The present invention relates to a process for separating at least one e-caprolactam oligomeric compound CPO from a stream comprising said at least one CPO and e-caprolactam monomeric compound CPM.

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

Surprisingly, it was found that the process of the present invention permits to efficiently separate e-caprolactam oligomers from e-caprolactam monomeric compounds compared to known processes, which permits among others to improve recycling of solid material comprising a polyamide, such as textile waste materials, in particular after hydrolytical depolymerization of a polyamide. Hence, using a process for separating at least one e-caprolactam oligomeric compound CPO from a stream SR comprising said at least one CPO and e-caprolactam monomeric compound CPM according to the present invention permits to reduce the CO2 footprint.

Therefore, the present invention relates to a process for separating at least one e-caprolactam oligomeric compound CPO from a stream SR comprising said at least one CPO and e- caprolactam monomeric compound CPM, the process comprising

(i) providing an aqueous liquid stream S comprising CPM dissolved in water at a concentration CR(CPM), CPM having a boiling point TCPM, wherein SR further comprises the at least one CPO at a concentration CR(CPO), CPO having a boiling point TCPO with TCPO > TCPM;

(ii) preparing an aqueous liquid mixture ME comprising the stream SR provided according to (i);

(iii) subjecting the mixture ME according to (ii) to evaporation conditions in an evaporation unit E1, obtaining an aqueous vapor stream Svi and an aqueous liquid stream SM , wherein Svi comprises CPM at a concentration Cvi(CPM) with Cvi(CPM) > CR(CPM), wherein SM comprises the at least one CPO at a concentration CM(CPO) with CM(CPO) > CR(CPO) and comprises CPM at a concentration CM(CPM) with CM(CPM) < CR(CPM);

(iv) dividing the stream SM according to (iii) into a first stream SLU and a second stream S1.12, wherein SLU and SLI2 have the same chemical composition as SLI ;

(v) passing the stream SLI2 obtained according to (iv) to a downstream treatment stage; wherein preparing the aqueous liquid mixture ME according to (ii) comprises mixing the stream SR with the stream SLU . In the context of the present invention, the term “c-caprolactam oligomeric compound” (CPO) encompasses any non-monomeric compounds form of e-caprolactam oligomeric, i.e. any oligomeric compound form of e-caprolactam including polyamide 6.

Preferably, the stream SR provided according to (i) has a temperature in the range of from 100 to 150 °C, more preferably in the range of from 110 to 145 °C, more preferably in the range of from 120 to 140 °C.

Preferably, the stream S provided according to (i) exhibits a CPM concentration in the range of from

15 to 90 weight-%, more preferably in the range of from 20 to 75 weight-%, more preferably in the range of from 25 to 60 weight-%, and a CPO concentration in the range of from 0.5 to 10 weight-%, more preferably in the range of from 0.5 to 7 weight-%, more preferably in the range of from 0.5 to 4 weight-%; the stream Svi obtained according to (iii) exhibits a CPM concentration in the range of from 65 to 99 weight-%, more preferably in the range of from 65 to 90 weight-%, more preferably in the range of from 65 to 80 weight-%, wherein the stream Svi obtained according to (iii) more preferably exhibits a CPO concentration in the range of from 0 to 0.4 weight-%, more preferably in the range of from 0 to 0.3 weight-%, more preferably in the range of from 0 to 0.2 weight-%; the stream SLI obtained according to (iii) exhibits a CPM concentration in the range of from 0.1 to 10 weight-%, more preferably in the range of from 0.5 to 7.5 weight-%, more preferably in the range of from 1 to 5 weight-%, and a CPO concentration in the range of from 1 to 10 weight-%, more preferably in the range of from 1 .5 to 10 weight-%, more preferably in the range of from 2 to 10 weight-%.

Preferably, according to a first alternative as to the preparation of the aqueous liquid mixture ME, preparing the aqueous liquid mixture ME according to (ii) further comprises, prior to mixing the stream SR with the stream SLU , heating the stream SLU obtained from (iv) to a temperature in the range of from 200 to 270 °C, more preferably in the range of from 210 to 270 °C, more preferably in the range of from 220 to 270 °C.

Preferably, according to said first alternative, heating the stream SLU comprises passing the stream SLU through a heat exchanger Hi. Preferably, according to said first alternative, according to (ii), the stream SR provided according to (i) and the stream SLU obtained from heating are mixed in the evaporation unit Ei. Preferably, according to said first alternative, prior to mixing the stream SR with the stream SLU , the stream SR provided according to (i) is not heated.

It is conceivable according to said first alternative that one or more heat exchangers upstream of Hi be preferably used. Preferably, no further heat exchanger is used upstream of Hi. The first alternative as to the preparation of the aqueous liquid mixture ME is in particular illustrated by Figure 1.

Preferably, according to a second alternative as to the preparation of the aqueous liquid mixture ME, preparing the aqueous liquid mixture ME according to (ii) comprises mixing the stream SR provided according to (i) with the stream SLU obtained from (iv) and heating the combined stream to a temperature in the range of from 200 to 270 °C, more preferably in the range of from 210 to 270 °C, more preferably in the range of from 220 to 270 °C.

Preferably heating the combined stream comprises passing the stream SLU through a heat exchanger Hi. Preferably, prior to mixing the stream S with the stream SLU , the stream SR provided according to (i) is not heated. It is conceivable according to said second alternative that one or more heat exchangers upstream of Hi be preferably used. Preferably, no further heat exchanger is used upstream of Hi.

The first alternative as to the preparation of the aqueous liquid mixture ME is in particular illustrated by Figure 2.

In the context of the present invention, preferably, the evaporation in the evaporation unit Ei according to (iii) is carried out in one or more stirred vessels, or in one or more film evaporators, or in one or more stirred vessels and in one or more film evaporators. More preferably, the evaporation in the evaporation unit Ei according to (iii) is carried out in one or more continuous stirred-tank reactors, or in one or more falling film evaporators, or in one or more continuous stirred-tank reactors and in one or more falling film evaporators. More preferably, the evaporation in the evaporation unit Ei according to (iii) is carried out in one or more continuous stirred-tank reactors, wherein more preferably, if evaporation in Ei is carried out in more than one continuous stirred-tank reactors, the continuous stirred-tank reactors are arranged in parallel.

Preferably, the one or more stirred vessels and the one or more film evaporators are equipped with heating means to indirectly providing heat for the evaporation carried out in Ei, the process comprising passing a heating medium through said heating means, wherein said heating means are more preferably heating jackets.

Preferably, the evaporation conditions according to (iii) comprise an evaporation temperature TEI of the mixture ME, wherein TEI is in the range of from 200 to 270 °C, more preferably in the range of from 210 to 270 °C, more preferably in the range of from 220 to 270 °C, and the evaporation conditions according to (iii) further comprise an evaporation pressure PEI , wherein PEI is more preferably less than 1 bar(abs).

Preferably, PEI is in the range of from 10 to 900 mbar(abs), more preferably in the range of from 10 to 850 mbar(abs), more preferably in the range of from 10 to 800 mbar(abs). Preferably, the evaporation conditions according to (iii) further comprise a residence time tei in the evaporation unit Ei, wherein tei is in the range of from 1 min to 5 h, more preferably in the range of from 5 min to 4 h, more preferably in the range of from 10 min to 3 h. More preferably, the evaporation conditions according to (iii) comprise an evaporation temperature TEI of the mixture ME, wherein TEI is in the range of from 200 to 270 °C, more preferably in the range of from 210 to 270 °C, more preferably in the range of from 220 to 270 °C; the evaporation conditions according to (iii) further comprise an evaporation pressure PEI , wherein PEI is more preferably less than 1 bar(abs), more preferably in the range of from 10 to 900 mbar(abs), more preferably in the range of from 10 to 850 mbar(abs), more preferably in the range of from 10 to 800 mbar(abs); and the evaporation conditions according to (iii) further comprise a residence time tEi in the evaporation unit Ei, wherein tsi is in the range of from 1 min to 5 h, more preferably in the range of from 5 min to 4 h, more preferably in the range of from 10 min to 3 h.

Preferably, according to (iv), the stream SLI is divided into the first stream SLU and the second stream SM2 at a mass ratio m(SM2): m(SLn) in the range of from 0.01 :1 to 0.02:1.

Preferably, the downstream treatment stage according to (v) comprises one or more of an evaporation unit; a depolymerization unit for depolymerizing at least one of the at least one e-caprolactam oligomeric compound CPO comprised in the stream S1.12; a separation unit for separating at least one solid residue from the stream SL-I 2; a processing unit for processing at least one solid residue comprised in the stream SL-I 2; an incineration stage for incinerating at least one solid residue comprised in the stream SL12-

Preferably, the downstream treatment stage according to (v) comprises an evaporation unit and the process further comprises

(vi) subjecting the stream S1.12 to evaporation conditions in an evaporation unit E2, obtaining an aqueous vapor stream Sv2 and a liquid stream SL2 wherein Sv2 comprises CPM at a concentration Cv2(CPM) with Cv2(CPM) > CM2(CPM), and CPO at a concentration Cv2(CPO) with c _V2 (CPO) < CM2(CPO); wherein SL2 comprises the at least one CPO at a concentration CL2(CPO) with CL2(CPO) > CM2(CPO);

(vii) passing the stream SL2 obtained according to (vi) to a downstream treatment stage.

The liquid stream SL2 is preferably a non-aqueous liquid stream, i.e. a liquid stream having a water content of at most 0.01 weight-%, preferably of at most 0.005 weight-%, preferably of most 0.002 weight-%, more preferably of at most 0.001 weight-%.

Preferably, the stream Sv2 obtained according to (vi) exhibits a CPM concentration in the range of from 50 to 100 weight-%, more preferably in the range of from 60 to 100 weight-%, more preferably in the range of from 80 to 100 weight-%, and a CPO concentration in the range of from 0 to 0.5 weight-%, more preferably in the range of from 0 to 0.3 weight-%, more preferably in the range of from 0 to 0.1 weight-%; the stream SL2 obtained according to (vi) exhibits a CPO concentration in the range of from 1 to 10 weight-%, more preferably in the range of from 1.5 to 10 weight-%, more preferably in the range of from 2 to 10 weight-%.

Preferably the evaporation in the evaporation unit E2 according to (vi) is carried out in one or more stirred vessels, or in one or more film evaporators, or in one or more stirred vessels and in one or more film evaporators. More preferably the evaporation in the evaporation unit E2 according to (vi) is carried out in one or more film evaporators. More preferably the evaporation in the evaporation unit E2 according to (vi) is carried out in one or more wipe film evaporators, wherein more preferably, if evaporation in E2 is carried out in more than one wipe film evaporators, the wipe film evaporators are arranged in parallel.

It is conceivable that the evaporation in the evaporation unit E2 according to (vi) be carried out in one or more kneaders.

Preferably the one or more stirred vessels and the one or more film evaporators are equipped with heating means to indirectly providing heat for the evaporation carried out in E2, the process comprising passing a heating medium through said heating means, wherein said heating means are more preferably heating jackets.

Preferably the evaporation conditions according to (vi) comprise an evaporation temperature TE2 of the stream S1.12, wherein TE2 is in the range of from 200 to 300 °C, more preferably in the range of from 215 to 300 °C, more preferably in the range of from 230 to 300 °C, and the evaporation conditions according to (vi) further comprise an evaporation pressure PE2, wherein PE2 is more preferably less than 1 bar(abs).

Preferably, PE2 is in the range of from 10 to 900 mbar(abs), more preferably in the range of from 10 to 850 mbar(abs), more preferably in the range of from 10 to 800 mbar(abs).

Preferably, the evaporation conditions according to (vi) further comprise a residence time tE2 in the evaporation unit E2, wherein tE2 is in the range of from 1 s to 5 min, more preferably in the range of from 5 s to 4 min, more preferably in the range of from 10 s to 3 min. More preferably, the evaporation conditions according to (vi) comprise an evaporation temperature TE2 of the stream S1.12, wherein TE2 is in the range of from 200 to 300 °C, more preferably in the range of from 215 to 300 °C, more preferably in the range of from 230 to 300 °C; the evaporation conditions according to (vi) further comprise an evaporation pressure PE2, wherein PE2 is more preferably less than 1 bar(abs), more preferably in the range of from 10 to 900 mbar(abs), more preferably in the range of from 10 to 850 mbar(abs), more preferably in the range of from 10 to 800 mbar(abs); and the evaporation conditions according to (vi) further comprise a residence time tE2 in the evaporation unit E2, wherein tE2 is in the range of from 1 s to 5 min, more preferably in the range of from 5 s to 4 min, more preferably in the range of from 10 s to 3 min.

Preferably, the downstream treatment stage according to (vii) comprises one or more of a depolymerization unit for depolymerizing at least one of the at least one e-caprolactam oligomeric compound CPO comprised in the stream S1.2; a separation unit for separating at least one solid residue from the stream SL.2; a processing unit for processing at least one solid residue comprised in the stream SL.2; an incineration stage for incinerating at least one solid residue comprised in the stream SL2.

Preferably, the process further comprises

(viii) passing the aqueous vapor stream Svi, more preferably the aqueous vapor stream Svi and the aqueous vapor stream Sv2, more preferably a combined stream of the aqueous vapor stream Svi and the aqueous vapor stream Sv2, to a water removal unit Wu for separating CPM from water, wherein the water removal unit more preferably comprises at least one distillation column, more preferably from 1 to 3 distillation columns, more preferably 2 or 3 distillation columns, more preferably 3 distillation columns, wherein, if the water removal unit Wu comprises more than one distillation column, the distillation columns are more preferably serially arranged.

Preferably, the bottoms stream of at least one distillation column, more preferably the bottoms stream of the downstream-most distillation column, is recycled into the evaporation unit E1.

Preferably providing the stream SR according to (i) comprises

(i.1 ) preparing an aqueous liquid mixture Mwc containing CPM dissolved in water and CPO, comprising

(i.1.1 ) providing an aqueous liquid stream Sw;

(i.1 .2) providing a solid material M containing a polyamide prepared from e-caprolactam;

(i.1 .3) preparing a mixture of the solid material M provided according to (i .1 .2) and the aqueous liquid stream Sw provided according to (i.1.1 );

(1.1 .4) preparing an aqueous liquid mixture MWP comprising the polyamide dissolved in water from the mixture prepared according to (i.1 .3);

(1.1 .5) subjecting the aqueous liquid mixture M P prepared according to (i.1 .4) to depolymerization conditions in a chemical reactor unit Ru, obtaining the aqueous liquid mixture Mwc comprising CPM dissolved in water and CPO;

(1.2) optionally subjecting the aqueous mixture Mwc obtained according to (i.1 .5) to depressurization in a depressurization unit Du, obtaining an aqueous vapor stream Svo and an aqueous liquid stream Sc, Sc comprising CPM dissolved in water and CPO;

(1.3) optionally passing the aqueous mixture Mwc obtained according to (i.1 .5) or the aqueous liquid stream Sc, obtained according to (i.2) to solid-liquid separation in a solid-liquid separation unit SLu, obtaining an aqueous liquid stream SL comprising CPM dissolved in water and CPO; (1.4) separating water from the aqueous liquid mixture Mwc obtained according to (i.1.5), or from the aqueous liquid stream Sc obtained according to (i.2), or from the aqueous liquid stream SL obtained according to (i.3), by evaporation in an evaporation unit Eu comprising least two evaporation sub-units Eui and Eu2, obtaining at least one aqueous vapor stream SVE and the aqueous liquid stream SR.

Preferably the solid material M provided according to (i.1.2) comprises, more preferably consists of waste material, wherein said waste material more preferably comprises textile waste material.

Preferably, preparing an aqueous liquid stream Swc containing e-caprolactam dissolved in water according to (i.1 ) comprises

(i.1 .1) providing an aqueous liquid stream Sw, wherein from 50 weight- % to 100 weight- % of Sw consist of water and wherein Sw has a temperature Tsw, wherein TSW>TP;

(i.1 .2) providing a solid material M containing the polyamide prepared from e-caprolactam, M having a temperature TM, wherein TM<TP,TP being the melting point of the polyamide;

(i.1 .3) preparing an aqueous mixture of the solid material M provided according to (i.1 .2) and the aqueous liquid stream Sw provided according to (i.1.1), comprising feeding the solid material M provided according to (i.1 .2) and the liquid aqueous stream Sw provided according to (i.1.1) into a chemical reactor unit Ru obtaining said mixture;

(1.1 .4) preparing an aqueous liquid mixture MWP comprising the polyamide dissolved in water from the mixture prepared according to (i.1 .3), comprising feeding the solid material M provided according to (i.1.2) and the liquid aqueous stream Sw provided according to (i.1.1) into a chemical reactor unit Ru obtaining said mixture;

(1.1 .5) subjecting the aqueous liquid mixture prepared according to (i.1 .4) to depolymerization conditions in a chemical reactor unit Ru, obtaining the aqueous liquid stream Mwc containing e-caprolactam dissolved in water, wherein the depolymerization conditions comprise a depolymerization temperature TD at a depolymerization pressure PD, wherein TM<TD<TSW.

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

Preferably, Tsw is in the range of from 250 to 350 °C, more preferably in the range of from 260 to 330 °C, more preferably in the range of from 290 to 325 °C.

The excess heat from the liquid aqueous stream Sw (Tsw) melts the solid material M containing the polyamide, the solid material M preferably being in the form of granules, and provides the needed reaction enthalpy. Any additional heat required to maintain the reaction temperature can be provided through a heating jacket using hot oil of the reactor unit Ru. This is detailed in the following. Preferably, AT=TSW-TP is in the range of from 10 to 70 °C, more preferably in the range of from 10 to 50 °C, more preferably in the range of from 10 to 30 °C.

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

Preferably, in the mixture prepared according to (i.1 .3), at least 75 weight-%, more preferably from 75 to 100 weight-%, more preferably from 85 to 100 weight-%, more preferably from 95 to 100 weight-%, of the polyamide comprised in the solid material M are comprised in liquid form.

Preferably, from 91 to 100 weight-%, more preferably from 92 to 100 weight-%, more preferably from 95 to 100 weight-% of Sw provided according to (i.1 .1) consist of water.

Preferably, the solid material M provided according to (i .1 .2) comprises, more preferably consists of waste material, wherein said waste material more preferably comprises textile waste material.

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

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

According to (i.1.4), M and Sw are preferably fed into Ru at a mixing ratio mw/kg : mp/kg, defined as the amount of water contained in Si, mw, relative to the mass of polyamide contained in M, mp, in the range of from 1 :1 to 20:1 , more preferably in the range of from 2:1 to 15:1 , more preferably in the range of from 5:1 to 10:1 .

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

Preferably, z>1 and at least two reactors R, more preferably the z reactors R are serially coupled.

Preferably, the z reactors R are serially coupled, wherein according to (i.1.4), MWP is fed into R, i=1 ; an aqueous liquid stream Si containing e-caprolactam dissolved in water is removed from Ri and fed into R+i, i<z; according to (i.1.5), Mwc is removed from R _z ; wherein in every reactor R, a depolymerization temperature TDI at a depolymerization pressure poi are maintained, wherein, independently of each other, TDI is in the range of from 230 to 320 °C, more preferably in the range of from 250 to 300 °C, more preferably in the range of from 270 to 295 °C, and wherein, independently of each other, poi is more preferably in the range of from 40 to 120 bar, more preferably in the range of from 50 to100 bar, more preferably in the range of from 60 to 90 bar.

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

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

Preferably, at least 1 , more preferably z reactors R, are configured as non-stirred reactors or as non-circulation reactors, more preferably as non-stirred reactors and non-circulation reactors. The system is preferably operated without stirrer and without circulation pump. That avoids difficult sealings, i.e. high pressure sealings, for the stirrer and pump.

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

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

Preferably, the residence time in one or more of the reactors Ri to R _y .i, more preferably in the reactors Ri to R _y .i, is in the range of from 5 to 40 minutes, more preferably in the range of from 10 to 30 minutes, more preferably in the range of from 15 to 25 minutes.

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

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

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

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

Preferably, subjecting the aqueous mixture Mwc obtained according to (i.1.5) to depressurization in a depressurization unit Du according to (i.2) comprises

(1.2.1 ) feeding the aqueous liquid stream Mwc as a feed stream to a first evaporation sub-unit DU11 , obtaining an aqueous vapor stream SVDH , and an aqueous liquid stream SLU comprising e-caprolactam dissolved in water; the aqueous liquid stream Mwc is optionally passed through at least one solid-liquid separation unit F1 ;

(1.2.2) feeding the aqueous liquid stream SLU as a feed stream to a second evaporation subunit DU 12, obtaining an aqueous vapor stream SVDI2, and the aqueous liquid stream Sc comprising e-caprolactam dissolved in water, the aqueous liquid stream SLU is optionally passed through at least one solid-liquid separation unit F2; wherein (ii.1) comprises at least one of passing Mwc through F1 and passing SLU through F2, wherein (ii.1) more preferably comprises passing Mwc through F1 and passing SLU through F2. This is in particular illustrated in Figure 8. The combination of SVDH and SVDI 2 corresponds to Svo.

Preferably, at least one of the solid-liquid separation unit F1 and the solid-liquid separation unit F2, more preferably the solid-liquid separation unit F1 and the solid-liquid separation unit F2 are filtration units, wherein F1 more preferably has a mesh size in the range of from 0.5 to 5 mm, more preferably in the range of from 1 to 3 mm, and F2 more preferably has a mesh size in the range of from 0.5 to 5 mm, more preferably in the range of from 1 to 3 mm.

Preferably, according to (i.4), the at least two evaporation sub-units Eui and Eu2 are serially coupled, wherein an aqueous vapor stream SVEI is obtained from Eui and an aqueous vapor stream SVE2 is obtained from Eu2, and wherein from Eu2, an aqueous liquid stream SR comprising e-caprolactam dissolved in water is obtained; more preferably the evaporation unit Eu comprises two evaporation units Eui and Eu2, wherein preferably from 75 to 100 weight- % of the aqueous liquid stream which is fed to evaporation according to (i.4) consist of water and e-caprolactam, said stream exhibiting a water concentration CH20 and preferably having a concentration of e-caprolactam CCPL in the range of from 5 to 20 weight-%; the process further comprising recycling at least a part of at least one of streams SVEI and SVE2 as a component of the aqueous liquid stream Sw, said recycling preferably comprising condensing the at least one of streams SVEI and SVE2. The combination of SVEI and SVE2 corresponds to SVE.

Preferably, according to (vii), passing the liquid stream SL2 to a downstream treatment stage comprises

(vii.1 ) dividing the stream SL2 into a first stream SL2I and a second stream SL.22, wherein S1.21 and SL.22 have the same chemical composition as SL2;

(vii.2) recycling the stream SL21 into the chemical reactor unit Ru according to (i.1.5);

(vii.3) passing the stream SL22 to a downstream treatment stage.

Preferably, the downstream treatment stage according to (vii.3) comprises one or more of a separation unit for separating at least one solid residue from the stream SL22; a processing unit for processing at least one solid residue comprised in the stream SL22; an incineration stage for incinerating at least one solid residue comprised in the stream SL22-

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

1 . A process for separating at least one e-caprolactam oligomeric compound CPO from a stream SR comprising said at least one CPO and e-caprolactam monomeric compound CPM, the process comprising

(i) providing an aqueous liquid stream S comprising CPM dissolved in water at a concentration CR(CPM), CPM having a boiling point TCPM, wherein SR further comprises the at least one CPO at a concentration CR(CPO), CPO having a boiling point TCPO with TCPO ^> TCPM!

(ii) preparing an aqueous liquid mixture ME comprising the stream SR provided according to (i);

(iii) subjecting the mixture ME according to (i) to evaporation conditions in an evaporation unit E1, obtaining an aqueous vapor stream Svi and an aqueous liquid stream SLI , wherein Svi comprises CPM at a concentration Cvi(CPM) with Cvi(CPM) > CR(CPM), wherein SLI comprises the at least one CPO at a concentration CM CPO) with CLI(CPO) > CR(CPO) and comprises CPM at a concentration CM CPM) with CM CPM) < CR(CPM); (iv) dividing the stream SLI according to (iii) into a first stream SLU and a second stream SLI2, wherein SLU and SLI2 have the same chemical composition as SLI ;

(v) passing the stream SLI2 obtained according to (iv) to a downstream treatment stage; wherein preparing the aqueous liquid mixture ME according to (ii) comprises mixing the stream SR with the stream SLU .

2. The process of embodiment 1 , wherein the stream S provided according to (i) has a temperature in the range of from 100 to 150 °C, preferably in the range of from 110 to 145 °C, more preferably in the range of from 120 to 140 °C.

3. The process of embodiment 1 or 2, wherein the stream SR provided according to (i) exhibits a CPM concentration in the range of from 15 to 90 weight-%, preferably in the range of from 20 to 75 weight-%, more preferably in the range of from 25 to 60 weight-%; and a CPO concentration in the range of from 0.5 to 10 weight-%, preferably in the range of from 0.5 to 7 weight- %, more preferably in the range of from 0.5 to 4 weight-%; wherein the stream Svi obtained according to (iii) exhibits a CPM concentration in the range of from 65 to 99 weight-%, preferably in the range of from 65 to 90 weight-%, more preferably in the range of from 65 to 80 weight-%; wherein the stream Svi obtained according to (iii) preferably exhibits a CPO concentration in the range of from 0 to 0.4 weight-%, preferably in the range of from 0 to 0.3 weight-%, more preferably in the range of from 0 to 0.2 weight-%; wherein the stream SLI obtained according to (iii) exhibits a CPM concentration in the range of from 0.1 to 10 weight-%, preferably in the range of from 0.5 to 7.5 weight-%, more preferably in the range of from 1 to 5 weight-%; and a CPO concentration in the range of from 1 to 10 weight-%, preferably in the range of from 1 .5 to 10 weight-%, more preferably in the range of from 2 to 10 weight-%.

4. The process of any one of embodiments 1 to 3, wherein preparing the aqueous liquid mixture ME according to (ii) further comprises, prior to mixing the stream SR with the stream SLU , heating the stream SLU obtained from (iv) to a temperature in the range of from 200 to 270 °C, preferably in the range of from 210 to 270 °C, more preferably in the range of from 220 to 270 °C.

5. The process of embodiment 4, wherein heating the stream SLU comprises passing the stream SLU through a heat exchanger Hi.

6. The process of embodiment 4 or 5, wherein according to (ii), the stream SR provided according to (i) and the stream SLU obtained from heating are mixed in the evaporation unit Ei.

7. The process of any one of embodiments 4 to 6, wherein prior to mixing the stream SR with the stream SLU , the stream SR provided according to (i) is not heated.

8. The process of any one of embodiments 1 to 3, wherein preparing the aqueous liquid mixture ME according to (ii) comprises mixing the stream S provided according to (i) with the stream SLU obtained from (iv) and heating the combined stream to a temperature in the range of from 200 to 270 °C, preferably in the range of from 210 to 270 °C, more preferably in the range of from 220 to 270 °C.

9. The process of embodiment 8, wherein heating the combined stream comprises passing the stream SLU through a heat exchanger Hi.

10. The process of embodiment 8 or 9, wherein prior to mixing the stream SR with the stream SLU , the stream SR provided according to (i) is not heated.

11 . The process of any one of embodiments 1 to 10, wherein the evaporation in the evaporation unit Ei according to (iii) is carried out in one or more stirred vessels, or in one or more film evaporators, or in one or more stirred vessels and in one or more film evaporators; wherein the evaporation in the evaporation unit Ei according to (iii) is preferably carried out in one or more continuous stirred-tank reactors, or in one or more falling film evaporators, or in one or more continuous stirred-tank reactors and in one or more falling film evaporators; wherein the evaporation in the evaporation unit Ei according to (iii) is more preferably carried out in one or more continuous stirred-tank reactors, wherein more preferably, if evaporation in Ei is carried out in more than one continuous stirred-tank reactors, the continuous stirred-tank reactor are arranged in parallel.

12. The process of embodiment 11 , wherein the one or more stirred vessels and the one or more film evaporators are equipped with heating means to indirectly providing heat for the evaporation carried out in Ei, the process comprising passing a heating medium through said heating means, wherein said heating means are preferably heating jackets.

13. The process of any one of embodiments 1 to 12, preferably of embodiment 11 or 12, wherein the evaporation conditions according to (iii) comprise an evaporation temperature TEI of the mixture ME, wherein TEI is in the range of from 200 to 270 °C, preferably in the range of from 210 to 270 °C, more preferably in the range of from 220 to 270 °C, and wherein the evaporation conditions according to (iii) further comprise an evaporation pressure PEI , wherein PEI is preferably less than 1 bar(abs).

14. The process of embodiment 13, wherein PEI is in the range of from 10 to 900 mbar(abs), preferably in the range of from 10 to 850 mbar(abs), more preferably in the range of from 10 to 800 mbar(abs).

15. The process of any one of embodiments 1 to 14, preferably of any one of embodiments 11 to 14, wherein the evaporation conditions according to (iii) further comprise a residence time tei in the evaporation unit Ei , wherein tei is in the range of from 1 min to 5 h, preferably in the range of from 5 min to 4 h, more preferably in the range of from 10 min to 3 h.

16. The process of any one of embodiments 1 to 15, wherein according to (iv), the stream SLI is divided into the first stream SLU and the second stream SM2 at a mass ratio m(SM2): m(SLn) in the range of from 0.01 :1 to 0.02:1.

17. The process of any one of embodiments 1 to 16, wherein the downstream treatment stage according to (v) comprises one or more of an evaporation unit; a depolymerization unit for depolymerizing at least one of the at least one E- caprolactam oligomeric compound CPO comprised in the stream S1.12; a separation unit for separating at least one solid residue from the stream S1.12; a processing unit for processing at least one solid residue comprised in the stream SL12; an incineration stage for incinerating at least one solid residue comprised in the stream S1.12.

18. The process of any one of embodiments 1 to 17, wherein the downstream treatment stage according to (v) comprises an evaporation unit, the process further comprising

(vi) subjecting the stream S1.12 to evaporation conditions in an evaporation unit E2, obtaining an aqueous vapor stream Sv2 and a liquid stream SL2 wherein Sv2 comprises CPM at a concentration Cv2(CPM) with Cv2(CPM) > CLI2(CPM), and CPO at a concentration Cv2(CPO) with Cv2(CPO) < CM2(CPO); wherein SL2 comprises the at least one CPO at a concentration CL2(CPO) with CL2(CPO) > CM2(CPO);

(vii) passing the stream SL2 obtained according to (vi) to a downstream treatment stage.

19. The process of embodiment 18, wherein the stream Sv2 obtained according to (vi) exhibits a CPM concentration in the range of from 50 to 100 weight-%, preferably in the range of from 60 to 100 weight-%, more preferably in the range of from 80 to 100 weight-%; and a CPO concentration in the range of from 0 to 0.5 weight-%, preferably in the range of from 0 to 0.3 weight-%, more preferably in the range of from 0 to 0.1 weight-%; wherein the stream SL2 obtained according to (vi) exhibits a CPO concentration in the range of from 1 to 10 weight-%, preferably in the range of from 1.5 to 10 weight-%, more preferably in the range of from 2 to 10 weight-%.

20. The process of embodiment 18 or 19, wherein the evaporation in the evaporation unit E2 according to (vi) is carried out in one or more stirred vessels, or in one or more film evaporators, or in one or more stirred vessels and in one or more film evaporators; wherein the evaporation in the evaporation unit E2 according to (vi) is preferably carried out in one or more film evaporators; wherein the evaporation in the evaporation unit E2 according to (vi) is more preferably carried out in one or more wipe film evaporators, wherein more preferably, if evaporation in E2 is carried out in more than one wipe film evaporators, the wipe film evaporators are arranged in parallel. The process of embodiment 20, wherein the one or more stirred vessels and the one or more film evaporators are equipped with heating means to indirectly providing heat for the evaporation carried out in E2, the process comprising passing a heating medium through said heating means, wherein said heating means are preferably heating jackets. The process of any one of embodiments 18 to 21 , wherein the evaporation conditions according to (vi) comprise an evaporation temperature TE2 of the stream S1.12, wherein TE2 is in the range of from 200 to 300 °C, preferably in the range of from 215 to 300 °C, more preferably in the range of from 230 to 300 °C, and wherein the evaporation conditions according to (vi) further comprise an evaporation pressure PE2, wherein PE2 is preferably less than 1 bar(abs). The process of embodiment 22, wherein PE2 is in the range of from 10 to 900 mbar(abs), preferably in the range of from 10 to 850 mbar(abs), more preferably in the range of from 10 to 800 mbar(abs). The process of any one of embodiments 18 to 23, wherein the evaporation conditions according to (vi) further comprise a residence time tE2 in the evaporation unit E2, wherein tE2 is in the range of from 1 s to 5 min, preferably in the range of from 5 s to 4 min, more preferably in the range of from 10 s to 3 min. The process of any one of embodiments 18 to 24, wherein the downstream treatment stage according to (vii) comprises one or more of a depolymerization unit for depolymerizing at least one of the at least one E- caprolactam oligomeric compound CPO comprised in the stream S1.2; a separation unit for separating at least one solid residue from the stream SL.2; a processing unit for processing at least one solid residue comprised in the stream SL2; an incineration stage for incinerating at least one solid residue comprised in the stream SL.2. The process of any one of embodiments 1 to 25, preferably of any one of embodiments 18 to 25, the process further comprising

(viii) passing the aqueous vapor stream Svi, preferably the aqueous vapor stream Svi and the aqueous vapor stream Sv2, more preferably a combined stream of the aqueous vapor stream Svi and the aqueous vapor stream Sv2, to a water removal unit Wu for separating CPM from water, wherein the water removal unit preferably comprises at least one distillation column, more preferably from 1 to 3 distillation columns, more preferably 2 or 3 distillation columns, more preferably 3 distillation columns, wherein, if the water removal unit Wu comprises more than one distillation column, the distillation columns are preferably serially arranged.

27. The process of embodiment 26, wherein the bottoms stream of at least one distillation column, preferably the bottoms stream of the downstream-most distillation column is recycled into the evaporation unit Ei.

28. The process of any one of embodiments 1 to 27, wherein providing the stream SR according to (i) comprises

(i.1 ) preparing an aqueous liquid mixture Mwc containing CPM dissolved in water and CPO, comprising

(i.1.1) providing an aqueous liquid stream Sw;

(i.1 .2) providing a solid material M containing a polyamide prepared from E- caprolactam;

(i.1 .3) preparing a mixture of the solid material M provided according to (i.1 .2) and the aqueous liquid stream Sw provided according to (i.1.1);

(1.1 .4) preparing an aqueous liquid mixture MWP comprising the polyamide dissolved in water from the mixture prepared according to (i.1 .3);

(1.1 .5) subjecting the aqueous liquid mixture M P prepared according to (i.1 .4) to depolymerization conditions in a chemical reactor unit Ru, obtaining the aqueous liquid mixture Mwc comprising CPM dissolved in water and CPO;

(1.2) optionally subjecting the aqueous mixture Mwc obtained according to (i.1.5) to depressurization in a depressurization unit Du, obtaining an aqueous vapor stream Svo and an aqueous liquid stream Sc, Sc comprising CPM dissolved in water and CPO;

(1.3) optionally passing the aqueous mixture Mwc obtained according to (i.1.5) or the aqueous liquid stream Sc, obtained according to (i.2) to solid-liquid separation in a solid-liquid separation unit SLu, obtaining an aqueous liquid stream SL comprising CPM dissolved in water and CPO;

(1.4) separating water from the aqueous liquid mixture Mwc obtained according to (i.1 .5) or from the aqueous liquid stream Sc obtained according to (i.2) or from the aqueous liquid stream SL obtained according to (i.3) by evaporation in an evaporation unit Eu comprising least two evaporation sub-units Eui and Eu2, obtaining at least one aqueous vapor stream SVE and the aqueous liquid stream S .

29. The process of embodiment 28, wherein the solid material M provided according to (i.1.2) comprises, preferably consists of waste material, wherein said waste material preferably comprises textile waste material.

30. The process of embodiment 28 or 29 insofar as embodiments 28 or 29 are dependent on any one of embodiments 18 to 25, wherein according to (vii), passing the liquid stream SL2 to a downstream treatment stage comprises

(vii.1 ) dividing the stream SL2 into a first stream SL2I and a second stream SL.22, wherein

SL21 and SL.22 have the same chemical composition as SL2;

(vii.2) recycling the stream SL21 into the chemical reactor unit according to (i.1.5);

(vii.3) passing the stream SL22 to a downstream treatment stage.

31 . The process of embodiment 30, wherein the downstream treatment stage according to (vii.3) comprises one or more of a separation unit for separating at least one solid residue from the stream SL22; a processing unit for processing at least one solid residue comprised in the stream SL22; an incineration stage for incinerating at least one solid residue comprised in the stream SL22.

In the context of the present invention, it is noted that the term „polyamide prepared from £-caprolactam“ as used herein refers to „polyamide 6“ being characterized by the formula (— N H— (CH2)s— CO— ) _n . In the context of the present invention, an e-caprolactam monomeric compound CPM is an e-caprolactam monomer. The term „bar“ as used in the context of the present invention refers to „bar(abs)”, i.e. bar (absolute), sometimes also referred to “bara”.

The term “textile material” covers textile raw materials and non-textile raw materials that are processed by various methods into linear, planar and spatial structures. It concerns the linear textile structures produced from them, such as yarns, twisted yarns and ropes, the sheet-like textile structures, such as woven fabrics, knitted fabrics, braids, stitch-bonded fabrics, nonwovens and felts, and the three-dimensional textile structures, i.e. body structures, such as textile hoses, stockings or textile semi-finished products; and it further concerns those finished products which, using the aforementioned products, are brought into a saleable condition by making up, opening up and/or other operations for onward transmission to the processor, the trade or the end consumer.

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

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

Description of the figures

Figure 1 is a schematic representation of a production unit used for the process according to preferred embodiments of the invention

The production unit comprises an evaporation unit Ei, a dividing means D and a mixing means M. An aqueous liquid stream SR comprising CPM dissolved in water at a concentration CR(CPM), CPM having a boiling point TCPM, wherein S further comprises the at least one CPO at a concentration CR(CPO), CPO having a boiling point TCPO with TCPO > TCPM is admixed with a stream SLU , obtaining the aqueous liquid mixture ME. The aqueous liquid mixture ME is fed to evaporation conditions into the evaporation unit Ei, obtaining an aqueous vapor stream Svi and an aqueous liquid stream SLI . Svi comprises CPM at a concentration Cvi(CPM) with Cvi(CPM) > CR(CPM). SM comprises the at least one CPO at a concentration CM(CPO) with CM(CPO) > CR(CPO) and comprises CPM at a concentration CM(CPM) with CM(CPM) < CR(CPM). The aqueous liquid stream SLI is divided in two streams SLU and SLI2. SLU and SLI2 have the same chemical composition as SLI . The aqueous liquid stream SLi2 is passed through a downstream treatment not shown in Figure 1 and the aqueous liquid stream SLU is recycled and mixed with SR.

Figure 2 is a schematic representation of a production unit used for the process according to preferred embodiments of the invention

As in Figure 1 , the production unit comprises an evaporation unit Ei and a dividing means D. However, compared to Figure 1 , the production unit further comprises a heat exchanger Hi and does not comprise a mixing means M. The aqueous liquid stream SR is fed into the evaporation unit Ei and the aqueous liquid stream SLU , prior to be recycled as a feed component into Ei, is passed through Hi for heating. ME is thus formed in Ei. Apart from said differences, the process illustrated in Figure 2 is carried out as the one illustrated in Figure 1.

Figure 3 is a schematic representation of a production unit used for the process according to preferred embodiments of the invention

The process illustrated by Figure 3 represents an alternative to the process illustrated by Figure 2. As in Figure 1 , the production unit comprises an evaporation unit Ei, a dividing means D and a mixing means M. However, compared to Figure 1 , the production unit further comprises a heat exchanger Hi, said heat exchanger Hi is positioned downstream of the mixing means M and upstream of Ei. Thus, Hi heats the combined streams, preferably to a temperature in the range of from 200 to 270 °C, more preferably in the range of from 210 to 270 °C, more preferably in the range of from 220 to 270 °C. Apart from said differences, the process illustrated in Figure 3 is carried out as the one illustrated in Figure 1 .

Figure 4 is a schematic representation of a production unit used for the process according to preferred embodiments of the invention

As in Figure 3, the production unit comprises an evaporation unit Ei, a dividing means D, a mixing means M and a heat exchanger Hi. However, compared to Figure 3, the production unit further comprises a second evaporation unit E2. The aqueous liquid stream S1.12 is fed to evaporation conditions in the second evaporation unit E2, obtaining an aqueous vapor stream Sv2 and a liquid stream SL2. SV2 comprises CPM at a concentration Cv2(CPM) with Cv2(CPM) > CM2(CPM), and CPO at a concentration Cv2(CPO) with Cv2(CPO) < CM2(CPO). SL2 comprises the at least one CPO at a concentration CL2(CPO) with CL2(CPO) > CM2(CPO). The liquid stream SL2 is passed through a downstream treatment stage not shown in Figure 4. Apart from said differences, the process illustrated in Figure 4 is carried out as the one illustrated in Figure 3.

Figure 5 is a schematic representation of a production unit used for the process according to preferred embodiments of the invention

As in Figure 4, the production unit comprises an evaporation unit Ei, a dividing means D, a mixing means M, a heat exchanger Hi and a second evaporation unit E2. However, compared to Figure 4, the production unit further comprises a water removal unit Wu for separating CPM from water. The water removal unit Wu comprises 3 distillation columns serially arranged. The bottoms stream of the downstream-most distillation column is recycled into the evaporation unit Ei. The aqueous vapor stream Svi and the aqueous vapor stream Sv2 are mixed and the combined stream is passed through the water removal unit Wu. Apart from said differences, the process illustrated in Figure 5 is carried out as the one illustrated in Figure 4.

Figure 6 is a schematic representation of a production unit used for the process according to preferred embodiments of the invention

As in Figure 5, the production unit comprises an evaporation unit Ei, a dividing means D, a mixing means M, a heat exchanger Hi, a second evaporation unit E2 and a water removal unit Wu for separating CPM from water. However, compared to Figure 5, the production unit further comprises, upstream of M and Ei, a chemical reactor unit Ru, a depressurization unit Du, a solidliquid separation in a solid-liquid separation unit SLu and an evaporation unit Eu comprising least two evaporation sub-units Eui and Eu2. A solid material M containing a polyamide prepared from e-caprolactam and an aqueous liquid stream S are fed to depolymerization conditions in a chemical reactor unit Ru, obtaining the aqueous liquid mixture Mwc comprising CPM dissolved in water and CPO. The aqueous liquid mixture Mwc is passed through a depressurization unit Du, obtaining an aqueous vapor stream SVD and an aqueous liquid stream Sc. Sc comprising CPM dissolved in water and CPO. The aqueous liquid stream Sc is subjected to solid-liquid separation by passing through the solid-liquid separation unit SLu, obtaining an aqueous liquid stream SL comprising CPM dissolved in water and CPO. Then, water is separated from aqueous liquid stream SL by evaporation in Eu comprising Eui and Eu2, obtaining an aqueous vapor stream SVE and the aqueous liquid stream SR. The aqueous liquid stream S is then treated as in the process illustrated in Figure 5.

Figure 7 is a schematic representation of a production unit used for the process according to preferred embodiments of the invention

As in Figure 6, the production unit comprises an evaporation unit Ei, a dividing means D, a mixing means M, a heat exchanger Hi, a second evaporation unit E2 and a water removal unit Wu for separating CPM from water and the production unit further comprises, upstream of M and E1, a chemical reactor unit Ru, a depressurization unit Du, a solid-liquid separation in a solid-liquid separation unit SLu and an evaporation unit Eu comprising two evaporation sub-units Eui and EU2. The process illustrated in Figure 7 is run as the process illustrated in Figure 6 except that the liquid stream SL2 is divided in two streams, a first stream SL21 and a second stream SL22. SL2I and SL22 have the same chemical composition as SL2. The stream SL21 is recycled as a component of the aqueous liquid stream Sw. The liquid stream SL22 is passed through a downstream treatment stage not shown in Figure 7.

Figure 8 is a schematic representation of a portion of the production unit used for the process according to preferred embodiments of the invention, namely the portion which provides SR

Said portion of the production unit comprises a reactor unit Ru, a depressurization unit Du, a solid-liquid separation unit SLU and an evaporation unit E1 comprising two evaporation sub-units Eui and Eu2, said two units are serially coupled as shown in Figure 8. The solid material M comprising the polyamide and an aqueous liquid stream Sw are fed into the reactor unit Ru and subjected to depolymerization conditions comprising a depolymerization temperature TD at a depolymerization pressure po as detailed in the foregoing. An aqueous liquid stream Mwc is removed from the bottom of Ru, Mwc comprising e-caprolactam dissolved in water. The aqueous liquid stream Mwc is fed into the depressurization unit Du obtaining an aqueous vapor stream SVD, and an aqueous liquid stream Sc comprising e-caprolactam dissolved in water. The aqueous vapor stream SVD is recycled as a component of the aqueous liquid stream Sw, preferably after at least partial condensation. The aqueous liquid stream Sc is passed through the solid-liquid separation unit SLU obtaining an aqueous liquid stream SSLU comprising e-caprolactam dissolved in water. The aqueous liquid stream SL is then fed to evaporation in E1, in particular SL is fed to Eui. An aqueous vapor stream SVEI is obtained from Eui and an aqueous vapor stream SVE2 is obtained from Eu2. The aqueous vapor streams SVEI and SVE2 are recycled as a component of the aqueous liquid stream Sw, preferably via condensation. Further, an aqueous liquid stream SRI comprising c-caprolactam dissolved in water is removed from Eui and fed into Eu2 and an aqueous liquid stream SR comprising e-caprolactam dissolved in water is obtained and removed from EU2. The aqueous liquid stream S is then further treated as disclosed in the foregoing and illustrated in Figures 1-7.

Figure 9 is a schematic representation of a portion of the production unit used for the process according to preferred embodiments of the invention, namely the portion which provides SR

Said portion of the production unit comprises a reactor unit Ru, a depressurization unit Du, a solid-liquid separation unit SLU and an evaporation unit Ei comprising two evaporation sub-units Eui and Eu2, said two units are serially coupled as shown in Figure 9. The depressurization unit Du comprises a depressurization sub-unit DU 11 , a depressurization sub-unit DU 12 and two solidliquid separation units F1 and F2. The aqueous liquid stream Mwc removed from the bottom of Ru is passed through the solid-liquid separation unit F1 , preferably filtration unit F1 , wherein F1 preferably has a mesh size in the range of from 0.5 to 5 mm, more preferably in the range of from 1 to 3 mm, prior to being fed into the sub-unit DU11 to obtain an aqueous vapor stream SVDH , and an aqueous liquid stream SLDH comprising e-caprolactam dissolved in water. The aqueous liquid stream SLDH is then passed through the solid-liquid separation unit F2, preferably filtration unit F2, wherein F2 preferably has a mesh size in the range of from 0.5 to 5 mm, more preferably in the range of from 1 to 3 mm, prior to being fed into the second depressurization sub-unit DU 12, as a feed stream, to obtain an aqueous vapor stream SVDI2, and the aqueous liquid stream Sc comprising e-caprolactam dissolved in water. The aqueous vapor streams SVDH and SVDI2 are recycled as a component of the aqueous liquid stream Sw, preferably after at least partial condensation. Downstream of Du, the process is carried out as the process in Figure 8.