Energy-efficient method for producing styrene while recycling heat

Abstract

The invention relates to a method for producing styrene, starting from ethylbenzene, the method in particular involving the process of transferring heat from the obtained product gas flow to an H2O-containing flow. It has been found that the present method for producing styrene allows the heat required to carry out the dehydrogenation reaction to be efficiently recycled, in particular in order to heat the H2O-containing input flow being used.

Description

Energy-efficient process for the production of styrene with heat recovery TECHNICAL AREA The present invention relates to a process for the production of styrene (referred to as phenylethene or ethenylbenzene according to the IUPAC nomenclature) by recirculating heat. INTRODUCTION Styrene is typically produced on an industrial scale by dehydrating ethylbenzene in the presence of steam. If the dehydration takes place under adiabatic conditions, all the heat required for the dehydration is supplied to the one or more reactors by adding superheated steam to the ethylbenzene. The reaction mixture exiting the reaction zone, which primarily consists of water vapor, styrene, unreacted ethylbenzene, and any byproducts formed during the reaction, is subsequently cooled to a temperature of approximately 100 to 120 °C by one or more heat exchangers downstream of the one or more reactors. The heat transferred to the heat exchanger can be used to heat and evaporate the reactants (ethylbenzene + low-pressure steam), thus generating, for example, water vapor. The reaction mixture, cooled to approximately 100 to 120 °C, can be condensed and cooled in a downstream condenser using cooling water or air for further processing, although the heat released in this process is lost for economic use. Alternative processes have already been described in which this heat can be used, for example, to generate the steam that is used as a feedstock in the process. German patent DE 3147323 A1 describes a process in which, within a steam generator, a portion of the resulting reaction mixture condenses, while another portion containing water is vaporized to form steam. In this way, a portion of the reaction mixture, which previously had a temperature of 97 °C, is cooled to 91 °C, and steam is generated at a pressure of 0.5 bar and a temperature of 81 °C. The generated steam is then compressed to a pressure of 1.6 bar by means of a compressor. Furthermore, US 5386075 describes a process for the distillative separation of ethylbenzene and styrene, in which an ethylbenzene-containing stream is used for heat transfer. US 2012 / 149960 A1 and EP 2651859 B1 each relate to a process for the dehydrogenation of ethylbenzene, the process in particular comprising heat recovery. A disadvantage of the industrial production of styrene is that the steam used to dilute the ethylbenzene-containing stream is typically generated in steam boilers heated with fossil fuels, thus consuming large amounts of primary energy. This leads to significant Scope 1 emissions from the steam used, particularly because the mass ratio of steam to ethylbenzene can be around 1:1 or even higher. Consequently, the generated steam contributes approximately 85% to the Scope 1 emissions generated per kilogram of styrene produced. If the steam could be generated with significantly lower CO2 emissions, the Scope 1 emissions of the process, and therefore the overall CO2 footprint, would be considerably reduced. Furthermore, it is disadvantageous that the gaseous mixture obtained from the reaction, which has already been cooled to about 100 °C after the heat exchange described above, is cooled in a downstream condenser using water or air to such an extent that it condenses, whereby the heat released in the process is lost for economic use. DETAILED DESCRIPTION The present invention was based on the objective of providing a process for the production of styrene that is resource-efficient, and in particular energy-efficient, and thus exhibits significantly reduced scope 1 emissions. Furthermore, it was an objective of the present invention to enable operation at a comparatively low pressure of the reaction mixture flow. Finally, it was an objective of the present invention to achieve a comparatively high selectivity, so that, in particular, fewer raw materials are consumed and, in particular, fewer scope 1 emissions are generated. The object of the invention is solved by a process for the production of styrene which enables efficient recycling of the heat required for carrying out the dehydration reaction, in particular to heat the input stream containing H2O. The present invention therefore relates to a process for the production of styrene, comprising (i) Providing an ethylbenzene-containing stream S1 ; (ii) Providing a water-containing stream S2; (iii) Introducing the streams provided in (i) and (ii) into a reactor unit comprising a catalyst, and contacting the streams with the catalyst, obtaining a product gas stream S3 comprising styrene; (iv) optional transfer of heat from the product gas stream S3 obtained from (iii) to the in (i) ethylbenzene-containing stream S1 provided, to the FW-containing stream S2 provided in (ii), to an FW-containing stream S4, to the ethylbenzene-containing stream S1 provided in (i) and to the FW-containing stream S2 provided in (ii), to the ethylbenzene-containing stream S1 provided in (i) and to an FW-containing stream S4, to the FW-containing stream S2 provided in (ii) and to an FW-containing stream S4, or to the ethylbenzene-containing stream S1 provided in (i) and to the FW-containing stream S2 provided in (ii) and to an FW-containing stream S4; (v) optionally compressing the product gas stream obtained from (iii) or (iv) to obtain a compressed product gas stream S5; (vi) Provision of a fire-powered electricity S6; (vii) Transferring heat from the product gas stream S3 obtained from (iii), or from the product gas stream S3 obtained from (iv), or from the compressed product gas stream S5 obtained from (v), to the FW-containing stream S6, obtaining a cooled product gas stream and a heated FW-containing stream S7; (viii) Expanding the heated FW-containing stream S7 obtained from (vii), yielding a gaseous FW-containing stream S8 and a liquid FW-containing stream S9; (ix) Compressing the gaseous FW-containing stream S8 to a pressure in the range of 2.6 to 7 bara, obtaining a compressed gaseous FW-containing stream S10. It is preferred that 90 to 100 wt%, more preferably 95 to 100 wt%, more preferably 99 to 100 wt%, of the ethylbenzene-containing stream S1 provided in (i) consist of ethylbenzene. It is preferred that the ethylbenzene-containing stream provided in (i) comprises S1 FW. If the ethylbenzene-containing stream S1 provided in (i) comprises FW, it is preferred that 0 to 10 wt%, more preferably 0 to 5 wt%, more preferably 0 to 1 wt% of the ethylbenzene-containing stream S1 provided in (i) consist of FW. It is preferred that the ethylbenzene-containing stream S1 provided in (i) has a mass flow rate in the range of 1 to 300 t / h, more preferably from 10 to 280 t / h, and more preferably from 20 to 240 t / h. It is preferred that 90 to 100 wt%, more preferably 95 to 100 wt%, more preferably 99 to 100 wt% of the FW-containing electricity S2 provided in (ii) consist of FW. It is preferred that the FW-containing stream S2 provided in (ii) has a mass flow rate in the range of greater than 0 to 300 t / h, more preferably of 20 to 270 t / h, more preferably of 40 to 250 t / h. It is preferred that the FW-containing current S2 provided in (ii) has a temperature in the range of 650 to 950 °C, more preferably 750 to 900 °C, more preferably 800 to 850 °C. It is preferred that the FW-containing stream S2 provided in (ii) has a pressure in the range of 0.5 to 7 bara, more preferably from 1 to 6 bara, more preferably from 1.5 to 5 bara. Preferably, the method according to (ii) and before (iii) further comprises Mixing the ethylbenzene-containing stream S1 provided in (i) with the FW-containing stream S2 provided in (ii), obtaining a reaction gas stream S11; wherein in (iii) the reaction gas stream S11 is introduced into the reactor unit comprising a catalyst and contacted with the catalyst; wherein the reaction gas stream S11 further preferably has a mass ratio of FW to ethylbenzene in the range of 0.8:1 to 1.3:1, more preferably in the range of 0.9:1 to 1.2:1, more preferably in the range of 1:1 to 1.1:1. It is preferred that the reactor unit according to (iii) comprises one or more reactors, more preferably two or more reactors, more preferably two reactors, each reactor comprising the catalyst. If the reactor unit according to (iii) comprises one or more reactors, each reactor comprising the catalyst, it is preferred that the reactor unit comprises two or more reactors, preferably two reactors, wherein the two or more reactors are connected in series or in parallel, more preferably in series. It is preferred that the contacting according to (iii) be carried out under adiabatic conditions. It is preferred that the contacting according to (iii) is carried out at a temperature in the range of 500 to 700 °C, more preferably in a range of 525 to 675 °C, and more preferably in a range of 550 to 650 °C. It is preferred that the contacting according to (iii) is carried out at a pressure in the range of 0.1 to 1.5 bara, more preferably in a range of 0.2 to 1.3 bara, more preferably in a range of 0.25 to 1.2 bara. It is preferred that the catalyst included in the reactor unit according to (iii) comprises one or more Fe-containing compounds, wherein the one or more Fe-containing compounds further preferably comprise FeO, Fe2Ü3, FeO and Fe2Ü3, wherein the catalyst further preferably comprises 85 to 95 wt%, more preferably 87 to 91 wt%, of the Fe-containing compounds. It is preferred that the catalyst included in the reactor unit according to (iii) comprises Cr, wherein the catalyst further preferably comprises 1.7 to 2.3 wt%, and further preferably 1.9 to 2.1 wt%, Cr. It is preferred that the catalyst included in the reactor unit according to (iii) comprises KOH, wherein the catalyst further preferably comprises 7 to 11 wt%, and further preferably 8 to 10 wt%, KOH. It is preferred that the product gas stream S3 obtained from (iii) comprises styrene from 18 to 36 wt%, more preferably from 20 to 34 wt%, more preferably from 22 to 32 wt%. It is preferred that the product gas stream S3 obtained from (iii) comprises ethylbenzene from 12 to 34 wt%, more preferably from 14 to 32 wt%, more preferably from 15.5 to 29 wt%. It is preferred that the product gas stream S3 obtained from (iii) comprises 40 to 65 wt%, more preferably 45 to 60 wt%, more preferably 50 to 55 wt% water vapor. It is preferred that the product gas stream S3 obtained from (iii) comprises H2 from 0.3 to 1.3 wt%, more preferably from 0.35 to 0.8 wt%, more preferably from 0.4 to 0.6 wt%. It is preferred that 90 to 100 wt%, more preferably 95 to 100 wt%, more preferably 96 to 100 wt%, of the product gas stream S3 obtained from (iii) consist of styrene, ethylbenzene, water vapor, and H2. It is preferred that the product gas stream S3 obtained from (iii) has a temperature in the range of 450 to 625 °C, more preferably 500 to 610 °C, more preferably 540 to 590 °C. It is preferred that the product gas stream S3 obtained from (iii) has a pressure in the range of 200 to 700 mbara, more preferably from 220 to 600 mbara, more preferably from 250 to 500 mbara. If heat is transferred from the product gas stream S3 obtained from (iii) to the ethylbenzene-containing stream S1 provided in (i) and / or to the H2O-containing stream S2 provided in (ii) and / or to an H2O-containing stream S4 in accordance with (iv), the product gas stream S3 obtained from (iii) may partially condense. It is preferred that the transfer of heat in (iv) is carried out by means of one or more, more preferably two or more, more preferably two or more connected in parallel, heat exchangers. It is preferred that the product gas stream S3 obtained from (iv) has a temperature in the range of 39 to 59 °C, more preferably of 42 to 58 °C, more preferably of 44 to 56 °C. It is preferred that the product gas stream S3 obtained from (iv) has a pressure in the range of 165 to 600 mbara, more preferably from 185 to 500 mbara, more preferably from 195 to 370 mbara. Preferably, the method according to (iv) and before (v) further comprises Injection of water into the product gas stream S3 obtained from (iv), wherein the product gas stream S3 obtained from the injection preferably has a temperature in the range of 39 to 59 °C, more preferably of 42 to 58 °C, more preferably of 44 to 56 °C, wherein the product gas stream S3 obtained from the injection further preferably has a pressure in the range of 240 to 320 mbara, more preferably of 260 to 300 mbara, more preferably of 270 to 290 mbara. If the product gas stream obtained from (iii) or (iv) is compressed according to (v), it is preferred that the product gas stream S3 obtained from (iii), (iv), or from injection according to the embodiment described above is compressed in (v) to a pressure in the range of 500 to 800 mbara, more preferably from 550 to 750 mbara, more preferably from 580 to 680 mbara. It is preferred that the compressed product gas stream S5 obtained from (v) has a temperature in the range of 80 to 130 °C, more preferably of 85 to 120 °C, more preferably of 90 to 110 °C. It is preferred that the FW-containing current S6 provided in (vi) has a mass flow rate in the range of 1 to 1000 t / h, more preferably from 30 to 300 t / h, more preferably from 50 to 250 t / h. It is preferred that the FW-containing current S6 provided in (vi) has a temperature in the range of 35 to 75 °C, more preferably of 40 to 70 °C, more preferably of 45 to 65 °C. It is preferred that in (vii) the FW-containing current S6 is heated to a temperature in the range of 45 to 85 °C, more preferably from 50 to 80 °C, more preferably from 55 to 75 °C. It is preferred that the heated FW-containing stream S7 obtained from (vii) has a pressure in the range of 1 to 10 bara, more preferably 1 to 8 bara, more preferably 1 to 5 bara. It is preferred that the pressure difference of the FW-containing stream S6 provided in (vi) to the pressure of the heated FW-containing stream S7 obtained from (vii) is in a range of 50 to 1000 mbara, more preferably from 150 to 600 mbara, more preferably from 250 to 300 mbara. It is preferred that in (vii) the product gas stream S3 obtained from (iii), or the product gas stream S3 obtained from (iv), or the compressed product gas stream S5 obtained from (v), is cooled to a temperature in the range of 50 to 85 °C, more preferably from 50 to 80 °C, more preferably from 50 to 75 °C. It is preferred that the cooled product gas stream S5 obtained from (vii) has a pressure in the range of 450 to 650 mbara, more preferably from 470 to 630 mbara, more preferably from 490 to 610 mbara. It is preferred that the transfer of heat in (vii) is carried out by means of one or more heat exchangers. It is preferred that the gaseous FW-containing stream S8 obtained from (vii) has a pressure in the range of 50 to 500 mbara, more preferably from 75 to 400 mbara. It is preferred that the expansion according to (viii) includes a relaxation evaporation of the heated FW-containing stream S7 obtained from (vii). It is preferred that the expansion according to (viii) is carried out by means of a pressure relief device, wherein the pressure relief device comprises one or more components selected from the group consisting of a pressure relief valve, a container, more preferably a pressure relief tank (flash tank), and a pressure relief column. It is preferred that the gaseous FW-containing stream S8 comprises 0.1 to 50 wt%, more preferably 0.2 to 25 wt%, more preferably 0.5 to 10 wt%, more preferably 1 to 2 wt%, of the heated FW-containing stream S7 obtained from (vii). It is preferred that the liquid FW-containing stream S9 comprises 50 to 99.9 wt%, more preferably 75 to 99.8 wt%, more preferably 90 to 99.5 wt%, more preferably 98 to 99 wt% of the heated FW-containing stream S7 obtained from (vii). It is preferred that in (ix) the gaseous FW-containing stream S8 is compressed to a pressure in the range of 2.7 to 6.6, more preferably from 3.0 to 5.0 bara, more preferably from 3.5 to 4.5 bara. It is preferred that the compressed FW-containing stream S10 obtained from (ix) has a temperature in the range of 138.8 to 250 °C, more preferably from 138.8 to 200 °C, more preferably from 138.8 to 180 °C. It is preferred that the compressed FW-containing stream S10 obtained from (ix) has a mass flow rate in the range of 10 to 200 t / h, more preferably from 20 to 175 t / h, more preferably from 25 to 150 t / h. Preferably the method according to (ix) further comprises (x) Returning at least part of the compressed gaseous FW-containing stream S10 obtained from (ix) to the FW-containing stream S2 provided according to (ii) or to the ethylbenzene-containing stream S1 provided according to (i). Preferably the method according to (ix), preferably according to (x) in the embodiment described herein, further comprises (xi) Separation of a gaseous FW-containing stream S12 from the gaseous FW-containing stream S10. If the process further comprises separating a gaseous FW-containing stream S12 from the gaseous FW-containing stream S10 according to (xi), it is preferred that the FW-containing stream S12 comprises 0.1 to 15 wt%, more preferably 0.75 to 10 wt%, more preferably 1 to 5 wt%, of the heated FW-containing stream S7 obtained from (vii). If the process further comprises separating a gaseous FW-containing stream S12 from the gaseous FW-containing stream S10 according to (xi), it is further preferred that the process according to (xi) further comprises (xii) Compressing the FW-containing stream S12, obtaining a compressed FW-containing stream S19. If the process comprises compressing the FW-containing stream S12 to obtain a compressed FW-containing stream S19 according to (xii), it is preferred that the FW-containing stream S12 is compressed to a pressure in the range of 4.5 to 15 bara, more preferably from 4.5 to 8.0 bara, more preferably from 4.5 to 7.0 bara. If the process comprises compressing the FW-containing stream S12 to obtain a compressed FW-containing stream S19 according to (xii), it is further preferred that the obtained compressed FW-containing stream S19 has a temperature in the range of 147.9 to 250 °C, more preferably from 147.9 to 200 °C, more preferably from 147.9 to 175 °C. If the process comprises compressing the FW-containing stream S12 to obtain a compressed FW-containing stream S19 according to (xii), it is further preferred that the obtained compressed FW-containing stream S19 has a mass flow rate in the range of 10 to 200 t / h, more preferably 20 to 175 t / h, more preferably 25 to 150 t / h. If the process comprises compressing the FW-containing stream S12 to obtain a compressed FW-containing stream S19 according to (xii), it is preferred that the process according to (xii) further comprises (xiii) Recycling at least part of the compressed FW-containing stream S19 obtained from (xii) into the FW-containing stream S2 provided according to (ii), wherein more preferably 50 to 100 wt%, more preferably 90 to 100 wt%, of the FW-containing stream S2 provided according to (ii) consists of the recycled compressed FW-containing stream S19. Preferably the method according to (viii), preferably according to (xiii), further comprises (xiv) Separation of a gaseous FW-containing stream S13 from the gaseous FW-containing stream S10. If the process comprises separating a gaseous FW-containing stream S13 from the gaseous FW-containing stream S10 according to (xiv), it is preferred that the FW-containing stream S13 comprises 0.1 to 15 wt%, more preferably 0.75 to 10 wt%, more preferably 1 to 5 wt%, of the heated FW-containing stream S7 obtained from (vii). If the process comprises separating a gaseous FW-containing stream S13 from the gaseous FW-containing stream S10 according to (xiv), it is further preferred that the process according to (xiv) further comprises (xv) Compressing the FW-containing current S13. If the method includes compressing the FW-containing stream S13 according to (xv), it is preferred that the FW-containing stream S13 according to (xv) is compressed to a pressure in the range of 1 to 15 bara, more preferably from 5.0 to 8.0 bara, more preferably from 6.0 to 7.0 bara. If the process includes compressing the FW-containing stream S13 according to (xv), it is further preferred that the compressed FW-containing stream obtained from (xv) has a temperature in the range of 110 to 250 °C, more preferably 160 to 195 °C, more preferably 170 to 185 °C. If the process includes compressing the FW-containing stream S13 according to (xv), it is further preferred that the compressed FW-containing stream obtained from (xv) has a mass flow rate in the range of 1 to 100 t / h, more preferably 40 to 80 t / h, more preferably 60 to 70 t / h. Preferably the method according to (viii) further comprises (xvi) Returning the liquid l-hO-containing stream S9 to the FhO-containing stream S6 provided in (vi). Preferably the method according to (vii) further comprises (xvii) optionally condense the cooled product gas stream obtained from (vii); (xviii) Separating the cooled product gas stream obtained from (vii) or (xvii) to obtain an FhO-containing phase, a preferably liquid organic phase, and a gas phase, wherein the organic phase comprises styrene and optionally ethylbenzene; (ixx) optionally return the l-hO-containing phase obtained in (xviii) to the l-hO-containing stream S2 provided in (ii) or to the l-hO-containing stream S6 provided in (vi); (xx) optional distillation of the organic phase obtained in (xviii) to obtain styrene. It is preferred that the process be operated continuously. Using the method described herein, FhO-containing streams can be provided, in particular for recycling into the process itself and also for further use in other processes, wherein these FhO-containing streams can be provided in various pressure and temperature ranges, preferably as steam streams. This applies in particular to the compressed gaseous l-hO-containing stream S10, the gaseous FhO-containing stream S12, the gaseous l-hO-containing stream S13, and the compressed l-hO-containing stream S19. 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 can be compressed to the extent required for the intended application. This is described in the embodiments, for example, in embodiment 51 concerning the compression of S12 to obtain S19. Compression of a gaseous H2O-containing stream can be carried out using one or more compressors, preferably a cascade of compressors. Positive displacement machines and / or turbomachines, such as screw compressors, radial blowers, radial turbo compressors (e.g., geared compressors), and / or axial turbo compressors, can be used as compressors. The compression preferably includes the addition of water to spray off the vapor after a compressor stage in order to increase the compression efficiency.Preferably, the water is sprayed to accelerate evaporation. The compressed steam can be fed into a steam network. The compressed steam can be used in the plant used for styrene production 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 0.5 to 2.0 barg. Alternatively, the compressed steam can be used in spatially adjacent plants. It can be used for heating evaporators and reactors (e.g., to reduce steam consumption from the grid). For example, compressing the steam to 3 barg may be sufficient. 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, liquid, or solid 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. 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 occur as described in those sections and the corresponding paragraphs in Reference RF1. The term "active pharmaceutical agents and / or intermediates thereof" includes 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 a 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 intermediates thereof, as well as pharmaceutical excipients, are discussed in paragraph [number].

[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 defines in more detail. The conversion steps for the production of animal feed additives, food additives for humans, and dietary supplements can be carried out by one or more synthesis steps and can be performed using conventional synthesis and techniques known to a specialist. The term "aroma chemical and aroma composition" encompasses a volatile organic substance with a molecular weight between 70 and 250 g / mol, which contains a functional group with a carbon skeleton of 5 to 16 carbon atoms, including linear, branched, cyclic, for example 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, wherein the one or more additional functional groups are preferably selected from alcohol, ether, ester, ketone, aldehyde, acetal, carboxylic acid, nitrile, thiol, or amine. In one aspect, the aroma chemical is a terpene-based aroma chemical, for example selected from monoterpenes and monoterpenoids, sesquiterpenes and sesquiterpenoids, diterpenes, triterpenes, or tetraterpenes. Aroma chemicals can be combined with other aroma chemicals to form an aroma composition. Aroma chemicals and aroma compositions are discussed in paragraph

[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 will be 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) an industrial polymer, an industrial surfactant, a descaling agent, an industrial biocide, an industrial solvent, an industrial dispersant, or a composition or formulation thereof; or iv) an agrochemical composition, an agrochemical formulation aid, or an 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, an aroma chemical, or an aroma 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 styrene and converted styrene (for example, from styrene converted to a polystyrene, a styrene-butadiene graft copolymer, a styrene-butadiene block copolymer, a styrene-acrylonitrile copolymer, an acrylonitrile-butadiene-styrene copolymer, or a cross-linked polystyrene), calculated as styrene, 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 styrene and converted styrene (for example, from styrene converted to a polystyrene, a styrene-butadiene graft copolymer, a styrene-butadiene block copolymer, a styrene-acrylonitrile copolymer, an acrylonitrile-butadiene-styrene copolymer, or a cross-linked polystyrene), calculated as styrene, 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 less, more preferably 25% by weight or less, more preferably 10% 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 the 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: Conversion of the product of the process, namely styrene, which can be obtained or is obtained by one of the above-mentioned embodiments, in order 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 bara refers to absolute pressure and the unit barg to relative pressure, where 1 bar equals 10 5 Pa corresponds. The present invention is further characterized by the following embodiments, including the individual and specific combinations of the embodiments, which are indicated by the respective dependencies. In particular, it should be noted that for each In cases where a specific number of embodiments are 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. This means that the formulation of this term is synonymous with "method according to one of embodiments 1, 2, 3, and 4" for the person skilled in the art. 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 toward preferred aspects of the present invention and thus appropriately supports, but does not constitute, the claims of the present invention. 1. Process for the production of styrene, comprising (i) Providing an ethylbenzene-containing stream S1 ; (ii) Providing a water-containing stream S2; (iii) Introducing the streams provided in (i) and (ii) into a reactor unit comprising a catalyst, and contacting the streams with the catalyst, obtaining a product gas stream S3 comprising styrene; (iv) optionally transferring heat from the product gas stream S3 obtained from (iii) to the ethylbenzene-containing stream S1 provided in (i), to the H2O-containing stream S2 provided in (ii), to an H2O-containing stream S4, to the ethylbenzene-containing stream S1 provided in (i) and to the H2O-containing stream S2 provided in (ii), to the ethylbenzene-containing stream S1 provided in (i) and to an H2O-containing stream S4, to the H2O-containing stream S2 provided in (ii) and to an H2O-containing stream S4, or to the ethylbenzene-containing stream S1 provided in (i) and to the H2O-containing stream S2 provided in (ii) and to an H2O-containing stream S4; (v) optionally compressing the product gas stream obtained from (iii) or (iv) to obtain a compressed product gas stream S5; (vi) Provision of a water-containing stream S6; (vii) Transferring heat from the product gas stream S3 obtained from (iii), or from the product gas stream S3 obtained from (iv), or from the compressed product gas stream S5 obtained from (v), to the H2O-containing stream S6, obtaining a cooled product gas stream and a heated H2O-containing stream S7; (viii) Expanding the heated H2O-containing stream S7 obtained from (vii), yielding a gaseous H2O-containing stream S8 and a liquid H2O-containing stream S9; (ix) Compressing the gaseous H2O-containing stream S8 to a pressure in the range of 2.6 to 7 bara, obtaining a compressed gaseous H2O-containing stream S10. 2. The method according to embodiment 1, wherein 90 to 100 wt%, preferably 95 to 100 wt%, more preferably 99 to 100 wt%, of the ethylbenzene-containing stream S1 provided in (i) consists of ethylbenzene. 3. The method according to embodiment 1 or 2, wherein the ethylbenzene-containing stream provided in (i) comprises S1 H2O. 4. The method according to embodiment 3, wherein 0 to 10 wt%, preferably 0 to 5 wt%, more preferably 0 to 1 wt%, of the ethylbenzene-containing stream S1 provided in (i) consists of H2O. 5. The method according to one of embodiments 1 to 4, wherein the ethylbenzene-containing stream S1 provided in (i) has a mass flow rate in the range of 1 to 300 t / h, preferably from 10 to 280 t / h, more preferably from 20 to 240 t / h. 6. The method according to one of embodiments 1 to 5, wherein 90 to 100 wt%, preferably 95 to 100 wt%, more preferably 99 to 100 wt%, of the FW-containing current S2 provided in (ii) consists of H2O. 7. The method according to one of embodiments 1 to 6, wherein the FhO-containing stream S2 provided in (ii) has a mass flow rate in the range of greater than 0 to 300 t / h, preferably from 20 to 270 t / h, more preferably from 40 to 250 t / h. 8. The method according to one of embodiments 1 to 7, wherein the FhO-containing current S2 provided in (ii) has a temperature in the range of 650 to 950 °C, preferably 750 to 900 °C, more preferably 800 to 850 °C. 9. The method according to one of embodiments 1 to 8, wherein the FhO-containing stream S2 provided in (ii) has a pressure in the range of 0.5 to 7 bara, preferably 1 to 6 bara, more preferably 1.5 to 5 bara. 10. The method according to one of embodiments 1 to 9, further comprising (ii) and before (iii) Mixing the ethylbenzene-containing stream S1 provided in (i) with the FW-containing stream S2 provided in (ii), obtaining a reaction gas stream S11; wherein in (iii) the reaction gas stream S11 is introduced into the reactor unit comprising a catalyst and contacted with the catalyst; wherein the reaction gas stream S11 preferably has a mass ratio of H2O to ethylbenzene in the range of 0.8:1 to 1.3:1, preferably in the range of 0.9:1 to 1.2:1, more preferably in the range of 1:1 to 1.1:1. 11. The method according to one of embodiments 1 to 10, wherein the reactor unit according to (iii) comprises one or more reactors, preferably two or more reactors, more preferably two reactors, each reactor comprising the catalyst. 12. The method according to embodiment 11, wherein the reactor unit comprises two or more reactors, preferably two reactors, wherein the two or more reactors are connected in series or in parallel, more preferably in series. 13. The method according to one of embodiments 1 to 12, wherein the contacting according to (iii) takes place under adiabatic conditions. 14. The method according to one of embodiments 1 to 13, wherein the contacting according to (iii) is carried out at a temperature in the range of 500 to 700 °C, preferably in a range of 525 to 675 °C, more preferably in a range of 550 to 650 °C. 15. The method according to one of embodiments 1 to 14, wherein the contacting according to (iii) is carried out at a pressure in the range of 0.1 to 1.5 bara, preferably in a range of 0.2 to 1.3 bara, more preferably in a range of 0.25 to 1.2 bara. 16. The method according to one of embodiments 1 to 15, wherein the catalyst included in the reactor unit according to (iii) comprises one or more Fe-containing compounds, wherein the one or more Fe-containing compounds preferably comprise FeO, Fe2Ü3, FeO and Fe2Ü3, wherein the catalyst preferably comprises 85 to 95 wt%, more preferably 87 to 91 wt%, of the Fe-containing compounds. 17. The method according to one of embodiments 1 to 16, wherein the catalyst included in the reactor unit according to (iii) comprises Cr, wherein the catalyst preferably comprises 1.7 to 2.3 wt%, preferably 1.9 to 2.1 wt%, Cr. 18. The method according to one of embodiments 1 to 17, wherein the catalyst included in the reactor unit according to (iii) comprises KOH, wherein the catalyst preferably comprises 7 to 11 wt%, preferably 8 to 10 wt%, KOH. 19. The method according to one of embodiments 1 to 18, wherein the product gas stream S3 obtained from (iii) comprises styrene from 18 to 36 wt%, preferably from 20 to 34 wt%, more preferably from 22 to 32 wt%. 20. The method according to one of embodiments 1 to 19, wherein the product gas stream S3 obtained from (iii) comprises ethylbenzene from 12 to 34 wt%, preferably from 14 to 32 wt%, more preferably from 15.5 to 29 wt%. 21. The method according to one of embodiments 1 to 20, wherein the product gas stream S3 obtained from (iii) comprises water vapor of 40 to 65 wt.%, preferably of 45 to 60 wt.%, more preferably of 50 to 55 wt.%. 22. The method according to one of embodiments 1 to 21, wherein the product gas stream S3 obtained from (iii) comprises H2 in 0.3 to 1.3 wt%, preferably in 0.35 to 0.8 wt%, more preferably in 0.4 to 0.6 wt%. 23. The method according to one of embodiments 1 to 22, wherein 90 to 100 wt%, preferably 95 to 100 wt%, more preferably 96 to 100 wt%, of the product gas stream S3 obtained from (iii) consists of styrene, ethylbenzene, water vapor, and H2. 24. The method according to one of embodiments 1 to 23, wherein the product gas stream S3 obtained from (iii) has a temperature in the range of 450 to 625 °C, preferably 500 to 610 °C, more preferably 540 to 590 °C. 25. The method according to one of embodiments 1 to 24, wherein the product gas stream S3 obtained from (iii) has a pressure in the range of 200 to 700 mbara, preferably 220 to 600 mbara, more preferably 250 to 500 mbara. 26. The method according to one of embodiments 1 to 25, wherein the transfer of heat in (iv) is carried out by means of one or more, preferably two or more, more preferably two or more connected in parallel, heat exchangers. 27. The method according to one of embodiments 1 to 26, wherein the product gas stream S3 obtained from (iv) has a temperature in the range of 70 to 150 °C, preferably 85 to 140 °C, more preferably 90 to 120 °C. 28. The method according to one of embodiments 1 to 27, wherein the product gas stream S3 obtained from (iv) has a pressure in the range of 165 to 600 mbara, preferably 185 to 500 mbara, more preferably 195 to 370 mbara. 29. The method according to one of embodiments 1 to 28, further comprising injecting water into the product gas stream S3 obtained from (iv) after (iv) and before (v), wherein the product gas stream S3 obtained from the injection preferably has a temperature in the range of 39 to 59 °C, more preferably of 42 to 58 °C, more preferably of 44 to 56 °C, wherein the product gas stream S3 obtained from the injection further preferably has a pressure in the range of 240 to 320 mbara, more preferably of 260 to 300 mbara, more preferably of 270 to 290 mbara. 30. The method according to one of embodiments 1 to 29, wherein the product gas stream S3 obtained from (iii), (iv), or from injection according to embodiment 29 is compressed in (v) to a pressure in the range of 500 to 800 mbara, preferably 550 to 750 mbara, more preferably 580 to 680 mbara. 31. The method according to one of embodiments 1 to 30, wherein the compressed product gas stream S5 obtained from (v) has a temperature in the range of 80 to 130 °C, preferably 85 to 120 °C, more preferably 90 to 110 °C. 32. The method according to one of embodiments 1 to 31, wherein the FhO-containing stream S6 provided in (vi) has a mass flow rate in the range of 1 to 1000 t / h, preferably 30 to 300 t / h, more preferably 50 to 250 t / h. 33. The method according to one of embodiments 1 to 32, wherein the FhO-containing current S6 provided in (vi) has a temperature in the range of 35 to 75 °C, preferably 40 to 70 °C, more preferably 45 to 65 °C. 34. The method according to one of embodiments 1 to 33, wherein in (vii) the FhO-containing stream S6 is heated to a temperature in the range of 45 to 85 °C, preferably 50 to 80 °C, more preferably 55 to 75 °C. 35. The method according to one of embodiments 1 to 34, wherein the heated FhO-containing stream S7 obtained from (vii) has a pressure in the range of 1 to 10 bara, preferably 1 to 8 bara, more preferably 1 to 5 bara. 36. The method according to one of embodiments 1 to 35, wherein the difference between the pressure of the FW-containing stream S6 provided in (vi) and the pressure of the heated FW-containing stream S7 obtained from (vii) is in a range of 50 to 1000 mbara, preferably 150 to 600 mbara, more preferably 250 to 300 mbara. 37. The method according to one of embodiments 1 to 36, wherein in (vii) the product gas stream S3 obtained from (iii), or the product gas stream S3 obtained from (iv), or the compressed product gas stream S5 obtained from (v), is cooled to a temperature in the range of 50 to 85 °C, preferably from 50 to 80 °C, more preferably from 50 to 75 °C. 38. The method according to one of embodiments 1 to 37, wherein the cooled product gas stream S5 obtained from (vii) has a pressure in the range of 450 to 650 mbara, preferably 470 to 630 mbara, more preferably 490 to 610 mbara. 39. The method according to one of embodiments 1 to 38, wherein the transfer of heat in (vii) is carried out by means of one or more heat exchangers. 40. The method according to one of embodiments 1 to 39, wherein the gaseous FhO-containing stream S8 obtained from (vii) has a pressure in the range of 50 to 500 mbara, more preferably from 75 to 400 mbara. 41. The method according to one of embodiments 1 to 40, wherein the expansion according to (viii) comprises a flash evaporation of the heated FW-containing stream S7 obtained from (vii). 42. The method according to one of embodiments 1 to 41, wherein the expansion according to (viii) is carried out by means of a pressure relief device, the pressure relief device comprising one or more components selected from the group consisting of a pressure relief valve, a container, preferably a pressure relief tank (flash tank), and a pressure relief column. 43. The method according to one of embodiments 1 to 42, wherein the gaseous H2O-containing stream S8 comprises 0.1 to 50 wt.%, preferably 0.2 to 25 wt.%, more preferably 0.5 to 10 wt.%, more preferably 1 to 2 wt.%, of the heated FW-containing stream S7 obtained from (vii). 44. The method according to one of embodiments 1 to 43, wherein the liquid FhO-containing stream S9 comprises 50 to 99.9 wt.%, preferably 75 to 99.8 wt.%, more preferably 90 to 99.5 wt.%, more preferably 98 to 99 wt.%, of the heated FW-containing stream S7 obtained from (vii). 45. The method according to one of embodiments 1 to 44, wherein in (ix) the gaseous FhO-containing stream S8 is compressed to a pressure in the range of 2.7 to 6.6, preferably from 3.0 to 5.0 bara, more preferably from 3.5 to 4.5 bara. 46. ​​The method according to one of embodiments 1 to 45, wherein the compressed FhO-containing stream S10 obtained from (ix) has a temperature in the range of 138.8 to 250 °C, preferably from 138.8 to 200 °C, more preferably from 138.8 to 180 °C. 47. The method according to one of embodiments 1 to 46, wherein the compressed FhO-containing stream S10 obtained from (ix) has a mass flow rate in the range of 10 to 200 t / h, preferably 20 to 175 t / h, more preferably 25 to 150 t / h. 48. The method according to one of embodiments 1 to 47, further comprising according to (ix) (x) Returning at least part of the compressed gaseous FW-containing stream S10 obtained from (ix) to the FW-containing stream S2 provided according to (ii) or to the ethylbenzene-containing stream S1 provided according to (i). 49. The method according to one of embodiments 1 to 48, further comprising (ix), preferably (x) according to embodiment 48 (xi) Separation of a gaseous FW-containing stream S12 from the gaseous FhO-containing stream S10. 50. The method according to embodiment 49, wherein the FhO-containing stream S12 comprises 0.1 to 15 wt%, preferably 0.75 to 10 wt%, more preferably 1 to 5 wt%, of the heated FW-containing stream S7 obtained from (vii). 51. The method according to embodiment 49 or 50, further comprising according to (xi) (xii) Compressing the FW-containing stream S12, obtaining a compressed H2O-containing stream S19. 52. The method according to embodiment 51, wherein the FhO-containing stream S12 is compressed to a pressure in the range of 4.5 to 15 bara, preferably from 4.5 to 8.0 bara, more preferably from 4.5 to 7.0 bara. 53. The method according to embodiment 51 or 52, wherein the obtained compressed H2O-containing stream S19 has a temperature in the range of 147.9 to 250 °C, preferably from 147.9 to 200 °C, more preferably from 147.9 to 175 °C. 54. The method according to one of the embodiments 51 to 53, wherein the obtained compressed FhO-containing stream S19 has a mass flow rate in the range of 10 to 200 t / h, preferably from 20 to 175 t / h, more preferably from 25 to 150 t / h. 55. The method according to one of the embodiments 51 to 54, further comprising (xii) (xiii) recycling at least a part of the compressed FhO-containing stream S19 obtained from (xii) into the FW-containing stream S2 provided according to (ii), wherein preferably 50 to 100 wt%, more preferably 90 to 100 wt%, of the FW-containing stream S2 provided according to (ii) consists of the recycled compressed FW-containing stream S19. 56. The method according to one of embodiments 1 to 55, further comprising (viii), preferably (xiii) (xiv) Separation of a gaseous FW-containing stream S13 from the gaseous FhO-containing stream S10. 57. The method according to embodiment 56, wherein the FhO-containing stream S13 comprises 0.1 to 15 wt%, preferably 0.75 to 10 wt%, more preferably 1 to 5 wt%, of the heated FW-containing stream S7 obtained from (vii). 58. The method according to embodiment 56 or 57, further comprising (xiv) (xv) Compressing the FW-containing current S13. 59. The method according to embodiment 58, wherein the FhO-containing stream S13 according to (xv) is compressed to a pressure in the range of 1 to 15 bara, preferably from 5.0 to 8.0 bara, more preferably from 6.0 to 7.0 bara. 60. The method according to embodiment 58 or 59, wherein the compressed H2O-containing stream obtained from (xv) has a temperature in the range of 110 to 250 °C, preferably 160 to 195 °C, more preferably 170 to 185 °C. 61. The method according to one of embodiments 58 to 60, wherein the compressed H2O-containing stream obtained from (xv) has a mass flow rate in the range of 1 to 100 t / h, preferably 40 to 80 t / h, more preferably 60 to 70 t / h. 62. The method according to one of embodiments 1 to 61, further comprising according to (viii) (xvi) recycling the liquid H2O-containing stream S9 into the provided in (vi) H2O-containing electricity S6. 63. The method according to any one of embodiments 1 to 62, further comprising according to (vii) (xvii) optionally condensing the cooled product gas stream obtained from (vii); (xviii) separating the cooled product gas stream obtained from (vii) or (xvii) to obtain a H2O-containing phase, a preferably liquid organic phase, and a gas phase, wherein the organic phase comprises styrene and optionally ethylbenzene; (ixx) optionally return the H2O-containing phase obtained in (xviii) to the H2O-containing stream S2 provided in (ii) or to the H2O-containing stream S6 provided in (vi); (xx) optional distillation of the organic phase obtained in (xviii) to obtain styrene. 64. The method according to one of embodiments 1 to 63, wherein the method is operated continuously. The present invention is further illustrated by the following reference examples, examples and comparative examples. EXAMPLES Comparative example 1: Production of styrene In a plant with a styrene production rate of approximately 64 t / h, 44 t / h of steam are required at a pressure of 1.7 bar and 90 t / h of steam at a pressure of 4 bar. A simplified representation of the plant is shown in Figure 1. In the heat exchanger downstream of the reactors, 37 t / h of steam are generated through heat recovery. Therefore, 97 t / h of steam are required for dehydrogenation. Example 2: Production of styrene according to the present invention In a plant with a styrene production rate of approximately 64 t / h, 44 t / h of steam are required at a pressure of 1.7 bar and 90 t / h of steam at a pressure of 4 bar. A simplified representation of the plant is shown in Figure 2. Alternatively, the process can also be carried out in a simplified plant as shown in Figure 3, which includes an additional compressor for compressing the product gas stream. 37 t / h of steam are generated in the heat exchanger downstream of the reactors through heat recovery. Thus, 97 t / h of steam are required for dehydrogenation. To further recover condensation heat from the product gas stream leaving the reactors, a heat pump is integrated, which uses water as a refrigerant. This generates steam, some of which is then reused in the process. Using green electricity to operate these additional plant components further reduces the CO2 footprint. Description of the illustrations Figure 1: shows a simplified representation of a plant for the production of styrene, in particular comprising a steam superheater for generating steam, a first and a second reactor, several heat exchangers and condensers or air coolers. Figure 2: shows a simplified representation of a plant for the production of styrene according to the present invention, in particular comprising a steam superheater for generating steam, a first and a second reactor, several heat exchangers and condensers or air coolers, and in particular a heat pump condenser. Figure 3 shows a simplified representation of a plant for the production of styrene according to the present invention, in particular comprising a steam superheater for generating steam, a first and a second reactor, several heat exchangers and condensers or air coolers, and in particular a heat pump condenser. In addition to the plant shown in Figure 2, the plant includes a compressor A16 for compressing the product gas stream. List of reference symbols 51 Ethylbenzene-containing current 52 H2O-containing electricity 53 Product gas flow 54 H2O-containing electricity 55 compressed product gas stream 56 FhO-containing electricity 57 heated FhO-containing current 58 gaseous FhO-containing current 59 liquid FhO-containing electricity 510 compressed gaseous FhO-containing current 511 Reaction gas stream 512 FhO-containing current separated from S10 513 FhO-containing current separated from S10 514 Combustion air and additional fuel 515 Exhaust gas 516 steam to other consumers 517 Organic phase comprising styrene and ethylbenzene for purification / distillation 518 Process water for purification 519 compressed FhO-containing current 520 steam to other consumers 521 Steam for export to the factory network 522 Dehydration gas A1 Steam superheater / Oven A2 first reactor A3 second reactor A4 inlet superheater A5 steam generator A6 Inlet evaporator A7 Condenser / Air Cooler A8 Gas / Liquid Separator A9 Liquid / Liquid Separator A10 Dehydration gas compressor A11 Condenser / Air cooler for aromatic recovery A12 heat pump condenser A13 Flash circuit pump A14 Degassing column A15 compressor A16 compressor A17 compressor A18 Process Compressor Cited literature - DE 3147323 A1 - US 5386075 - US 2012 / 149960 A1 - EP 2651859 B1

Claims

Claims 1. Process for the production of styrene, comprising (I) Providing an ethylbenzene-containing stream S1 ; (ii) Providing a water-containing stream S2; (iii) Introducing the streams provided in (i) and (ii) into a reactor unit comprising a catalyst, and contacting the streams with the catalyst, obtaining a product gas stream S3 comprising styrene; (iv) optionally transfer heat from the product gas stream S3 obtained from (iii) to the ethylbenzene-containing stream S1 provided in (i) and / or to the H2O-containing stream S2 provided in (ii) and / or to an H2O-containing stream S4; (v) optionally compressing the product gas stream obtained from (iii) or (iv) to obtain a compressed product gas stream S5; (vi) Provision of a water-containing stream S6; (vii) Transferring heat from the product gas stream S3 obtained from (iii), or from the product gas stream S3 obtained from (iv), or from the compressed product gas stream S5 obtained from (v), to the H2O-containing stream S6, obtaining a cooled product gas stream and a heated H2O-containing stream S7; (viii) Expanding the heated H2O-containing stream S7 obtained from (vii), yielding a gaseous H2O-containing stream S8 and a liquid H2O-containing stream S9; (ix) Compressing the gaseous H2O-containing stream S8 to a pressure in the range of 2.6 to 7 bara, obtaining a compressed gaseous H2O-containing stream S10.

2. The method according to claim 1, wherein 90 to 100 wt% of the ethylbenzene-containing stream S1 provided in (i) consists of ethylbenzene.

3. The method according to claim 1 or 2, further comprising, after (ii) and before (iii), mixing the ethylbenzene-containing stream S1 provided in (i) with the H2O-containing stream S2 provided in (ii), obtaining a reaction gas stream S11; wherein, in (iii), the reaction gas stream S11 is introduced into the reactor unit comprising a catalyst and contacted with the catalyst.

4. The method according to any one of claims 1 to 3, wherein the reactor unit according to (iii) comprises one or more reactors, each reactor comprising the catalyst.

5. The method according to any one of claims 1 to 4, wherein the product gas stream S3 obtained from (iii) comprises 18 to 36 wt% styrene.

6. The method according to any one of claims 1 to 5, wherein the product gas stream S3 obtained from (iii) comprises 40 to 65 wt% water vapor.

7. The method according to any one of claims 1 to 6, wherein the product gas stream S3 obtained from (iii) comprises 0.3 to 1.3 wt% H2.

8. The method according to any one of claims 1 to 7, wherein the product gas stream S3 obtained from (iii) has a pressure in the range of 200 to 700 mbara.

9. The method according to any one of claims 1 to 8, wherein the transfer of heat in (iv) is carried out by means of one or more heat exchangers.

10. The method according to any one of claims 1 to 9, wherein the product gas stream S3 obtained from (iii) or (iv) is compressed in (v) to a pressure in the range of 500 to 800 mbara, preferably 550 to 750 mbara, more preferably 580 to 680 mbara.

11. The method according to any one of claims 1 to 10, wherein the cooled product gas stream S5 obtained from (vii) has a pressure in the range of 450 to 650 mbara.

12. The method according to any one of claims 1 to 11, wherein the gaseous FhO-containing stream S8 obtained from (vii) has a pressure in the range of 50 to 500 mbara.

13. The method according to any one of claims 1 to 12, wherein the compressed FhO-containing stream S10 obtained from (ix) has a mass flow rate in the range of 10 to 200 t / h.

14. The method according to any one of claims 1 to 13, further comprising according to (ix) (x) Returning at least part of the compressed gaseous l-hO-containing stream S10 obtained from (ix) to the l-hO-containing stream S2 provided according to (ii) or to the ethylbenzene-containing stream S1 provided according to (i).

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

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