolactam in a concentration c CPL , wherein

[0198] c SL < c UWS < c UD < c SCPL。

[0199] 35. The process of any one of embodiments 28 to 34, wherein the water separation unit U WS comprises at least two heat-consuming water separation sub-units U WS1 and U WS2 , preferably two heat-consuming water separation sub-units U WS1 and U WS2 coupled in series, wherein the stream S L is fed to U WS1 , and wherein at least part of the heat consumed in one or more of U WS1 and U WS2 is provided by at least one of the one or more streams S V .

[0200] 36. The process of embodiment 35, comprising one or more of (ii-1) and (ii-2), preferably (ii-1) and (ii-2):

[0201] (ii-1) obtaining at least one at least partially condensed aqueous stream S WS1 from U VW11 ;

[0202] (ii-2) obtaining at least one at least partially condensed aqueous stream S WS2 from U VW12 .

[0203] 37. The method according to embodiment 36, wherein at least one aqueous stream S RW1 is obtained from U WS1 and at least one aqueous stream S RW2 is obtained from U WS2 and wherein at least one of S RW1 and S RW2 is fed to U RW1 and S RW2 . W

[0204] 38. The method according to any one of embodiments 35 to 37, wherein downstream of U WS1 and upstream of U WS2 a separation unit U I is positioned, the method comprising obtaining an aqueous stream S WS1 from U UWS1 , feeding the stream S UWS1 to the separation unit U I , obtaining an aqueous stream S I from U UI , and feeding the stream S UI to the unit U WS2 , wherein in U I one or more impurities are separated from S UWS1 , thereby obtaining an impurities stream S I from U I , said impurities preferably comprising at least one impurity comprised in S R according to (vii).

[0205] 39. The method according to any one of embodiments 28 to 38, wherein the evaporation unit U E comprises two or more evaporation sub-units, the method comprising obtaining at least two vapor streams S V1 and S V2 , passing the vapor stream S V1 to at least one heat consuming unit, and passing the vapor stream S V 2to at least one heat consuming unit, wherein the vapor streams S V1 and S V2 differ from each other in terms of pressure and / or temperature.

[0206] 40. The method according to any one of embodiments 28 to 39, wherein downstream of U R at least one solid-liquid separation unit is arranged, wherein preferably at least one of the streams S L and S R is passed through at least one solid-liquid separation unit before being passed to the next downstream unit. ​

[0207] 41. The method of any one of embodiments 28 to 40, further comprising providing the stream S CPL to a polyamide 6 production unit U PP , wherein the polyamide 6 produced in U PP is preferably provided as a raw material to a textile material production unit U TP , from which unit U TP ,

[0208] (A) obtaining a marketable textile material M T , wherein after a lifetime T T of said textile material M MT , it is at least partially collected as textile waste in a textile material collection unit U TC ;

[0209] (B) obtaining a remaining material M R as textile waste;

[0210] wherein at least a portion of the textile waste according to (A), or at least a portion of the textile waste according to (B), or at least a portion of the textile waste according to (A) and at least a portion of the textile waste according to (B) is provided to U M , suitably via U R .

[0211] 42. The method of any one of embodiments 1 to 41, wherein 90 to 100 wt-%, preferably 91 to 100 wt-%, more preferably 92 to 100 wt-%, more preferably 93 to 100 wt-%, more preferably 94 to 100 wt-%, more preferably 95 to 100 wt-% of the liquid aqueous stream S W provided according to (iii) consists of water.

[0212] 43. The method of any one of embodiments 1 to 42, which is a continuous method, a semi-continuous method or a batch method.

[0213] 44. The method of any one of embodiments 1 to 43, wherein the solid material M provided according to (i) comprises, preferably consists of, waste material, preferably one or more of textile waste material and engineering plastic waste material, more preferably textile waste material.

[0214] 45. The S CPL for the preparation of polyamide 6, preferably further comprising the use of said polyamide 6 as a raw material for the preparation of one or more of textile material and engineering plastic material, more preferably for the preparation of textile material.

[0215] 46. A method for making polyamide 6, the method comprising using S CPL as a starting material, wherein the method preferably further comprises using the polyamide 6 as a feedstock for making one or more of a textile material and an engineering plastic material, more preferably for making a textile material.

[0216] 47. S CPL for making one or more of a polymer and a polymer product; or

[0217] A method for making one or more of a polymer and a polymer product, the method comprising using S CPL obtained or obtainable by the method of any one of embodiments 28 to 44 as a starting material.

[0218] 48. The use or method of embodiment 47, wherein the polymer, or the polymer product, or the polymer and the polymer product is in the form of at least one of a granule, a strand, a rod, a plate, a tube, a foil, a laminate, a film, a sheet, a fiber, a filament, a coating, an extruded article, a molded article, a flexible foam, a semi-rigid foam, and a rigid foam.

[0219] 49. The use or method of embodiment 47 or 48, wherein the polymer, or the polymer product, or the polymer and the polymer product comprises polyamide 6 and optionally at least one additional polymeric compound, wherein the at least one additional polymeric compound preferably comprises one or more of at least one polyamide 6.6; at least one semi-aromatic 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 cellulosic material; at least one natural elastomer; at least one synthetic elastomer; at least one copolymer of two or more of the polymeric compounds, including a statistical copolymer, a gradient copolymer, an alternating copolymer, a block copolymer, and a graft copolymer; and at least one rubber material, including one or more of at least one natural rubber material and at least one synthetic rubber material.

[0220] 50. The use or method of any one of embodiments 47 to 49, wherein the polymer, or the polymer product, or the polymer and the polymer product is part of one or one of:

[0221] - automotive parts, preferably cylinder head covers, engine covers, housings for charge air coolers, charge air cooler baffles, intake pipes, intake manifolds, connectors, gears, fan wheels, cooling water tanks, housings or housing parts for heat exchangers, coolant coolers, charge air coolers, thermostats, water pumps, radiators, fastening parts for electric cars or parts of battery systems, instrument panels, steering column switches, seats, headrests, center consoles, transmission parts, door modules, automotive exterior for A-, B-, C- or D-pillar covers, spoilers, door handles, exterior mirrors, windscreen wipers, windscreen wiper protection housings, decorative grilles, cover strips, roof racks, window frames, sunroof frames, antenna panels, headlamps, tail lamps, airbags, and / or seat cushions;

[0222] - cloth, clothing, preferably shirts, trousers, pullovers, boots, shoes, shoe soles, tights and / or jackets;

[0223] - electrical parts, preferably electrical components, electronic passive components, electronic active components, printed circuit boards, housing components, foils, lines, switches (such as microswitches), plugs, sockets, distributors, relays, resistors, capacitors, inductors, spools, lamps, diodes (such as LEDs), transistors, connectors, regulators, integrated circuits (IC), processors, controllers, memories, sensors, micro pushbuttons, semiconductors, reflector housings, for example for light emitting diodes, fasteners, spacers, bolts, strips, slide-in rails, screws, nuts, film hinges, snap hooks (clips) and / or spring tongues for electrical and / or electronic components;

[0224] - consumer and / or pharmaceutical products, preferably tennis strings, climbing ropes, brush bristles, brushes, artificial turf, 3D-printed filaments, lawn mowers, zippers, Velcro, paper machine wire cloths, extrusion coatings, fishing lines, fishing nets, offshore pipelines and ropes, vials, syringes, ampoules, bottles, sliding elements, spindle nuts, chain conveyors, plain bearings, rollers, wheels, gears, rollers, ring gears, screw and spring dampers, hoses, pipes, cable sheaths, sockets, switches, cable ties, fan wheels, carpets, boxes and / or bottles for cosmetics, mattresses, seat cushions, insulating materials;

[0225] - packaging for the food industry, preferably single- and / or multi-layer blown films, cast films (single- and / or multi-layer), biaxially stretched films, laminated films.

[0226] 51. The use or method of any one of embodiments 47 to 50, wherein the polymer, or the polymer product, or the polymer and the polymer product contains polyamide 6 in an amount of 1 wt-% or more, preferably 2 wt-% or more, more preferably 5 wt-% or more, more preferably 15 wt-% or more, more preferably 30 wt-% or more, more preferably 40 wt-% or more, more preferably 60 wt-% or more, more preferably 80 wt-% or more, more preferably 90 wt-% or more, more preferably 95 wt-% or more; and / or in an amount of 100 wt-% or less, preferably 95 wt-% or less, more preferably 90 wt-% or less, more preferably 50 wt-% or less, more preferably 25 wt-% or less, more preferably 10 wt-% or less.

[0227] For embodiment 51, the respective amounts are preferably determined based on an identity preservation and / or segregation and / or mass balance and / or book and claim regulatory chain model, more preferably based on a mass balance, more preferably based on the International Sustainability and Carbon Certification (ISCC) standard.

[0228] For embodiments 47 to 51, the preparation of the polymer, the polymer product, or the polymer and the polymer product can comprise one or more synthesis steps and can be carried out by conventional synthesis and techniques well known to the person skilled in the art. Examples of synthesis steps are described in "Industrial Organic Chemistry [Industrial Organic Chemistry]", Vol. 3, Wiley-VCH [Wiley-VCH Verlag], 1997; ISBN: 978-3-527-28838-0; "Kunststoffhandbuch [Plastics Handbook]", 11 of 17 subvolumes, Carl Hanser Verlag, in particular Vol. 6, "Polyamide [Polyamide]", 1st edition, 1966; "Injection Molding Reference Guide [Injection Molding Reference Guide]", 4th edition, CreateSpace Independent Publishing Platform, 2011, ISBN: 978-1466407824; WO 2008 / 155271 A1 and WO 2013 / 139827 A1, each of which is incorporated herein by reference.

[0229] The term "bar" as used herein refers to "abs", i.e. bar (absolute), sometimes also referred to as "bara".

[0230] The term "textile material" as used herein encompasses textile and non-textile raw materials which are processed into linear, planar and spatial structures by various methods. It relates to linear textile structures such as yarns, twisted yarns and ropes, planar textile structures such as woven fabrics, knitted fabrics, braids, stitch-bonded fabrics, nonwovens and felts, and three-dimensional textile structures, i.e. body structures, such as textile hoses, stockings or textile semi-finished products, produced therefrom; and it further relates to those end products which are brought into a saleable state by assembling, untying and / or other operations using the above-mentioned products, to be forwarded to processors, traders or end consumers. The term "textile waste" as used herein encompasses textile materials as defined above, whose intrinsic value has been consumed from the perspective of their current holder, and which is therefore scrap material for said holder.

[0231] The term "engineering plastics" as used herein refers to high-performance plastic grades which have physical properties that enable them to be used for long periods in structural applications, over a wide temperature range, under mechanical stress, and in difficult chemical and physical environments, for example, to manufacture plastic parts that replace traditional engineering materials like metals and ceramics. Engineering plastics are particularly suitable for the manufacture of mechanical parts in several industries such as automotive, medical, electrical and electronic, aerospace, construction and consumer goods. The term "engineering plastics waste" as used herein encompasses engineering plastic materials as defined above, whose intrinsic value has been consumed from the perspective of their current holder, and which is therefore scrap material for said holder.

[0232] The term "elastane" as used herein is also known as "spandex", and common brand names for spandex include Lycra, Elaspan, Acepora, Creora, Inviya, Roica, Dorlastan, Linel, or ESPA.

[0233] In the context of this invention, the term "X is one or more of A, B, and C" (where X is a given feature and each of A, B, and C represents a specific implementation of said feature) should be understood to disclose that X is A, or B, or C, or A and B, or A and C, or B and C, or A and B and C. In this respect, it should be noted that those skilled in the art can translate the above abstract terms into concrete examples, for example, where X is a chemical element and A, B, and C are specific elements such as Li, Na, and K, or X is a temperature and A, B, and C are specific temperatures such as 10°C, 20°C, and 30°C. In this regard, it should be further noted that those skilled in the art can extend the above terms to less specific implementations of the feature, such as "X is one or more of A and B," which discloses that X is A, or B, or A and B, or extend them to more specific implementations of the feature, such as "X is one or more of A, B, C, and D," which discloses that X is A, or B, or C, or D, or A and B, or A and C, or A and D, or B and C, or B and D, or C and D, or A and B and C, or A and B and D, or B and C and D, or A and B and C and D.

[0234] As described below, in Figures 1 to 14 The preferred aspects of the invention are further illustrated below. Attached Figure Description

[0235] Figure 1 The method according to the invention is demonstrated. A suitably provided solid material M comprising polyamide 6 is fed into the melting unit U. M In this process, a liquid flow S is obtained from the melting unit. M And further transfer the liquid flow to the pre-reaction unit U PR In this pre-reaction unit, it is reacted with a liquid aqueous stream S W Mix. Then it will be from unit U PR The obtained liquid flow S F Transferred to reaction unit U R In this reaction unit, it is subjected to polyamide 6 depolymerization conditions to obtain an aqueous depolymerization mixture containing ε-caprolactam dissolved in water. Then, from unit U... R The outlet flow S of the aqueous liquid reactor containing ε-caprolactam dissolved in water will be... R Remove.

[0236] Figure 2 The method according to the present invention is demonstrated. In addition... Figure 1 In addition to the method design shown in the figure, according to Figure 2 Melting unit U M It is equipped with a degassing system. Through this degassing system, the gas stream S... GM Removed when solid material M is in UM The gas stream is obtained during melting. Then the stream S... GM Transmitted to washing unit U S .

[0237] Figure 3 The method according to the present invention is demonstrated. In addition... Figure 2 In addition to the method design shown, the filter unit U F Arranged in melting unit U M Downstream and reaction unit U R Upstream of unit U. M The obtained stream S M Passing through the filter unit, and in U F The downstream of the appropriate filtered stream S M Transferred to pre-reaction unit U PR .

[0238] Figure 4 The method according to the present invention is demonstrated. (And...) Figure 3 Compared to the method design shown in the previous section, the reaction unit U is shown. R The preferred design. Based on this preferred design, unit U... R It consists of three reactors, R1, R2, and R3, arranged in series and preferably vertically. The pre-reaction unit U... PR The obtained stream S SF The feed is introduced into reactor R1, where it is subjected to polyamide 6 depolymerization conditions, and a liquid aqueous stream S1 is obtained from the reactor. This liquid aqueous stream contains ε-caprolactam dissolved in water and further contains undepolymerized polyamide 6. Stream S1 is then transferred, preferably by gravity only, to reactor R2, where it is subjected to polyamide 6 depolymerization conditions, and a liquid aqueous stream S2 is obtained from the reactor. This liquid aqueous stream contains ε-caprolactam dissolved in water and further contains undepolymerized polyamide 6. Stream S2 is then transferred, preferably by gravity only, to reactor R3, where it is subjected to polyamide 6 depolymerization conditions, and a liquid aqueous stream S3 is obtained from the reactor. This liquid aqueous stream contains ε-caprolactam dissolved in water. Stream S3 is then used as stream S. R From reaction unit U R Move out of the middle.

[0239] Figure 5 The reactor R used according to the present invention is shown. i The preferred design. If more than one reactor R is used. i For example, as mentioned above Figure 4 As described in the context, it is preferred that each reactor R i This demonstrates the superior design.Figure 5 The reactor R i is a stirred tank reactor. In Figure 5 the following reference signs are used:

[0240] (1) vertically arranged three-compartment reactor R i

[0241] (2) outlet device for degassing the reactor

[0242] (3) outlet device for removing the liquid reaction mixture from R i

[0243] (4) inlet device for feeding a liquid stream into R i (like stream S F into R1),

[0244] (5) heating jacket

[0245] (6.1) top compartment

[0246] (6.2) middle compartment

[0247] (6.3) bottom compartment

[0248] (7.1) stirrer of the top compartment

[0249] (7.2) stirrer of the middle compartment

[0250] (7.3) stirrer of the middle compartment

[0251] (8) drive unit for the stirrers according to (7.1)-(7.3)

[0252] (9.1) partition between the top compartment and the middle compartment with flow-through openings

[0253] (9.2) partition between the middle compartment and the bottom compartment with flow-through openings

[0254] (10.1) inlet device for passing a heating medium into the heating jacket (5)

[0255] (10.2) outlet device for removing the heating medium from the heating jacket (5)

[0256] Figure 6 A method according to the application is illustrated. Compared to the method design Figure 4 illustrated, it is shown how a preferred design of the solid material M is provided. According to Figure 6 , the solid material is in the delivery unit M MD ​The delivery unit U, for example, can comprise one or more bulk bag stations and / or one or more bulk container stations. The material M is then delivered from the unit U MD to a suitable material collection unit M MC， The material collection unit M preferably comprises, more preferably consists of, a drum. The material M is then delivered from the unit M MC to a suitable melting unit U M .

[0257] Figure 7 A method according to the application is shown. In comparison to the method design shown in Figure 6 how the solid material M is delivered from the delivery unit U MD to the collection unit M MC is shown. The preferred method according to Figure 7 the unit U MD comprises, for example, one bulk container station and two bulk bag stations, from which the material M is delivered to the particle separation unit U FMPS (1), wherein the material M is delivered from the first bulk bag station to the particle separation unit U FMPS (2.1), and wherein the material M is delivered from the second bulk bag station to the particle separation unit U FMPS (2.2). The material M is then passed from U FMPS (1) through a feeding unit U FMF (1), such as a rotary feeder, and via U FMF (1) to a receiving and discharge device U MRD (3), preferably a hopper, and U MRD (4), preferably a hopper. Further, the material M is then delivered from U FMPS (2.1) to a receiving and discharge device U MRD (2.1), preferably a hopper, and from U MRD (2.1) through a feeding unit U FMF (2.1), such as a rotary feeder, and via U FMF (2.1) to a receiving and discharge device U MRD (3) and U MRD (4). Likewise, the material M is then delivered from U FMPS (2.2) to a receiving and discharge device U MRD (2.2), preferably a hopper, and from U MRD (2.2) through a feeding unit U FMF (2.2), such as a rotary feeder, and via U FMF (2.2) to a receiving and discharge device U MRD(3) and U MRD (4). Then material M is transferred from U MRD (3) and / or U MRD (4) Via unit U FMF (3) Preferably a rotary feeder and / or unit U FMF (4) Preferably, a rotary feeder delivers the feed to the collection unit UMC. Further in... Figure 7 The gas flow S is shown in the figure. G (1) S G (2) and S G (3) These gas streams are delivered to the corresponding sections of the first connecting line to pneumatically transport material M to the corresponding downstream unit as shown. Prior to delivery to the corresponding sections of the first connecting line (not shown), preferably at least one, preferably all, of the gas streams are subjected to gas filtration, followed by compression and subsequent cooling.

[0258] Figure 8 The method according to the present invention is demonstrated. (And...) Figure 6 Compared to the method design shown, this demonstrates how solid material is transferred from the collection unit U via a second connecting line. MC (Preferably including a collecting drum) transferred to the melting unit U M The preferred method. According to Figure 8 Solid material M is fed through the first feeding unit U. SMF (1) For example, the rotary feeder from unit U MC Transferred to particle separation unit U SMPS For example, a vibrating screen. Then the material M is transferred from U... SMPS Transferred to the second feeding unit U SMF (2) Preferably, a weightless feeding device, such as a weightless screw, is used to appropriately transfer the material M from the second feeding unit to the melting unit U. M Preferably, with, as Figure 6 The preferred method shown is combined with the following to see Figure 8 The unit U shown M The preferred method for upstream components.

[0259] Figure 9 The method according to the present invention is demonstrated. (And...) Figure 4 Compared to the method design shown, a further demonstration is shown in unit U. R Each reactor R included i Obtain gas flow S Gi And remove it from each reactor. Then these gas streams, especially S... G1 S G2 and S G3 Appropriately merge and transfer to the washing unit U S It should be noted that the flow SGi It can also be passed to unit U separately. S (Alternative solutions are not shown). It is further conceivable to consider stream S... Gi One or more of them are fed into U S Before and from the melting unit U M The obtained gas flow S GM Merge (alternative options are not shown).

[0260] Figure 10 The method according to the present invention is demonstrated. Figure 10 The reaction unit U is shown in the figure. R The preferred sequence of downstream stages, and the flow of water through stream S W Optimal recycling. According to Figure 10 The method obtains the liquid aqueous flow S3 and uses it as flow S R The liquid aqueous stream containing ε-caprolactam and one or more impurities is removed from the last reactor R3 of unit UR. Then the stream S... R Transferred to evaporation unit U E Liquid aqueous flow S is obtained from this evaporation unit. L and one or more water vapor streams S V And remove it; in Figure 10 In the diagram, only one vapor flow S is shown. V Flow S L Having specific flow S R Higher ε-caprolactam concentration. Then flow S L Transferred to the heat-consuming purification unit U P Further purification of ε-caprolactam occurs in this unit. From the feed to U P Flow S in L Ultimately, the product flow S is obtained. CPL Its concentration is significantly higher than that of the flow S. L The concentration of ε-caprolactam. According to the method of the present invention, purification unit U... P At least a portion of the heat consumed is generated by one or more steam streams S V At least one of them is provided, and based on S V To obtain one or more at least partially condensed aqueous flows S VW and from U P Remove from the middle; in Figure 10 Only one stream S is shown in the diagram. VW Furthermore, from purification unit U P From S L Obtain one or more water-borne flows S RW Then at least one stream S VWrecycled at least partially to the reaction unit U R and at least one stream S RW is further recycled at least partially to the reaction unit U R wherein for the purpose of said recycling, the stream S VW and S RW is passed to a water treatment unit U W from which a stream S W is obtained which is then recycled (at least partially) to the reaction unit U W (or a part thereof) as aqueous stream S R . From U W one or more waste water streams S WW are further obtained which are not recycled to the process. Preferably, the water treatment unit U W comprises a water recovery unit U WR and optionally a waste water unit U WW . Preferably, the streams S VW and S RW are passed to a water treatment unit U W in which they are suitably purified and / or suitably collected in order to obtain one or more aqueous recycle streams. Streams obtained from such purification can then be passed to a waste water treatment unit U WW from which a waste water stream S WW is obtained.

[0261] Figure 11 A process according to the present application is illustrated. The process according to Figure 11 illustrates the further use of the stream S CPL , i.e. the purified ε-caprolactam. According to the present application, the stream S CPL is preferably passed to a polyamide 6 production unit U PP in which the stream S CPL is used as starting material. If desired, one or more further streams S NCPL containing non-recycled ε-caprolactam, i.e. ε-caprolactam from a conventional source, can be additionally passed to U PP . The correspondingly prepared polyamide 6 material is then passed to a unit U TP in which the polyamide 6 material is used as starting material for the preparation of a material comprising polyamide 6, preferably a textile material comprising polyamide 6. If desired, one or more further streams S NPA6 containing non-recycled polyamide 6, i.e. polyamide 6 from a conventional source, can be additionally passed to U TP . According to the process in U TPThe types of materials prepared in the process can also transfer other streams containing one or more starting materials other than polyamide 6 to U. TP This material, preferably from U... TP The obtained textile material M T Then it enters the market and remains there for a given lifespan T. MT Subsequently, the corresponding scrap materials are appropriately collected in collection unit U. TC In the preferred textile material collection unit, waste materials are collected from this unit as flow S M Or as a flow S M A portion is appropriately transferred to reaction unit U R Preferably via unit U M Transferred to reaction unit U R Used to transfer stream S M Provide to U R This type of unit U M Typically, it includes the means by which a preferred solid material M can be suitably transferred to the reaction unit U. R Any device. Preferably, U M This includes devices such as one or more silos, one or more hoppers, one or more truck unloading stations, one or more large bag unloading stations, etc. Further in... Figure 11 The diagram shows the production unit U. TP In this process, surplus material M is obtained from the production method. R That is, not included in M T The materials in [the text]. As an example, M... R It can be in the form of textile shavings. This material can be processed via U... TC and / or directly via U M As flow S M Or as a flow S M Part of the feed is sent to U R Preferably, according to the above text Figure 6 , 7 The methods shown in section 8.

[0262] Figure 12 The method according to the present invention is demonstrated. (And...) Figure 11 In contrast, unit U is shown. P The preferred design, namely Figure 12 The method shown illustrates the purification process of ε-caprolactam stream S. L The preferred method. According to this method, firstly, the flow S... L Transferred to water separation unit U WS One or more streams S are obtained from this unit. RW Then, preferably, the one or more streams are passed to, as already in use, the destination. Figure 11 The water treatment unit U shown in the figureW Further, at least one of the streams S V is passed to U WS for at least partially satisfying the heat demand of U WS ; based on the at least one stream S WS passed to U V , one or more at least partially condensed streams S VW1 are obtained and preferably further passed to the water treatment unit U W , in particular U WR . The stream S UWS containing ε-caprolactam is then preferably passed to the distillation unit U D for further purification with respect to ε-caprolactam. Further, at least one of the streams S V is passed to U D for at least partially satisfying the heat demand of U D ; based on the at least one stream S D passed to U V , one or more at least partially condensed streams S VW2 are obtained and preferably further passed to the water treatment unit U W , in particular U WR . The stream S UD containing ε-caprolactam is then preferably passed to the crystallization unit U C for further purification with respect to ε-caprolactam. Further, at least one of the streams S V is passed to U C for at least partially satisfying the heat demand of U C ; based on the at least one stream S C passed to U V , one or more at least partially condensed streams S VW3 are obtained and preferably further passed to the water treatment unit U W , in particular U WR .

[0263] Figure 13 A process according to the present application is shown. Compared to Figure 13 , a preferred design of the unit U WS is shown, i.e. the process shown in Figure 13 shows a preferred way of separating water from the stream S L . According to this process, the stream S L is first passed to a first stage of water separation in the unit U WS1 . The stream S UWS1 containing ε-caprolactam is then passed from U WS1 to an intermediate treatment stage U IImpurities can be removed at this stage. Then it will be removed from U I The purified stream S obtained from this process UI Further transmission to unit U WS2 The second stage of water separation is carried out in unit U. WS2 Obtain a stream S containing ε-caprolactam. UWS2 This flow corresponds to, for example Figure 12 The flow S shown UWS And then preferably it is passed to the distillation unit U. D From intermediate unit U I The stream S containing the corresponding separated impurities is removed. I Depending on the amount and / or chemical properties of the impurities, the stream can be used for further applications. According to this method, one or more aqueous streams S are obtained. RW1 Then preferably it is transferred to the water treatment unit U W Especially U WR Furthermore, based on this method, one or more aqueous flows S are obtained. RW2 Then preferably it is transferred to the water treatment unit U W Especially U WR Preferably, the flow S V At least one of them is passed to U WS1 To be used to at least partially satisfy U WS1 The heat demand; based on the transfer to U WS1 The at least one stream S V To obtain one or more at least partially condensed streams S VW11 And preferably, it is further transferred to the water treatment unit U. W Especially U WR Preferably, the flow S V At least one of them is passed to U WS2 To be used to at least partially satisfy U WS2 The heat demand; based on the transfer to U WS2 The at least one stream S V To obtain one or more at least partially condensed streams S VW12 And preferably, it is further transferred to the water treatment unit U. W Especially U WR .

[0264] Figure 14 The method according to the present invention is demonstrated. (And...) Figure 13 In contrast, another example is shown above. Figure 11 The preferred recycling loop shown above, and as already described above... Figure 9 The diagram shows the gas stream S obtained and removed from reactors R1, R2, and R3. GiThe processing of the data is performed.

Claims

1. A process for hydrolytic depolymerization of polyamide 6 contained in a solid material M, the process comprising (i) providing the solid material M; (ii) melting the solid material M provided according to (i) in a melting unit U M , thereby obtaining a liquid stream S M having a temperature T SM at a pressure p SM ; (iii) providing a liquid aqueous stream S SW having a temperature T SW at a pressure p W ; (iv) mixing the stream S PR obtained according to (ii) with the stream S M provided according to (iii) in a pre-reaction unit U W , thereby obtaining a liquid reaction feed stream S SF having a temperature T SF at a pressure p F ; (v) passing the stream S obtained according to (iv) F to the chemical reaction unit U R ; (vi) In this reaction unit U R The middle makes this flow S F Exposed to the depolymerization pressure p of polyamide 6 D The depolymerization temperature T of polyamide 6 below D The depolymerization conditions of polyamide 6, thus in U R To obtain an aqueous depolymerization mixture containing ε-caprolactam dissolved in water; (vii) removing aqueous liquid reactor outlet stream S R from the U R , which stream S R comprises ε-caprolactam dissolved in water; where 0.8 < T SF / T D ≤ 1.05 and 0.9 < p SF / p D ≤ 1.

05.

2. The method of claim 1, wherein, 0.6 ≤ T SM / T SF ≤ 1.05 and 0.9 ≤ p SM / p SF ≤1.05, and wherein 0.8 ≤ T SW / T SF ≤ 1.3 and 0.9 ≤ p SW / p SF ≤ 1.

05.

3. The method of claim 1 or 2, wherein, The pre-reaction unit U according to (iv) PR comprising, preferably consisting of, a mixing unit, preferably a static mixing unit, wherein S W and S M are mixed in U W with a mixing ratio (m P / kg) / (m PR / kg) in the range of preferably 1 : 1 to 20 : 1, more preferably 2 : 1 to 15 : 1, more preferably 5 : 1 to 10 : 1, wherein m W is the amount of water contained in S W and m P is the amount of polyamide 6 contained in S M ; Wherein the melting unit U M Includes an extruder, preferably a single-screw extruder or a twin-screw extruder, preferably composed of an extruder, preferably a single-screw extruder or a twin-screw extruder, wherein the melting unit U M Preferably equipped with a degassing system, the method preferably includes, during the melting process according to (ii), removing gas from U M Middle removed gas flow S GM The gas flow S GM Under pressure p GM Below has temperature T GM Preferably, 0.95 ≤ T GM / T SM ≤ 1.05, where makes from U M The gas stream S removed from the middle GM Preferably in the washing unit U S It has undergone purification.

4. The method of any one of claims 1 to 3, wherein, Downstream of the melting unit U M and upstream of the reaction unit U R , a filtration unit U F , preferably a filtration unit U F is arranged for separating particles having a particle size in the range of 100 to 500 microns, preferably in the range of 200 to 400 microns, from the liquid stream S M , wherein the method comprises passing the stream liquid stream S M through U F prior to mixing according to (iv).

5. The method of any one of claims 1 to 4, wherein, According to (vi), T D in the range of 230 to 330 °C and p D in the range of 40 to 140 bar, preferably wherein T D in the range of 250 to 320 °C and p D in the range of 40 to 125 bar, more preferably wherein T D in the range of 270 to 310 °C and p D in the range of 40 to 110 bar.

6. The method of any one of claims 1 to 5, wherein, the reaction unit U according to (v) R comprising z chemical reactors R i , i = 1...z, wherein z is in the range of 1 to 10, preferably in the range of 1 to 8, more preferably in the range of 1 to 6, more preferably in the range of 1 to 5, more preferably in the range of 1 to 4, more preferably in the range of 1 to 3, wherein if z > 1, at least 2 reactors R i , preferably z reactors R i are coupled in series, wherein - according to (v), the stream S SF is fed to R i where i = 1 ; - an aqueous liquid stream S containing ε-caprolactam dissolved in water i from the reactor R i and fed to the reactor R i+1 where i < z; - according to (vii), the aqueous liquid stream S containing ε-caprolactam dissolved in water is removed from the reactor R z as stream S R from the reactor R z ; wherein in each reactor R i the depolymerization temperature T Di is maintained at a depolymerization pressure p Di wherein independently from each other, T Di is in the range of 230 to 330 °C and p Di is in the range of 40 to 140 bar, preferably wherein T Di is in the range of 250 to 320 °C and p Di is in the range of 40 to 125 bar, more preferably wherein T Di is in the range of 270 to 310 °C and p Di is in the range of 40 to 110 bar, wherein for z > 1, the z reactors R i are preferably arranged vertically, wherein R1 is the topmost reactor and R z is the bottommost reactor, wherein S i obtained from R i is transferred to R i+1 , preferably by gravity, more preferably by gravity only.

7. The method of claim 6, wherein, at least 1, preferably z reactors R i are stirred tank reactors, wherein preferably each stirred tank reactor R i preferably have 2 to 6 compartments, more preferably 2 to 5 compartments, more preferably 2 to 4 compartments, independently from each other, which are preferably arranged in series, more preferably in series and vertically, wherein 2 adjacent compartments are separated by a partition comprising at least one flow-through opening, wherein preferably the reactor R i comprises at least one compartment comprising at least one stirrer, wherein more preferably each reactor R i comprises at least one compartment comprising at least one stirrer, wherein more preferably each reactor R i comprises one stirrer per compartment, wherein the process comprises stirring the depolymerization mixture in a given compartment for at least a portion of the time during which said compartment is subjected to depolymerization conditions; The depolymerization conditions of polyamide 6 according to (vi) preferably further include the aqueous depolymerization mixture in unit U. R In the z reactors R, it is more preferable to use the z reactors R i The total residence time t in the z stirred tank reactors is preferred. D The aqueous depolymerization mixture contains at least 85% by weight, preferably at least 90% by weight, and more preferably at least 95% by weight, having a t in the range of 30 to 90 min. D ; wherein for z > 1 the residence time of the aqueous depolymerisation mixture in the reactor R i is t Di , and wherein preferably 0.90 ≤ (t Di / t Di+1 ) ≤ 1.10, more preferably 0.95 ≤ (t Di / t Di+1 ) ≤ 1.

05.

8. The process according to claim 6 or 7, comprising removing from at least one reactor R i , preferably from all z reactors R i , a respective gas stream S Gi (given gas stream S Gi having a temperature T Gi at a pressure p Gi ), wherein 0.95 ≤ T Gi / T Di ≤ 1.05, the process preferably further comprising merging at least one, preferably all streams S GM in the gas stream S Gi with the gas stream S Gi prior to subjecting the gas stream S GM as defined in claim 3 to washing as defined in claim 3.

9. The method of any one of claims 1 to 8, wherein, The provision of the solid material M according to (i) comprises (i.1) providing the solid material M in a delivery unit U MD , wherein U MD preferably comprises one or more of at least one big bag station and at least one bulk container station; (i.2) passing the solid material M provided according to (i.1) from the unit U via a first connecting line to MD a material collection unit U MC , preferably a collection drum, wherein the first connecting line preferably comprises one or more of MRD at least one first material feeding unit U FMF and at least one first particle separation unit U FMPS at least one material receiving and discharge unit U (i.3) removing the solid material M from the unit U MC via a second connection line to the unit U M wherein the second connection line preferably comprises one or more of at least one second material feeding unit U SMF , at least one second particle separating unit U SMPS and at least one metal detector; wherein the first connecting line according to (i.2) preferably comprises at least one unit U MRD , preferably at least one hopper, more preferably at least one single-zone hopper, and preferably further comprising at least one unit U FMF , preferably at least one rotary feeder, and preferably further comprising at least a particle separation unit U FMPS , more preferably at least one filter, more preferably at least one screen filter; In order to transfer the solid material M from the unit U via the first connecting pipe MD Transmitted to this unit U MC Preferably, at least one gas flow S G Passing through the first connecting pipeline, the at least one gas flow preferably contains air or rarefied air, more preferably consists of air or rarefied air, wherein before passing through the first connecting pipeline, the at least one gas flow is preferably pretreated by at least one of filtration, compression and cooling, more preferably by filtration, compression and cooling; wherein the second connecting line according to (i.3) preferably comprises at least two units U SMF , preferably a rotary feeder and a loss-in-weight feeder, wherein more preferably the rotary feeder is arranged upstream of the loss-in-weight feeder, and further comprising units U SMPS , preferably a vibrating screen.

10. The method of any one of claims 1 to 9, wherein, According to (i), the solid material M is provided in the form of particles, preferably to U M wherein the particle size distribution of the particles is preferably characterized by one or more, preferably by two or more, more preferably by the following three pairs of values: - a D10 value of the particle width in the range of 0.3 to 15 mm and a D10 value of the particle length in the range of 0.3 to 15 mm; - a D50 value of the particle width in the range of 0.5 to 20 mm and a D50 value of the particle length in the range of 0.5 to 20 mm; - a D90 value of the particle width in the range of 0.8 to 30 mm and a D90 value of the particle length in the range of 0.8 to 30 mm; wherein preferably 10 to 100 wt-%, more preferably 30 to 100 wt-%, more preferably 50 to 100 wt-%, more preferably 60 to 100 wt-%, more preferably 70 to 100 wt-%, more preferably 80 to 100 wt-% of the solid material M consists of polyamide 6.

11. The method of any one of claims 1 to 10, wherein, 90 to 100 wt-%, preferably 91 to 100 wt-%, more preferably 92 to 100 wt-%, more preferably 93 to 100 wt-%, more preferably 94 to 100 wt-%, more preferably 95 to 100 wt-% of the liquid aqueous stream S provided according to (iii) W consists of water.

12. The method of any one of claims 1 to 11, wherein, The solid material M provided according to (i) comprises, preferably consists of, waste material, preferably one or more of textile waste material and engineering plastic waste material, more preferably textile waste material.

13. The method of any one of claims 1 to 12, wherein, According to (vii), the stream S R comprising ε-caprolactam in a concentration c SR ε-caprolactam dissolved in water, the stream S R further comprising one or more impurities, the method further comprising (viii) passing the liquid aqueous stream S R to the evaporation unit U E , thereby obtaining from S R a liquid aqueous stream S SL containing ε-caprolactam dissolved in water at a concentration c L , wherein c SL > c SR , and further obtaining from S R one or more aqueous vapor streams S V ; (ix) This water flow S L Transferred to the heat-consuming purification unit U P In, thus from S L Obtain the concentration c SCPL The flow of ε-caprolactam S CPL , where c SCPL >> c SL And further from S L Obtain one or more water-borne flows S RW U P At least a portion of the heat consumed is generated by one or more streams S V At least one of them is provided, thereby from the at least one stream S V Obtain at least one at least partially condensed aqueous flow S VW ; (x) at least one stream S VW at least partially recycled to the reaction unit U R and at least one stream S RW at least partially recycled to the reaction unit U R .

14. The method as claimed in claim 13, further comprising providing the stream S obtained according to (ix) CPL to a polyamide 6 production unit U PP , wherein the polyamide 6 produced in U PP is preferably provided as a raw material to a textile material production unit U TP , from which unit U TP ​ (A) obtaining a textile material M put on the market T wherein after a lifetime T T of said textile material M MT at least a part of it is collected in a textile material collecting unit U TC as textile waste; (B) obtaining the remaining material M R as textile waste; wherein at least a portion of the textile waste according to (A), or at least a portion of the textile waste according to (B), or at least a portion of the textile waste according to (A) and at least a portion of the textile waste according to (B) is suitably subjected to U M providing to U R .

15. S obtainable or obtained by the method according to claim 16 CPL Use for the preparation of one or more of the polymers and polymer products, wherein, The polymer, or the polymer product, or the polymer and the polymer product, is in the form of at least one of a particle, a strand, a rod, a plate, a tube, a foil, a laminate, a film, a sheet, a fiber, a filament, a coating, an extruded article, a molded article, a flexible foam, a semi-rigid foam, and a rigid foam; and wherein the polymer, or the polymer product, or the polymer and the polymer product, comprises polyamide 6 and optionally at least one additional polymeric compound, wherein the at least one additional polymeric compound preferably comprises one or more of at least one polyamide 6.6; at least one semi-aromatic polyamide, including one or more of polyamide 6T and polyamide 61; 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 cellulosic material; at least one natural elastomer; at least one synthetic elastomer; at least one copolymer of two or more of the polymeric compounds, including statistical copolymers, gradient copolymers, alternating copolymers, block copolymers, and graft copolymers; and at least one rubber material, including one or more of at least one natural rubber material and at least one synthetic rubber material; wherein the polymer, or the polymer product, or the polymer and the polymer product, is preferably part of one or of one of: at least one polyamide 6.6; at least one semi-aromatic polyamide, including one or more of polyamide 6T and polyamide 61; at least one polyethylene terephthalate; at least one polyurethane; at least one polyester; at least one polyether; at least one polyvinyl chloride; - automotive parts, preferably cylinder head covers, engine covers, housings for charge air coolers, charge air cooler baffles, intake pipes, intake manifolds, connectors, gears, fan impellers, cooling water tanks, housings or housing parts for heat exchangers, coolant coolers, charge air coolers, thermostats, water pumps, radiators, fastening parts for electric cars or parts of battery systems, instrument panels, steering column switches, seats, headrests, center consoles, transmission parts, door modules, automotive exterior for A-, B-, C- or D-pillar covers, spoilers, door handles, exterior mirrors, windscreen wipers, windscreen wiper protection housings, decorative grilles, cover strips, roof racks, window frames, sunroof frames, antenna panels, headlamps, tail lamps, airbags, and / or seat cushions; - cloth, clothing, preferably shirts, trousers, pullovers, boots, shoes, shoe soles, tights and / or jackets; - electrical parts, preferably electrical components, electronic passive components, electronic active components, printed circuit boards, housing components, foils, lines, switches (such as microswitches), plugs, sockets, distributors, relays, resistors, capacitors, inductors, spools, lamps, diodes (such as LEDs), transistors, connectors, regulators, integrated circuits (IC), processors, controllers, memories, sensors, micro pushbuttons, semiconductors, reflector housings, for example for light emitting diodes, fasteners, spacers, bolts, strips, slide-in rails, screws, nuts, film hinges, snap hooks (clips) and / or spring tongues for electrical and / or electronic components; - consumer and / or pharmaceutical products, preferably tennis strings, climbing ropes, brush bristles, brushes, artificial turf, 3D printing filaments, lawn mowers, zippers, nylon snaps, paper machine wire cloths, extrusion coatings, fishing lines, fishing nets, offshore pipelines and ropes, vials, syringes, ampoules, bottles, sliding elements, spindle nuts, chain conveyors, plain bearings, rollers, wheels, gears, rollers, ring gears, screw and spring dampers, hoses, pipes, cable sheaths, sockets, switches, cable ties, fan impellers, carpets, boxes and / or bottles for cosmetics, mattresses, seat cushions, insulating materials; - packaging for the food industry, preferably single- and / or multi-layer blown films, cast films (single- and / or multi-layer), biaxially stretched films, laminated films.

Images