Energy-efficient method for producing a polymer

Abstract

The present invention relates to a method for processing a polar, aprotic solvent, the method in particular comprising a method step for separating a flow which contains H2O and solvent into a flow which contains water vapour and a gas flow which contains solvent, wherein the obtained flow which contains water vapour is recycled into the method itself after compression or serves as an energy source for heating a process flow of the same or another method. It has been found that, surprisingly, the amount of water vapour required can thereby be reduced, which leads to an energy saving and, as a result, the CO2 emissions of the method can also be reduced.

Description

Energy-efficient process for producing a polymer TECHNICAL AREA The present invention relates to an energy-efficient process for the work-up of a polar, aprotic solvent (e.g. NMP) which is used as a solvent for the production of a polymer. INTRODUCTION Polymers such as polyethersulfone (PESU), polysulfone (PSU), and polyphenylsulfone (PPSU) can be industrially produced by polycondensation to NMP (short for N-methyl-2-pyrrolidone, also known as 1-methylpyrrolidin-2-one). A large amount of steam is required to recover NMP and distill the mixture of NMP and water produced during the reaction. Often, the heat of condensation from the vapor is dissipated to cooling water, resulting in heat loss. CN 116947728 A relates to a process for recycling NMP by saving energy in a single tower, comprising the following steps: Step S1: Preheating NMP raw material, evaporating the NMP raw material, introducing the NMP-containing vapor phase into a rectification tower, and introducing the liquid phase into a distillation apparatus; Step S2: Using the vapor phase from the top of the rectification tower as a heat source for an evaporation apparatus after the vapor phase has been compressed and heated, wherein a portion of the vapor phase is drawn off after condensation, and a portion of the vapor phase is returned to the top of the rectification tower, the vapor phase comprising NMP, which is drawn off from the side line of the rectification tower, is used as a heat source for the evaporation apparatus and an evaporator of the rectification tower after it has been compressed and heated, yielding NMP after condensation;Step S3: Returning the vapor phase condensate from the distillation apparatus to the evaporation apparatus, and draining off the concentrated residual liquid. CN 219558744 U relates to an NMP rectification device in the polysulfone manufacturing process. The NMP rectification device comprises a rectification tower and an evaporator. The rectification tower is provided with an NMP extraction outlet for the high-purity gas phase in the side line. It is characterized in that the vapor outlet pipe at the upper end of the distillation tower is connected to a compressor, the outlet pipe of the compressor is connected to the inlet of the gas heat exchange channel of the evaporator, and the inlet of the liquid heat exchange channel of the evaporator is connected by the pump- The pipe of the tower boiler is connected. The liquid outlet of the tower is located at the bottom of the rectification tower, and the outlet pipe for the liquid heat exchange channel of the evaporator is connected to the return liquid inlet of the rectification tower. EP 4091688 A1 relates to a plant for purifying recovered NMP from lithium-ion battery production. According to claim 1, this plant comprises in particular a first column for separating low-boiling impurities, which has a feed for the recovered NMP in its central part, and a second column for separating high-boiling impurities. US 2018 / 171079 A1 relates to a process for the production of polyarylene sulfides, which, according to claim 1, in particular includes washing a polyarylene sulfide-containing mixture comprising an organic amide-based solvent with water. The vapor produced during the distillation of the water-solvent mixture is compressed, and the heat generated is used to operate the distillation. US 12005381 B2 relates to a system for the production of an anhydrous organic solvent, wherein the system includes distillation steps and a dehydration unit. Furthermore, this system includes mechanical vapor compression to recover heat from a distillation section. Against this background, it can be considered an object of the present invention to provide, in particular, a process for the work-up of a polar, aprotic solvent that can be used as a solvent for the production of a polymer, wherein the process is comparatively energy- and resource-efficient, and in particular enables robust and stable operation of the process. Furthermore, it can be considered an object of the present invention to provide an energy-efficient process for the production of a polymer that, in particular, has a comparatively lower demand for water vapor and, in particular, enables a reduction in CO2 emissions. DETAILED DESCRIPTION Surprisingly, it was discovered that by introducing a mechanical compressor, the steam generated during the processing of the solvent NMP could be used as a heating medium. Firstly, it was unexpectedly found that this steam could be used to heat and evaporate the mixture of water and NMP that is generated and processed in the subsequent processing step following the polycondensation. Secondly, it could be used to preheat a process stream or the water used for separating (and washing) the polymer in the process. This enabled the development of an energy-efficient process for processing a polar, aprotic solvent, which, in particular, has a comparatively lower energy consumption. has a need for water vapor, and in particular enables a reduction in CO2 emissions. Furthermore, it was surprisingly found that the use of compressed steam for heating the mixture obtained from the work-up, comprising water and NMP, can be made comparatively energy-efficient if, as shown in Example 2, a pressure increase from about 200 bara to 2.3 bara is achieved during steam compression, in contrast to a pressure increase to 12-16 bara, which would be required to heat the sump of the separation device. Therefore, the present invention relates to a process for the work-up of a polar, aprotic solvent, the process comprising (i) Reacting a reactant stream comprising an aromatic dihydroxy component, a bis(halophenyl)sulfone component, and a polar, aprotic solvent, under polycondensation conditions, obtaining a product stream comprising the polymer, the solvent, and optionally one or more salts, (ii) Provision of a fire-powered electricity S1 , (iii) Introducing the FW-containing stream S1 provided according to (ii) or the heated FW-containing stream S1 obtained from (vi.2) into the product stream obtained from (i) or (i.1) to separate the polymer, obtaining the polymer and an FW- and solvent-containing stream S2, (iv) Introducing the FW and solvent-containing stream S2 into a separation device, and separating the FW and solvent-containing stream S2 into a water vapor-containing stream S3 and a solvent-containing gas stream, (v) Compressing the water vapor-containing stream S3 obtained in (iv), obtaining a compressed water vapor-containing stream S4, (vi.1) Transferring heat from at least part of the compressed water vapor-containing stream S4 obtained in (v) to the FW and solvent-containing stream S2 obtained in (iii), obtaining an FW-containing stream S5 and a heated FW and solvent-containing stream S2, and / or (vi.2) optionally transferring heat from at least part of the compressed water vapor-containing stream S4 obtained from (v) to the FW and solvent-containing stream S2 introduced into the separation device according to (iv), Transferring heat from at least a part of the compressed water vapor-containing stream S4 obtained from (v) to the FW-containing stream S1 according to (ii), obtaining a, preferably liquid, FW-containing stream S6, and a heated FW-containing stream S1, and / or (vi.4) Transferring heat from at least part of the compressed steam-containing stream S4 obtained in (v) to a process stream, wherein the process stream is sub- different from the reactant stream according to (i) and the H2O- and solvent-containing stream S2 obtained in (iii), obtaining a preferably liquid, FW-containing stream S7, and a heated process stream, and / or (vi.3) Recycling at least part of the compressed water vapor-containing stream S4 obtained in (v) into the FW-containing stream S1 provided in (ii). It is preferred that the method comprises (vi.1 ) and / or (vi.2) and / or (vi.3). If the method includes (vi.1 ) and / or (vi.2) and / or (vi.3), it is preferred that the method includes (vi.1 ). If the method includes (vi.1 ) and / or (vi.2) and / or (vi.3), it is preferred that the method includes (vi.2). If the method includes (vi.1 ) and / or (vi.2) and / or (vi.3), it is preferred that the method includes (vi.3). If the method includes (vi.1 ) and / or (vi.2) and / or (vi.3), it is preferred that the method includes (vi.1 ) and (vi.2). If the method includes (vi.1 ) and / or (vi.2) and / or (vi.3), it is preferred that the method includes (vi.1 ) and (vi.3). If the method includes (vi.1 ) and / or (vi.2) and / or (vi.3), it is preferred that the method includes (vi.2) and (vi.3). If the method includes (vi.1 ) and / or (vi.2) and / or (vi.3), it is preferred that the method includes (vi.1 ) and (vi.2) and (vi.3). If the method includes (vi.1 ) and / or (vi.2) and / or (vi.3), it is preferred that the method further includes (vi.4). It is preferred that the polymer comprises one or more of polyethersulfone (PESU), polysulfone (PSU), and polyphenylsulfone (PPSU). It is preferred that the polar, aprotic solvent is selected from the group consisting of N-methyl-2-pyrrolidone (NMP), N,N-dimethylacetamide (DMAC), dimethyl sulfoxide (DMSO), monochlorobenzene (MCB), tetrahydrothiophene-1,1-dioxide (sulfolane), diphenyl sulfone, and mixtures of two or more thereof, further preferably from the group consisting of N-methyl-2-pyrrolidone (NMP), N,N-dimethylacetamide (DMAC), dimethyl sulfoxide (DMSO), monochlorobenzene (MCB), tetrahydrothiophene-1,1-dioxide (sulfolane), and mixtures of two or more thereof, further preferably from the group consisting of N-methyl-2-pyrrolidone (NMP), N,N-Dimethylacetamide (DMAC), Dimethyl sulfoxide (DMSO), Monochlorobenzene (MCB), and mixtures of two or more thereof, further preferably from the group consisting of N-methyl-2-pyrrolidone (NMP), N,N-Dimethylacetamide (DMAC), Dimethyl sulfoxide (DMSO), and mixtures of two or more thereof, wherein the polar, aprotic solvent is further preferably one or more of N-methyl-2-pyrrolidone (NMP) and Dimethyl sulfoxide (DMSO), wherein the polar, aprotic solvent is further preferably N-methyl-2-pyrrolidone (NMP). It is preferred that the bis(halophenyl)sulfone component comprises 4,4'-dichlorodiphenylsulfone (also referred to as bis(4-chlorophenyl)sulfone or DCDPS for short). It is preferred that the aromatic dihydroxy component comprises one or more of bisphenol A (IUPAC: 4-[2-(4-hydroxyphenyl)propan-2-yl]phenol), bisphenol S (also known as bis(4-hydroxyphenyl)sulfone), and biphenyl-4,4'-diol. It is preferred that the reactant current includes one or more activators. It is preferred that the polycondensation conditions according to (i) include heating the reactant stream to a temperature in the range of 120 to 220 °C. It is preferred that the polycondensation conditions according to (i) include applying a pressure in the range of 700 to 1300 bara. Preferably, the method according to (i) and before (iii) further comprises (i.1) Separation of one or more salts. If the process further comprises separating the one or more salts according to (i.1 ), it is preferred that the one or more salts are selected from the group consisting of KCl, NaCl, and mixtures of two or more thereof. If the process further includes separating the one or more salts according to (i.1), it is preferred that the separation be carried out by filtration. It is preferred that the FW-containing stream S1 provided according to (ii) comprises drinking water, demineralized water (DI water), boiler feedwater, at least a part of the compressed steam-containing stream S4 obtained in (v), at least a part of the FW-containing stream S5 obtained from (vi.1), or at least a part of the FW-containing stream S7 obtained from (vi.4), wherein the FW-containing stream S1 provided according to (ii) further preferably consists of drinking water, demineralized water (DI water), or boiler feedwater. Preferably, the process according to (iii) and prior to (iv) further comprises (iii.1) separation of the polymer. It is preferred that the H2O and solvent-containing stream S2 obtained in (iii) has an H2O content in the range of 30 to 95 wt%. It is preferred that the H2O and solvent-containing stream S2 obtained in (iii) has a solvent content in the range of 5 to 70 wt%. It is preferred that 99.0 to 100 wt%, more preferably 99.5 to 100 wt%, more preferably 99.9 to 100 wt%, of the H2O and solvent-containing stream S2 obtained in (iii) consist of H2O and the solvent. Preferably the process according to (iii) and prior to (iv), preferably according to (iii.1) and prior to (iv), further (iii.2) heating the H2O and solvent-containing stream S2 obtained in (iii). It is preferred that the separation of the H2O and solvent-containing stream S2 according to (iv) comprises heating the H2O and solvent-containing stream S2 in the separation device, wherein the heating is further preferably carried out by means of one or more heat exchangers, wherein the heating further preferably comprises transferring heat from at least a part of the compressed water vapor-containing stream S4 obtained in (v) to the H2O and solvent-containing stream S2. It is preferred that the separation device comprises one or more, more preferably one, two or three, columns. It is preferred that the temperature in the separation device according to (iv) is in a range of 50 to 300 °C. It is preferred that the pressure in the separating device according to (iv) is in a range of 123 to 1432 mbara. It is preferred that the separation be carried out by distillation. Preferably, the method according to (iv) and before (v) further comprises (iv.1 ) Heating the steam-containing stream S3 obtained in (iv), wherein the heating is preferably carried out by means of a steam superheater. It is preferred that the water vapor-containing stream S3 obtained in (iv) and in (iv.1) independently have a solvent content in the range of 0 to 1000 ppm. It is preferred that the water vapor-containing stream S3 obtained in (iv) and in (iv.1) independently have a pressure in the range of 123 to 1432 mbara. It is preferred that the water vapor-containing stream S3 obtained in (iv) and in (iv.1) independently have a mass flow rate in the range of 1 to 50 t / h. It is preferred that the pressure ratio p(S4):p(S3) of the compressed water vapor-containing stream S4 obtained in (v) to the water vapor-containing stream S3 obtained in (iv) is in a range of 1 :1 to 12 : 1, preferably from 2 : 1 to 10 : 1, more preferably from 3 : 1 to 6 : 1. It is preferred that the compressed water vapor-containing stream S4 obtained in (v) has a pressure in the range of 0.124 to 39.8 bara, more preferably from 0.385 to 15.5 bara, more preferably from 0.845 to 11.3 bara, more preferably from 1.208 to 9 bara, more preferably from 1.69 to 7 bara. It is preferred that the compressed water vapor-containing stream S4 obtained in (v) has a mass flow rate in the range of 1 to 50 t / h. It is preferred that the compression according to (v) is carried out in one or more compression stages, preferably in 2 to 4 stages, more preferably in 3 compression stages, wherein the one or more compression stages are more preferably carried out one after the other. If the compression according to (v) is carried out in one or more compression stages, it is preferred that in a first compression stage the pressure ratio of the compressed water vapor-containing stream S4 obtained therefrom to the water vapor-containing gas stream S4 obtained in (v) is in a range of 1.7:1 to 2.5:1, more preferably from 1.8:1 to 2.3:1, more preferably from 1.9:1 to 2.1:1. If the compression according to (v) is carried out in one or more compression stages, it is preferred that the method according to (v) further comprises (v.1 ) Injecting H2O into the water vapor-containing stream S4 obtained in the first compression stage. If the process according to (v) further comprises injecting H2O into the water vapor-containing stream S4 obtained in the first compression stage according to (v.1), it is preferred that the water vapor-containing stream S4 obtained in (v.1) has a temperature in the range of 90 to 120 °C, more preferably 95 to 115 °C, more preferably 100 to 110 °C. If the process according to (v) further comprises injecting H2O into the water vapor-containing stream S4 obtained in the first compression stage according to (v.1 ), it is preferred that in a second compression stage the water vapor-containing stream S4 obtained in (v.1 ) is compressed to a pressure in the range of 1,020 to 2,000 mbara, more preferably from 1,105 to 1,900 mbara, more preferably from 1,275 to 1,700 mbara. If, in a second compression stage, the water vapor-containing stream S4 obtained in (v.1) is compressed to a pressure in the range of 1,020 to 2,000 mbar, it is preferred that the method according to (v.1) further comprises (v.2) Injecting H2O into the water vapor-containing stream S4 obtained in the second compression stage. If the process according to (v.1) further includes injecting H2O into the water vapor-containing stream S4 obtained in the second compression stage according to (v.2), it is preferred that the water vapor-containing stream S4 obtained in (v.2) has a temperature in the range of 105 to 135 °C, more preferably 110 to 130 °C, more preferably 115 to 125 °C. If the process according to (v.1) further comprises injecting H2O into the water vapor-containing stream S4 obtained in the second compression stage according to (v.2), it is preferred that in a third compression stage the water vapor-containing stream S4 obtained in (v.2) is compressed to a pressure in the range of 1,735 to 4,000 mbara, more preferably from 1,880 to 3,800 mbara, more preferably from 2,170 to 3,400 mbara. If, in a third compression stage, the water vapor-containing stream S4 obtained in (v.2) is compressed to a pressure in the range of 1,735 to 4,000 mbar, it is preferred that the method according to (v.2) further comprises (v.3) Injecting H2O into the water vapor-containing stream S4 obtained in the third compression stage. If the process according to (v.2) further includes injecting H2O into the water vapor-containing stream S4 obtained in the third compression stage according to (v.3), it is preferred that the water vapor-containing stream S4 obtained in (v.3) has a temperature in the range of 145 to 175 °C, more preferably 150 to 170 °C, more preferably 155 to 165 °C. It is preferred that the compression according to (v) is carried out by means of mechanical vapor recompressiori. It is preferred that the transfer of heat according to (vi.2) and (vi.4) takes place independently of each other by means of a heat exchanger. It is preferred that the H2O- and solvent-containing stream S2 according to (iv) is separated into a water vapor-containing stream S3, a solvent-containing gas stream and a recyclable bottom stream, optionally separating a portion of the recyclable bottom stream, wherein according to (vi.2) heat is transferred from at least a portion of the compressed water vapor-containing stream S4 obtained from (v) to the recyclable bottom stream, obtaining a heated recyclable bottom stream, wherein the heated recyclable bottom stream is recirculated into the separation device according to (iv). It is preferred that the process stream according to (vi.4) is different from the reactant stream according to (i), from the FW-containing stream S1 according to (ii), from the H2O and solvent-containing stream S2 obtained in (iii), from the water vapor-containing stream S3 obtained in (iv), from the solvent-containing stream obtained in (iv), or from the compressed water vapor-containing stream S4 obtained in (v), wherein the process stream according to (vi.4) is further preferably different from the reactant stream according to (i), from the FW-containing stream S1 according to (ii), from the FW and solvent-containing stream S2 obtained in (iii), from the water vapor-containing stream S3 obtained in (iv), from the solvent-containing gas stream obtained in (iv), and from the compressed water vapor-containing stream S4 obtained in (v). It is preferred that in (vi.4) heat from at least a part of the compressed steam-containing stream S4 obtained in (v) is transferred to a process stream of a chemical process, wherein the chemical process according to (vi.4) further preferably comprises the work-up or production of the polar, aprotic solvent. It is preferred that the process stream according to (vi.4) comprises one or more of NMP and H2O, wherein the process stream according to (vi.4) further preferably comprises one or more of drinking water, demineralized water (DI water), or boiler feedwater, wherein the process stream according to (vi.4) further preferably consists of drinking water, demineralized water (DI water), or boiler feedwater. Preferably, the method according to (vi.1) further comprises (vii) Transferring heat from the H2O-containing stream S5 obtained from (vi.1) to the H2O-containing stream S1 provided according to (ii), wherein the H2O-containing stream S1 is preferably heated by 65 to 85 K, more preferably by 70 to 80 K. Preferably, the method according to (vi.1) further comprises (viii) Recycling at least part of the H2O-containing stream S5 obtained from (vi.1 ) into the H2O-containing stream S1 provided according to (ii). Preferably, the method according to (vi.4) further comprises (ix) Transfer of heat from the H2O-containing stream S7 obtained from (vi.4) to a KG-containing stream S8 or to the KO-containing stream S1 provided according to (ii). Preferably, the method according to (vi.4) further comprises (x) Recycling at least part of the KO-containing stream S7 obtained from (vi.4) into the KO-containing stream S1 provided according to (ii). It is preferred that the heated KO-containing stream S1 obtained from (vi.2) and the KO-containing stream S7 obtained from (vi.4) independently have a content of the polar, aprotic solvent in the range of 0 to 10 ppm, more preferably from 0 to 5 ppm. Preferably, the process according to (iii) further comprises (xi) drying the polymer obtained according to (iii). It is preferred that the process according to (iii) or (vii) further comprises (xii) forming the polymer obtained according to (iii) or (xi) into a shaped body. If the process further comprises forming the polymer obtained according to (iii) or (xi) into a shaped body according to (xii), it is preferred that the forming according to (xii) comprises extrusion, and wherein the polymer obtained according to (iii) or (xi) is further preferably formed into a strand, wherein the strand is further preferably cut into cylinders or cut into lens shapes under water. It is preferred that the procedure be carried out continuously. The present invention further relates to a method for producing a target product by converting the polymer that can be obtained or has been obtained according to one of the embodiments described herein. Using the method described herein, H2O-containing streams can be provided, in particular for recycling into the process itself, for heat transfer, including further use in other processes, wherein these H2O-containing streams can be provided in various pressure and temperature ranges, preferably as steam streams. This applies in particular to the compressed steam-containing stream S4 obtained in (v). With regard to these streams, it is preferred that they are in gaseous form, i.e., as water vapor. The water vapor can initially be generated in a vacuum. The resulting water vapor is preferably further compressed, as described in the embodiments, for example, in embodiments 26 to 38 concerning the compression of the water vapor-containing stream S3 obtained in (iv). Compression of a gaseous H2O-containing stream can be carried out by means of one or more compressors, preferably a cascade of compressors. Positive displacement machines and / or turbomachines, for example, screw compressors, radial blowers, radial turbo compressors, and / or axial turbo compressors, can be used as compressors. The compression preferably includes the supply of water for spraying off the vapor after a compressor with the longest possible inlet length.Preferably, the water is sprayed to accelerate evaporation and prevent the formation of droplet streaks, as water droplets can impair the function of compressor blades. In particular, the blades of an axial turbo compressor should not come into contact with water droplets. Alternatively, water can also be sprayed for cooling purposes, for example, when screw compressors and / or radial blowers are used. In this way, the water vapor can be compressed to a pressure in the range of 1 to 120 barg at a temperature in the range of 127 to 450 °C, preferably to a pressure in the range of 1.5 to 2.0 barg at a temperature in the range of 127 to 200 °C, a pressure in the range of 4.0 to 5.8 barg at a temperature in the range of 151 to 200 °C, a pressure in the range of 15.0 to 17.8 barg at a temperature in the range of 201 to 250 °C, a pressure in the range of 40 to 49 barg at a temperature in the range of 250 to 300 °C, or a pressure in the range of 100 to 117 barg at a temperature in the range of 310 to 450 °C. Compression to a pressure in the range of 4.0 to 5.8 barg is comparatively more economical than compression to a pressure in the range of 15.0 to 17.8 barg. Steam at a pressure in the range of 40 to 49 barg or in the range of 100 to 117 barg can be generated by the compression described; however, generation using waste heat from a cracker or similar processes is comparatively more energy-efficient. The compressed steam can be fed into a steam network, preferably in one of the pressure and temperature ranges described herein, and then fed into the process itself or into another process. The compressed steam can be used in the plant used for purifying a polar, aprotic solvent or in spatially adjacent plants for (accompanying) heating of equipment and pipelines (e.g., for frost protection in winter), preferably at a pressure in the range of 1.5 to 2.0 barg. Alternatively, the compressed steam can be used in spatially adjacent plants for heating evaporators and reactors (e.g., to reduce steam consumption from the network). For example, compressing the steam to 3 barg may be sufficient. In another alternative, the compressed green steam can be mixed with steam from the steam network, even at different pressure levels. The "green steam" produced via waste heat and with the aid of green electrical energy in compressors can then be allocated to other plants or their products when connected via pipelines or a steam network.This can reduce the Product Carbon Footprint (PCF) of products manufactured in plants that do not generate green steam. The present invention further relates to a target product that can be obtained or is attainable by a method according to the present invention. The publication “Chemical Compounds”; Issue 684; paragraphs

[1000] until

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

[1000] to

[8005] described. Preferably, the method described here is furthermore a method for producing a product, preferably the target product. The conversion step for obtaining the target product preferably comprises one or more steps as described below and can be carried out by conventional methods known to a person skilled in the art. The conversion step preferably comprises one or more of the following: recycling, preferably depolymerization, gasification, pyrolysis, and / or steam cracking; and / or purification, preferably crystallization, (solvent) extraction, distillation, evaporation, hydrotreating, absorption, adsorption, and / or ion exchange treatment; and / or processing, preferably foaming, synthesis, chemical conversion, polymerization, and / or compounding; and / or shaping, preferably foaming, extrusion, and / or forming; and / or finishing, preferably coating and / or smoothing. Additionally, the one or more steps in Reference RF1 are described in the paragraphs below.

[1000] to

[8005] described in detail. The term "building block," as used here, encompasses compounds that exist in a gaseous or liquid state under standard conditions of 0°C and 0.1 MPa. Building blocks are typically used in the chemical industry to form secondary products that exhibit higher structural complexity and / or a higher molecular weight than the building block on which the secondary product is based. The building block is preferably selected from the group consisting of hydrogen, carbon monoxide, carbon dioxide, ethylene oxide, ethylene glycols, synthesis gas consisting of a mixture of hydrogen and carbon monoxide, alkanes, alkenes, alkynes, and aromatic compounds. The alkanes, alkenes, alkynes, and aromatic compounds include, in particular, those with 1 to 12 carbon atoms. The term "monomer," as used here, encompasses molecules that can react with one another to form polymers by polymerization. The monomer is preferably selected from the group consisting of (meth)acrylic acid, salts of (meth)acrylic acid, in particular sodium, potassium, and zinc salts, (meth)acrolein, and (meth)acrylates. (Meth)acrylates with 1 to 22 carbon atoms are preferred, especially those with 1 to 8 carbon atoms. The terms (meth)acrylic acid, (meth)acrolein, or (meth)acrylate refer to acrylic acid, acrolein, or acrylate, respectively, and to methacrylic acid, methacrolein, or methacrylate, respectively. Furthermore, the monomer can be selected from hexamethylenediamine (HMD) and adipic acid. The building block can also be an intermediate compound. The term "intermediate compound," as used here, encompasses organic reagents used to form compounds of higher molecular complexity. The intermediate compound can be selected, for example, from the group consisting of phosgene, polyisocyanates, and propylene oxide. The polyisocyanates are, in particular, aromatic di- and polyisocyanates, preferably toluene diisocyanate (TDI) and / or diphenylmethane diisocyanate (MDI). The building block and the monomer, as well as typical conversion steps for obtaining the building block or monomer, are described in the following paragraphs.

[1000] to

[1012] The reference RF1 is described in more detail. The term "Polymer A", as used here, includes thermoplastic polymers, e.g. polyamide or thermoplastic polyurethane, thermosetting polymers, e.g. polyurethane, elastomers, e.g. polybutadiene, or a copolymer or a mixture thereof, and is further defined in the following paragraphs.

[2001] until

[2007] defined by reference RF1. The term "polymer composition A", as used here, includes all compositions containing a polymer as described above and one or more additives, e.g., reinforcing agents, colorants, modifiers and / or flame retardants, and is further specified in paragraph

[2008] defined by reference RF1. The term "polymer product A", as used here, encompasses a product containing polymer A and / or polymer composition A as described above and is further specified in the paragraphs

[2009] and

[2010] defined by reference RF1. The steps for obtaining the polymer, preferably polymer A, the polymer composition, preferably polymer composition A, or the polymer product, preferably polymer product A, are described in more detail in paragraph

[2011] described in reference RF1. The term "polymer for industrial use" includes rheological polymers, polycarboxylates, alkoxysilated polyalkylenamines, alkoxysilated polyalkylenimines, polyether-based polymers, color inhibition and dirt removal or cleaning polymers, which are described in the paragraphs

[3035] until

[3044] are defined in more detail by the reference RF1. The term "surfactant for industrial use" includes non-ionic, anionic and amphoteric surfactants for industrial use, which are described in the paragraphs

[3008] until

[3034] are defined in more detail by reference RF1. The term "descaling agents for industrial use" includes non-phosphate-based builders (NPB) and phosphonates (CoP), which are described in the paragraphs

[3001] until

[3005] are described in more detail in reference RF1. The term "biocide for industrial use" refers to a chemical compound that kills microorganisms or inhibits their growth or reproduction, as described in the paragraphs

[3006] until

[3007] further defined by the reference RF1. The term "solvents for industrial use" includes alkylamides, alkylactamides, alkyl esters, lactate esters, alkyl diesters, cyclic alkyl diesters, cyclic carbonates, aromatic aldehydes and aromatic esters, which are listed in the paragraphs

[3045] until

[3055] are defined in more detail by the reference RF1. The term "dispersants for industrial use" includes anionic and non-ionic dispersants for industrial use, which are described in the paragraphs

[3056] until

[3058] are defined in more detail by the reference RF1. The term "composition and / or formulation thereof" in relation to polymers for industrial use, surfactants for industrial use, descaling agents for industrial use and / or biocides for industrial use refers to compositions for industrial use and / or products for institutional use and / or textile and household care products and / or personal care products which are listed in paragraph

[3059] The conversion steps for the production of the polymer for industrial use, the surfactant for industrial use, the descaling agent for industrial use and / or the biocide for industrial use are defined in paragraph

[3060] Reference RF1 is defined in more detail. The conversion steps for the manufacture of the composition for industrial use or the formulation of the polymer for industrial use, the surfactant for industrial use, the descaling agent for industrial use and / or the biocide for industrial use are described in paragraph

[3061] defined in more detail by reference RF1. The term "plant protection product composition" generally refers to a composition that includes an agrochemically active ingredient and at least one agrochemical formulation additive. Examples of plant protection product compositions, active ingredients, and additives are given in paragraph [number].

[4001] The reference RF1 describes it in more detail. The plant protection product composition can be in any conventional formulation. The plant protection product compositions are manufactured using conventional methods, e.g., as described in the publications by Mollet and Grubemann, Formulation technology, Wiley VCH, Weinheim, 2001; or Knowles, New developments in crop protection product formulation, Agrow Reports DS243, T&F Informa, London, 2005. The conversion steps for the production of the agrochemically active ingredients and additives can be carried out analogously to the manufacturing steps of their analogues based on petrochemical or other precursors not obtained through recycling processes.Furthermore, conversion to compounds mentioned in the sections "Polymer" and "Cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, other cosmetic ingredients or compositions or formulations thereof" can take place as described in those sections and the corresponding paragraphs in Reference RF1. The term "active pharmaceutical agents and / or intermediates thereof" encompasses substances that produce a pharmacological effect or other direct action in the diagnosis, cure, alleviation, treatment, or prevention of disease, or that affect the structure or function of the body. Intermediates thereof are isolated products that arise during a multi-step synthesis route of an active pharmaceutical agent. The term "pharmaceutical excipients" encompasses compounds or mixtures of compounds used in compositions for various pharmaceutical applications that are not themselves substantially pharmaceutically active. Active pharmaceutical ingredients and / or intermediate products thereof, as well as pharmaceutical excipients, are included in paragraph

[5001] The reference RF1 defines in more detail. The conversion steps for the production of the active pharmaceutical ingredients and / or intermediates thereof and pharmaceutical excipients can be carried out by one or more synthesis steps and can be performed using conventional synthesis and techniques known to a person skilled in the art. The terms animal feed additives, food additives for humans and food supplements include vitamins, provitamins and active metabolites thereof, including intermediates and precursors, in particular vitamins A, B, E, D, K and their esters such as acetate, propionate, palmitate esters or alcohols thereof such as retinol or their salts, as well as any combinations thereof; tetraterpenes, in particular isoprenoids such as carotenoids and xanthophylls, including their intermediates and precursors, as well as mixtures and derivatives thereof, in particular beta-carotene, canthaxanthin, citranaxanthin, astaxanthin, zeaxanthin, lutein, lycopene, apo-carotenoids and any combinations thereof;Organic acids, in particular formic acid, propionic acid and their salts such as sodium, calcium or ammonium salts and any combinations thereof, such as, but not limited to, mixtures of formic acid and sodium formate, propionic acid and ammonium propionate, formic acid and propionic acid, formic acid and sodium formate and propionic acid, propionic acid and sodium propionate and formic acid and sodium formate; glycerides of carboxylic acids and short-chain and medium-chain fatty acids, conjugated linoleic acids such as omega-6 fatty acid (C18:2) methyl esters and 1,2-propanediol, as well as beverage stabilizers such as polyvinylpyrrolidone polymer or polyvinylimidazole-polyvinylpyrrolidone copolymer. Animal feed additives, food additives for humans and food supplements are listed in paragraph 1.

[5002] Reference RF1 further defines the conversion steps for the production of animal feed additives, food additives for humans, and dietary supplements. These conversion steps can be carried out by one or more synthesis steps and can be performed using conventional synthesis and techniques known to a skilled person. The term "aroma chemical and aroma composition" encompasses a volatile organic compound with a molecular weight between 70 and 250 g / mol containing a functional group with a carbon skeleton of 5 to 16 carbon atoms, including linear, branched, cyclic (e.g., with a ring size of C5-C18), bicyclic, or tricyclic aliphatic chains, and not necessarily one or more unsaturated structural elements such as double bonds, triple bonds, aromatics, or heteroaromatics. The one or more additional functional groups are preferably selected from alcohols, ethers, esters, ketones, aldehydes, acetals, carboxylic acids, nitriles, thiols, or amines. In one aspect, the aroma chemical is a terpene-based aroma chemical, selected, for example, from monoterpenes and monoterpenoids, sesquiterpenes and sesquiterpenoids, diterpenes, triterpenes, or tetraterpenes.Aroma chemicals can be combined with other aroma chemicals to form an aroma composition. Aroma chemicals and aroma compositions are discussed in paragraph [number].

[5003] The reference RF1 defines it in more detail. The conversion steps for the production of the aroma chemical and aroma composition can be carried out by one or more synthesis steps and can be performed using conventional synthesis and techniques known to a person skilled in the art. The term "aqueous polymer dispersion" includes aqueous compositions containing dispersed polymers and described in section

[6001] Reference RF1, entitled "aqueous polymer dispersion", defines the dispersed polymers in more detail. These polymers can be selected from acrylic emulsion polymers, styrene-acrylic emulsion polymers, styrene-butadiene dispersions, aqueous dispersions with composite particles, acrylate-alkyd hybrid dispersions, polyurethanes (including UV-curable polyurethanes), and polyurethane-poly(meth)acrylate hybrid polymers. The term "emulsion polymer" encompasses polymers produced by free-radical emulsion polymerization. Aqueous polyurethane dispersions are discussed in section [number missing in original text].

[6002] Reference RF1, entitled "Polyurethane dispersions", is defined in more detail. UV-curable polyurethanes are described in section

[6017] further defined in reference RF1. Polyurethane and poly(meth)acrylate hybrid polymers are described in section

[6016] further defined by the reference RF1. The term "polymeric dispersant" preferably includes polymers with a polyether-side chain, in particular polycarboxylate ether polymers and polycondensation products, which are described in paragraph

[6020] Reference RF1, entitled "Polymeric Dispersant," defines these in more detail. The conversion (polymerization) steps for the production of aqueous polymer dispersions with emulsion polymers are described in section [section number missing in original text].

[6003] further defined in reference RF1 entitled "Emulsion polymerization". The compositions and uses of aqueous polymer dispersions and polymeric dispersants are further defined in the following sections of Reference RF1: Section

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

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

[6006] entitled "Binders for paper coating", section

[6007] with the title "Binder for fiber bonding", Section

[6008] entitled "Adhesive polymers and adhesive compositions", Section

[6015] entitled "Aqueous polyurethane dispersions for coating compositions", Section

[6016] entitled "Aqueous polyurethane-poly(meth)acrylate hybrid polymers for coating compositions", Section

[6017] entitled "Aqueous UV-curable polyurethane dispersions, their manufacture and use and compositions containing them", Section

[6018] entitled “Inorganic binder compositions with polymeric dispersants and their use”, Section

[6019] entitled "100% curable coating compositions made of UV crosslinkable poly(meth)acrylate and their use in the manufacture of pressure-sensitive self-adhesive articles". Polyisocyanates, compositions containing them, and their uses are discussed in section

[6010] further defined in reference RF1 entitled "Polyisocyanates". Hyperbranched polyester polyols and their uses are discussed in section

[6011] Reference RF1, entitled "Organically solvent-based hyperbranched polyester polyols for coating compositions," is defined in more detail. The conversion steps for producing the hyperbranched polyester polyols are described in section

[6012] further defined in reference RF1 entitled "Production of organic solvent-based hyperbranched polyester polyols". Coating compositions containing hyperbranched polyester polyols, polyisocyanates and additives, as well as substrates coated therewith, are described in section

[6013] further defined in reference RF1 entitled "Organic solvent-based two-component coating compositions with hyperbranched polyester polyols and polyisocyanates". Unsaturated polyester polyols, solvent-based coating compositions containing these unsaturated polyester polyols, and substrates for coating with these coating compositions are described in section

[6018] further defines reference RF1 entitled "Organic solvent-based coating compositions with unsaturated polyester polyols". 100% curable coating compositions are described in section

[6019] further defines the reference RF1. Polymer dispersants for inorganic binder compositions are discussed in section

[6020] further defines the reference RF1. Inorganic binder compositions with polymeric dispersants and their use are discussed in section

[6021] Reference RF1 is defined in more detail. The conversion steps for the production of the polymeric dispersants are described in section

[6020] further defines the reference RF1. The term "cosmetic surfactant", as used here, includes non-ionic, anionic, cationic and amphoteric surfactants and is defined in paragraph

[7002] Reference RF1 defines the term "emollient" as used here. It refers to a chemical compound used to protect, moisturize, and / or lubricate the skin and is further defined in paragraph [reference number missing in original text].

[7003] further defined by the reference RF1. The term "wax", as used here, includes pearlescent agents and opacifying agents and is defined in paragraph

[7004] further defined by the reference RF1. The term "cosmetic polymer", as used here, encompasses any polymer that can be used as a component of a cosmetic formulation and is defined in paragraph

[7005] further defined by the reference RF1. The term "UV filter", as used here, refers to a chemical compound that blocks or absorbs ultraviolet light and is discussed in paragraph

[7006] further defined by the reference RF1. The term "other cosmetic ingredient," as used here, encompasses any ingredient suitable for the manufacture of a cosmetic formulation. Several sources list cosmetically acceptable ingredients. For example, the Cosing database on the European Commission's website contains cosmetic ingredients, and the International Cosmetic Ingredient Dictionary and Handbook, published by the Personal Care Products Council (PCPC), lists cosmetic ingredients. The term "composition and / or formulation thereof" in relation to the cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter and / or other cosmetic ingredient refers to personal care and / or cosmetic compositions or formulations described in paragraph

[7007] The conversion steps for the production of the cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, or other cosmetic ingredient are defined in more detail in paragraph [number].

[7008] further defined by the reference RF1. The terms "polymer B", "polymer composition B", "coating composition", "further functional composition", "film", "shaped body", "coating" and "coated substrate" are known to those skilled in the art and are used in the paragraphs

[8000] until

[8005] further defines the reference RF1. In a preferred embodiment, the target product is selected from: i) a building block or monomer; or ii) a polymer, preferably polymer A, a polymer composition, preferably polymer composition A, or a polymer product, preferably polymer product A; or iii) a cleaning polymer, cleaning surfactant, descaling agent, cleaning biocide, or a composition or formulation thereof; or iv) an agrochemical composition, agrochemical formulation aid, or agrochemical active substance; or v) an active pharmaceutical ingredient or an intermediate thereof, a pharmaceutical excipient, a feed additive, a human food additive, a dietary supplement, a flavoring chemical, or a flavoring composition;or vi) Aqueous polymer dispersion, preferably polyurethane or polyurethane-poly(meth)acrylate hybrid polymer dispersion, emulsion, binder for paper and fiber coatings, UV-curable acrylic polymer for hot melts and coatings, polyisocyanates, hyperbranched polyester polyols, polymeric dispersant for inorganic binder compositions, unsaturated polyester polyol or 100% curable composition; or vii) Cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, other cosmetic ingredients or compositions or formulations thereof; or viii) Polymer B, polymer composition B, coating composition, other functional composition, film, molded body, coating or coated substrate.; In a preferred embodiment, the content of the polymer produced or producible according to the present process in the target product is 1% by weight or more, preferably 2% by weight or more, more preferably 5% by weight or more, more preferably 15% by weight or more, more preferably 30% by weight or more, more preferably 40% by weight or more, more preferably 60% by weight or more, more preferably 80% by weight or more, more preferably 90% by weight or more, more preferably 95% by weight or more; and / or wherein the content of the polymer produced or producible according to the present process in the target product is 100% by weight or less, preferably 95% by weight or less, more preferably 90% by weight or less, more preferably 50% by weight or more. percent by weight or less, more preferably 25 percent by weight or less, more preferably 10 percent by weight or less; and wherein the content is preferably determined on the basis of identity preservation and / or separation and / or mass balance and / or book and chain of custody models, preferably on the basis of mass balance, preferably the International Sustainability and Carbon Certification (ISCC) Standard. In a preferred embodiment, the method, preferably according to one of the embodiments mentioned above, comprises the step of converting the polymer produced or producible according to one of the embodiments of the present method to obtain the target product. The present invention further comprises a target product, preferably a target product according to one of the embodiments mentioned herein, which is produced or can be produced by a process that includes the use of a steam stream produced by the process described herein. The unit bar (abs) or bara refers to absolute pressure and the unit bar (gauge) or barg to relative pressure, where 1 bar equals 10 5 Pa is. Within the scope of the present invention, pressure values ​​given in bar (gauge) refer to the gauge pressure p (gauge) relative to the ambient atmospheric pressure. To convert to the absolute pressure p (abs) in bar (absolute), the atmospheric pressure p (atm) is added, using a standard atmospheric pressure of 1.01325 bar. The conversion is performed according to the following equation: p (abs) = p (gauge) + p (atm), where p (atm) = 1.01325 bar. The present invention is further characterized by the following embodiments, including the individual and specific combinations of embodiments indicated by the respective dependencies. It should be noted in particular that in each case where a specific number of embodiments is defined, for example in the context of a term such as "method according to one of embodiments 1 to 4", each embodiment in this set is explicitly disclosed to the person skilled in the art, which means that the formulation of this term is to be understood by the person skilled in the art as synonymous with "method according to one of embodiments 1, 2, 3 and 4".Furthermore, it is expressly pointed out that the following list of exemplary embodiments constitutes an adequate, structured part of the general description, which is directed towards preferred aspects of the present invention and thus appropriately supports, but does not constitute, the claims of the present invention. 1. A process for the work-up of a polar, aprotic solvent, comprising the process (i) Reacting a reactant stream comprising an aromatic dihydroxy component, a bis(halophenyl)sulfone component, and a polar, aprotic solvent, under polycondensation conditions, obtaining a product stream comprising the polymer, the solvent, and optionally one or more salts, (ii) Provision of a fire-powered electricity S1 , (iii) Introducing the FW-containing stream S1 provided according to (ii) or the heated FW-containing stream S1 obtained from (vi.2) into the product stream obtained from (i) or (i.1) to separate the polymer, obtaining the polymer and an FW- and solvent-containing stream S2, (iv) Introducing the FW and solvent-containing stream S2 into a separation device, and separating the FW and solvent-containing stream S2 into a water vapor-containing stream S3 and a solvent-containing gas stream, (v) Compressing the water vapor-containing stream S3 obtained in (iv), obtaining a compressed water vapor-containing stream S4, (vi.1) Transferring heat from at least part of the compressed water vapor-containing stream S4 obtained in (v) to the FW and solvent-containing stream S2 obtained in (iii), obtaining an FW-containing stream S5 and a heated FW and solvent-containing stream S2, and / or (vi.2) optionally transferring heat from at least a part of the compressed water vapor-containing stream S4 obtained from (v) to the FW and solvent-containing stream S2 introduced into the separation device according to (iv), transferring heat from at least a part of the compressed water vapor-containing stream S4 obtained from (v) to the FW-containing stream S1 according to (ii), obtaining a, preferably liquid, FW-containing stream S6, and a heated FW-containing stream S1, and / or (vi.4) Transferring heat from at least a part of the compressed water vapor-containing stream S4 obtained in (v) to a process stream, wherein the process stream is different from the reactant stream according to (i) and from the FW and solvent-containing stream S2 obtained in (iii), obtaining a, preferably liquid, FW-containing stream S7, and a heated process stream, and / or (vi.3) Recycling at least part of the compressed water vapor-containing stream S4 obtained in (v) into the FW-containing stream S1 provided in (ii). 2. The method according to embodiment 1, the method comprising (vi.1 ) and / or (vi.2) and / or (vi.3). 3. The method according to embodiment 2, comprising (vi.1 ). 4. The method according to embodiment 2, the method comprising (vi.2). 5. The method according to embodiment 2, comprising the method (vi.3). 6. The method according to embodiment 2, comprising (vi.1) and (vi.2). 7. The method according to embodiment 2, comprising (vi.1) and (vi.3). 8. The method according to embodiment 2, comprising (vi.2) and (vi.3). 9. The method according to embodiment 2, comprising (vi.1) and (vi.2) and (vi.3). 10. The method according to one of embodiments 2 to 9, the method further comprising (vi.4). 11. The method according to one of embodiments 1 to 10, wherein the polymer comprises one or more of polyethersulfone (PESU), polysulfone (PSU), and polyphenylsulfone (PPSU), is preferred. 12. The process according to one of embodiments 1 to 11, wherein the polar, aprotic solvent is selected from the group consisting of N-methyl-2-pyrrolidone (NMP), N,N-dimethylacetamide (DMAC), dimethyl sulfoxide (DMSO), monochlorobenzene (MCB), tetrahydrothiophene-1,1-dioxide (sulfolane), diphenyl sulfone, and mixtures of two or more thereof, preferably from the group consisting of N-methyl-2-pyrrolidone (NMP), N,N-dimethylacetamide (DMAC), dimethyl sulfoxide (DMSO), monochlorobenzene (MCB), tetrahydrothiophene-1,1-dioxide (sulfolane), and mixtures of two or more thereof, further preferably from the group consisting of N-methyl-2-pyrrolidone (NMP), N,N-dimethylacetamide (DMAC), dimethyl sulfoxide (DMSO), monochlorobenzene (MCB), and mixtures of two or more thereof, further preferably from the group consisting of N-methyl-2-pyrrolidone (NMP), N,N-dimethylacetamide (DMAC), dimethyl sulfoxide (DMSO), and mixtures of two or more thereof, wherein the polar,aprotic solvents are further preferably one or more of N-methyl-2-pyrrolidone (NMP) and dimethyl sulfoxide (DMSO), wherein the polar aprotic solvent is further preferably N-methyl-2-pyrrolidone (NMP). 13. The method according to one of embodiments 1 to 12, wherein the bis(halophenyl)sulfone component comprises 4,4'-dichlorodiphenylsulfone (also referred to as bis(4-chlorophenyl)sulfone or DCDPS for short), is preferred. 14. The method according to one of embodiments 1 to 13, wherein the aromatic dihydroxy component comprises one or more of bisphenol A (IUPAC: 4-[2-(4-hydroxyphenyl)propan-2-yl]phenol), bisphenol S (also known as bis(4-hydroxyphenyl)sulfone), and biphenyl-4,4'-diol, is preferred. 15. The method according to one of embodiments 1 to 14, wherein the reactant current comprises one or more activators. 16. The method according to any of embodiments 1 to 15, wherein the polycondensation conditions according to (i) comprise heating the reactant stream to a temperature in the range of 120 to 220 °C. 17. The method according to one of embodiments 1 to 16, wherein the polycondensation conditions according to (i) include applying a pressure in the range of 700 to 1300 bara. 18. The method according to one of embodiments 1 to 17, further comprising (i) and (iii) (1.1) Separation of one or more salts. 19. The method according to embodiment 18, wherein the one or more salts are selected from the group consisting of KCl, NaCl, and mixtures of two or more thereof. 20. The method according to embodiment 18 or 19, wherein the separation is carried out by means of filtration. 21. The method according to one of embodiments 1 to 20, wherein the FhO-containing stream S1 provided according to (ii) comprises drinking water, demineralized water (DI water), boiler feedwater, at least a part of the compressed steam-containing stream S4 obtained in (v), at least a part of the FW-containing stream S5 obtained from (vi.1), or at least a part of the FW-containing stream S7 obtained from (vi.4), wherein the FW-containing stream S1 provided according to (ii) preferably consists of drinking water, demineralized water (DI water), or boiler feedwater. 22. The method according to one of embodiments 1 to 21, further comprising (iii) and before (iv) (111.1) Separation of the polymer. 23. The method according to one of embodiments 1 to 22, wherein the H2O and solvent-containing stream S2 obtained in (iii) has an H2O content in the range of 30 to 95 wt%. 24. The method according to one of embodiments 1 to 23, wherein the H2O and solvent-containing stream S2 obtained in (iii) has a solvent content in the range of 5 to 70 wt%. 25. The method according to one of embodiments 1 to 24, wherein 99.0 to 100 wt%, preferably 99.5 to 100 wt%, more preferably 99.9 to 100 wt%, of the H2O and solvent-containing stream S2 obtained in (iii) consists of H2O and the solvent. 26. The method according to one of embodiments 1 to 25, further comprising (iii) and before (iv), preferably (iii.1) and before (iv), (iii.2) Heating the H2O and solvent-containing stream S2 obtained in (iii). 27. The method according to one of embodiments 1 to 26, wherein the separation of the H2O and solvent-containing stream S2 according to (iv) comprises heating the H2O and solvent-containing stream S2 in the separation device, wherein the heating is preferably carried out by means of one or more heat exchangers, wherein the heating further preferably comprises transferring heat from at least a part of the compressed water vapor-containing stream S4 obtained in (v) to the H2O and solvent-containing stream S2. 28. The method according to one of embodiments 1 to 27, wherein the separation device comprises one or more, preferably one, two or three, more preferably one or two, columns. 29. The method according to one of embodiments 1 to 28, wherein the temperature in the separation device according to (iv) is in a range of 50 to 300 °C. 30. The method according to one of embodiments 1 to 29, wherein the pressure in the separating device according to (iv) is in a range of 123 to 1432 mbara. 31. The method according to one of embodiments 1 to 30, wherein the separation is carried out by distillation. 32. The method according to one of embodiments 1 to 31, further comprising (iv) and (v) (iv.1) Heating the steam-containing stream S3 obtained in (iv), wherein the heating is preferably carried out by means of a steam superheater. 33. The method according to one of embodiments 1 to 32, wherein the one in (iv) and in (iv.1 ) obtained water vapor-containing stream S3 independently exhibit a solvent content in the range of 0 to 1000 ppm. 34. The method according to one of embodiments 1 to 33, wherein the water vapor-containing stream S3 obtained in (iv) and in (iv.1) independently have a pressure in the range of 123 to 1432 mbara. 35. The method according to one of embodiments 1 to 34, wherein the water vapor-containing stream S3 obtained in (iv) and in (iv.1) independently have a mass flow rate in the range of 1 to 50 t / h. 36. The method according to one of embodiments 1 to 35, wherein the pressure ratio p(S4):p(S3) of the compressed water vapor-containing stream S4 obtained in (v) to the water vapor-containing stream S3 obtained in (iv) is in a range of 1 :1 to 12:1, preferably from 2 :1 to 10 :1, more preferably from 3 :1 to 6 :1. 37. The method according to one of embodiments 1 to 36, wherein the compressed water vapor-containing stream S4 obtained in (v) has a pressure in the range of 0.124 to 39.8 bara, preferably from 0.385 to 15.5 bara, more preferably from 0.845 to 11.3 bara, more preferably from 1.208 to 9 bara, more preferably from 1.69 to 7 bara. 38. The method according to one of embodiments 1 to 37, wherein the compressed water vapor-containing stream S4 obtained in (v) has a mass flow rate in the range of 1 to 50 t / h. 39. The method according to one of embodiments 1 to 38, wherein the compression according to (v) is carried out in one or more compression stages, preferably in 2 to 4 stages, more preferably in 3 compression stages, wherein the one or more compression stages are preferably carried out one after the other. 40. The method according to embodiment 39, wherein in a first compression stage the pressure ratio of the compressed water vapor-containing stream S4 obtained therefrom to the water vapor-containing gas stream S4 obtained in (v) is in a range of 1.7:1 to 2.5:1, preferably from 1.8:1 to 2.3:1, more preferably from 1.9:1 to 2.1:1. 41. The method according to embodiment 39 or 40, further comprising according to (v) (v.1) Injecting H2O into the water vapor-containing stream S4 obtained in the first compression stage. 42. The method according to embodiment 41, wherein the steam-containing stream S4 obtained in (v.1) has a temperature in the range of 90 to 120 °C, preferably 95 to 115 °C, more preferably 100 to 110 °C. 43. The method according to embodiment 41 or 42, wherein in a second compression stage the water vapor-containing stream S4 obtained in (v.1) is compressed to a pressure in the range of 1,020 to 2,000 mbara, preferably from 1,105 to 1,900 mbara, more preferably from 1,275 to 1,700 mbara. 44. The method according to one of embodiments 41 to 43, further comprising according to (v.1) (v.2) Injecting H2O into the water vapor-containing stream S4 obtained in the second compression stage. 45. The method according to embodiment 44, wherein the water vapor-containing stream S4 obtained in (v.2) has a temperature in the range of 105 to 135 °C, preferably 110 to 130 °C, more preferably 115 to 125 °C. 46. ​​The method according to embodiment 44 or 45, wherein in a third compression stage the water vapor-containing stream S4 obtained in (v.2) is compressed to a pressure in the range of 1,735 to 4,000 mbara, preferably from 1,880 to 3,800 mbara, more preferably from 2,170 to 3,400 mbara. 47. The method according to one of embodiments 44 to 46, further comprising (v.2) (v.3) Injecting H2O into the water vapor-containing stream S4 obtained in the third compression stage. 48. The method according to embodiment 47, wherein the steam-containing stream S4 obtained in (v.3) has a temperature in the range of 145 to 175 °C, preferably 150 to 170 °C, more preferably 155 to 165 °C. 49. The method according to one of embodiments 1 to 48, wherein the compression according to (v) is carried out by means of mechanical vapor recompressiori. 50. The method according to one of embodiments 1 to 49, wherein the transfer of heat according to (vi.2) and (vi.4) is carried out independently of each other by means of a heat exchanger. 51. The method according to one of embodiments 1 to 50, wherein the H2O- and solvent-containing stream S2 according to (iv) is separated into a water vapor-containing stream S3, a solvent-containing gas stream and a recyclable bottom stream, optionally separating a portion of the recyclable bottom stream, and wherein, according to (vi.2), heat is transferred from at least a part of the compressed water vapor-containing stream S4 obtained from (v) to the recirculated bottom stream, obtaining a heated recirculated bottom stream, wherein the heated recirculated bottom stream is recirculated into the separation device according to (iv). 52. The method according to one of embodiments 1 to 51, wherein the process stream according to (vi.4) is different from the reactant stream according to (i), from the l-hO-containing stream S1 according to (ii), from the H2O- and solvent-containing stream S2 obtained in (iii), from the water vapor-containing stream S3 obtained in (iv), from the solvent-containing stream obtained in (iv), or from the compressed water vapor-containing stream S4 obtained in (v), wherein the process stream according to (vi.4) is preferably different from the reactant stream according to (i), from the FhO-containing stream S1 according to (ii), from the H2O- and solvent-containing stream S2 obtained in (iii), from the water vapor-containing stream S3 obtained in (iv), from the solvent-containing gas stream obtained in (iv), and from the compressed water vapor-containing stream S4 obtained in (v). 53. The method according to one of embodiments 1 to 52, wherein in (vi.4) heat from at least a part of the compressed steam-containing stream S4 obtained in (v) is transferred to a process stream of a chemical process, wherein the chemical process according to (vi.4) preferably comprises the work-up or production of the polar, aprotic solvent. 54. The method according to one of embodiments 1 to 53, wherein the process stream according to (vi.4) comprises one or more of NMP and H2O, wherein the process stream according to (vi.4) preferably comprises one or more of drinking water, demineralized water (DI water), or boiler feedwater, wherein the process stream according to (vi.4) further preferably consists of drinking water, demineralized water (DI water), or boiler feedwater. 55. The method according to one of embodiments 1 to 54, further comprising according to (vi.1 ) (vii) Transferring heat from the H2O-containing stream S5 obtained from (vi.1) to the H2O-containing stream S1 provided according to (ii), wherein the H2O-containing stream S1 is preferably heated by 65 to 85 K, more preferably by 70 to 80 K. 56. The method according to one of embodiments 1 to 55, further comprising (vi.1) (viii) Recycling at least part of the H2O-containing stream S5 obtained from (vi.1) into the H2O-containing stream S1 provided according to (ii). 57. The method according to one of embodiments 1 to 56, further comprising (vi.4) (ix) Transferring heat from the l-hO-containing stream S7 obtained from (vi.4) to an l-hO-containing stream S8 or to the l-hO-containing stream S1 provided according to (ii). 58. The method according to one of embodiments 1 to 57, further comprising (vi-4) (x) Recycling at least part of the l-hO-containing stream S7 obtained from (vi.4) into the l-hO-containing stream S1 provided according to (ii). 59. The method according to one of embodiments 1 to 58, wherein the heated FhO-containing stream S1 obtained from (vi.2) and the l-hO-containing stream S7 obtained from (vi.4) independently have a content of the polar, aprotic solvent in the range of 0 to 10 ppm, preferably 0 to 5 ppm. 60. The method according to one of embodiments 1 to 59, further comprising according to (iii) (xi) Drying of the polymer obtained according to (iii). 61. The method according to one of embodiments 1 to 60, further comprising (iii) or (vii) (xii) Forming the polymer obtained according to (iii) or (xi) into a shaped body. 62. The method according to embodiment 61, wherein the forming according to (xii) comprises extrusion, and wherein the polymer obtained according to (iii) or (xi) is preferably formed into a strand, the strand being further preferably cut into cylinders or cut into lens shape under water. 63. The method according to one of embodiments 1 to 62, wherein the method is carried out continuously. 64. Method for producing a target product by converting the polymer that can be obtained or has been obtained according to any one of embodiments 1 to 63. The present invention is further illustrated by the following example. EXAMPLES Example 1: Production of a polymer according to the present invention A reactant stream comprising an aromatic dihydroxy component, a bis(halophenyl)sulfone component, and a suitable solvent is provided. Figure 1 illustrates this. The process for producing a polymer is simplified below. The aromatic dihydroxy component and the bis(halophenyl)sulfone component are subjected to polycondensation conditions. In the first workup step, the resulting salt is separated from the product stream. In the second step, a water-containing stream is added to the polymer-solvent mixture to separate the solvent. The remaining mixture, consisting of water and the solvent, is then processed by distillation, yielding a solvent-containing stream and a steam-containing stream. The solvent-purified polymer is subsequently processed into the finished product in further steps. Distillation requires a large amount of steam to distill the solvent-water mixture. The vapor is further processed by mechanical vapor compression and can be used to generate heating steam, which in turn can be used to heat the distillation column. Surprisingly, it was found that the remaining residual heat is sufficient to heat water, which can then be used for separation in the second processing step. Instead of steam produced using fossil fuels in the old process, the new process now uses electricity, preferably of renewable origin, as the energy source to operate the mechanical vapor compression. This has reduced the net energy requirement for producing one ton of steam. Example 2: Production of a polymer according to the present invention As described in Example 1, a polymer is produced. Upon separation from the polymer, a mixture is obtained comprising approximately 74 wt% H₂O, approximately 26 wt% solvent NMP, as well as small amounts of salt and high-boiling components. This mixture is then processed by distillation. In a first evaporator stage V1, the mixture is initially heated from 55 °C to 88 °C at a pressure of 350 mbar absolute, during which it partially evaporates. Heating is achieved by heat transfer from the vapor stream, which is obtained through the mechanical compression of the vapor stream at the head of the separator. At the head of the separator, a vapor stream with a temperature of 61 °C and a pressure of 205 mbar absolute is obtained. Compression yields a vapor stream with a temperature of 125–127 °C and a pressure of 2.3 bar absolute, which is used for heat transfer, resulting in a vapor condensate with a temperature of 110–120 °C. The heated mixture, comprising H₂O and the solvent NMP, is then introduced into the separator. Furthermore, the obtained steam condensate can be used to heat an H2O-containing stream S1 from 20-25 °C to 98 °C by means of a further heat transfer, which is used to separate the poly- The system can be used to further cool the steam condensate to 50-60 °C. The cooled steam condensate can then be returned to the top of the separating device. The portion of the mixture comprising H₂O and solvent NMP that does not evaporate in the first evaporator stage V1 is evaporated in two further evaporator stages at temperatures of 130 °C and 145 °C and introduced into the separation device. The separation device is operated in the sump at a temperature of 165 °C. Figure 3 shows a simplified representation of the procedure according to Example 2. In addition to the technical effects described in Example 1, it was found that the process according to Example 2 is particularly relatively more efficient and therefore more cost-effective if a pressure increase from approximately 200 mbar absolute to 2.3 bar absolute is achieved during steam compression, rather than an increase to 12-16 bar absolute, as would be necessary to heat the sump. List of streams in the process Educ current Product stream (obtained from (i)) 51 FhO-containing electricity (provided in (ii)) heated FW-containing electricity (obtained from (vi.2)) 52 H2O and solvent-containing stream (obtained from (iii)) Heated H2O and solvent-containing stream (obtained from (vi.1 )) 53 Water vapor-containing stream (obtained from (iv)) Solvent-containing gas stream (obtained from (iv)) 54 compressed water vapor-containing stream (obtained from (v)) 55 FW-containing electricity (obtained from (vi.1 )) 56 FW-containing electricity S6 (obtained from (vi.2)) 57 FW-containing electricity S7 (obtained from (vi.4)) 58 FW-containing electricity Description of the illustrations Figure 1: shows a simplified representation of a manufacturing process for a polymer. Figure 2: shows a simplified representation of the process steps for separating the solvent-water mixture, here by means of distillation, the subsequent Compression of the vapor, and possible uses of the compressed vapor. Figure 3: shows a simplified representation of the process steps of separating the solvent-water mixture by distillation, the subsequent Compression of the vapor, and use of the compressed vapor to heat an H2O and solvent-containing stream (S2) which is introduced into the separation device, as well as an FW-containing stream (S1) which can be used to separate and wash the polymer. Cited literature - CN 116947728 A - CN 219558744 U - EP 4091688 A1 - US 2018 / 171079 A1 - US 12005381 B2

Claims

Claims 1. A process for the work-up of a polar, aprotic solvent, comprising the process (i) Reacting a reactant stream comprising an aromatic dihydroxy component, a bis(halophenyl)sulfone component, and a polar, aprotic solvent, under polycondensation conditions, obtaining a product stream comprising the polymer, the solvent, and optionally one or more salts, (ii) Provision of a fire-powered electricity S1 , (iii) Introducing the FW-containing stream S1 provided according to (ii) or the heated FW-containing stream S1 obtained from (vi.2) into the product stream obtained from (i) to separate the polymer, obtaining the polymer and an FW- and solvent-containing stream S2, (iv) Introducing the FW and solvent-containing stream S2 into a separation device, and separating the FW and solvent-containing stream S2 into a water vapor-containing stream S3 and a solvent-containing gas stream, (v) Compressing the water vapor-containing stream S3 obtained in (iv), obtaining a compressed water vapor-containing stream S4, (vi.1) Transferring heat from at least part of the compressed water vapor-containing stream S4 obtained in (v) to the FW and solvent-containing stream S2 obtained in (iii), obtaining an FW-containing stream S5 and a heated FW and solvent-containing stream S2, and / or (vi.2) optionally transferring heat from at least part of the compressed water vapor-containing stream S4 obtained from (v) to the FW and solvent-containing stream S2 introduced into the separation device according to (iv), Transferring heat from at least part of the compressed water vapor-containing stream S4 obtained from (v) to the FW-containing stream S1 according to (ii), obtaining an FW-containing stream S6 and a heated FW-containing stream S1, and / or (vi.3) Recycling at least part of the compressed water vapor-containing stream S4 obtained in (v) into the FW-containing stream S1 provided in (ii).

2. The method according to claim 1, further comprising (vi.4) Transferring heat from at least part of the compressed water vapor-containing stream S4 obtained in (v) to a process stream, wherein the process stream is different from the reactant stream according to (i) and from the FW and solvent-containing stream S2 obtained in (iii), obtaining an FW-containing stream S7, and a heated process stream.

3. The method according to claim 1 or 2, wherein the polar, aprotic solvent is selected from the group consisting of N-methyl-2-pyrrolidone, N,N-dimethylacetamid, dimethyl sulfoxide, monochlorobenzene, tetrahydrothiophene-1,1-dioxide, diphenyl sulfone, and mixtures of two or more thereof.

4. The method according to any one of claims 1 to 3, wherein the H2O and solvent-containing stream S2 obtained in (iii) has an H2O content in the range of 30 to 95 wtno.

5. The method according to any one of claims 1 to 4, wherein the H2O and solvent-containing stream S2 obtained in (iii) has a solvent content in the range of 5 to 70 wt%.

6. The method according to any one of claims 1 to 5, wherein the separation device comprises one or more columns.

7. The method according to any one of claims 1 to 6, wherein the temperature in the separation device according to (iv) is in a range of 50 to 300 °C.

8. The method according to any one of claims 1 to 7, wherein the pressure in the separating device according to (iv) is in a range of 123 to 1432 mbara.

9. The method according to any one of claims 1 to 8, further comprising (iv) and (v) (iv.1) Heating the steam-containing stream S3 obtained in (iv).

10. The method according to any one of claims 1 to 9, wherein the water vapor-containing stream S3 obtained in (iv) and in (iv.1) independently has a solvent content in the range of 0 to 1000 ppm.

11. The method according to any one of claims 1 to 10, wherein the water vapor-containing stream S3 obtained in (iv) and in (iv.1) independently have a pressure in the range of 123 to 1432 mbara.

12. The method according to any one of claims 1 to 11, wherein the compressed water vapor-containing stream S4 obtained in (v) has a pressure in the range of 0.124 to 39.8 bara.

13. The method according to any one of claims 1 to 12, wherein the compression according to (v) is carried out in one or more compression stages.

14. The method according to any one of claims 1 to 13, further comprising (vii) Transfer of heat from the FW-containing electricity S5 obtained from (vi.1) to the FW-containing electricity S1 provided according to (II).

15. Method for producing a target product by converting the polymer that can be obtained or has been obtained according to any one of claims 1 to 14.

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