Process for utilizing acrylic acid production waste streams by gasification and fermentation

Abstract

The present invention concerns a process for utilizing waste streams from an acrylic acid production plant by gasification and fermentation, and an acrylic acid production plant comprising the necessary units for utilizing waste streams generated during acrylic acid production, separation and upgrading. The process comprises conversion of a high caloric first waste stream W1 purged from the separation unit and optionally a high caloric fifth waste stream W5 purged from the upgrading unit of the acrylic acid production plant by a gasification process comprising at least one gasifier into synthesis gas. The process further comprises conversion of an aqueous second waste stream W2 purged from the separation unit and optionally a sixth waste stream W6 purged from the upgrading unit of the acrylic acid production plant by a fermentation process comprising at least one anaerobic fermentation unit into a mixture of CH4 and CO2. Both synthesis gas and the mixture of CH4 and CO2 can then be utilized e.g., for production of chemicals in a chemical production plant.

Description

Process for utilizing acrylic acid production waste streams by gasification and fermentationTechnical areaThe present invention relates to a process utilizing acrylic acid production waste streams, an acrylic acid production plant comprising an integrated production waste streams treatment facility and the use of said plant for said process. of the inventionAcrylic acid is an important commodity in the chemical industry. Accordingly, large amounts of waste streams are formed during synthesis and / or purification of crude acrylic acid and / or its upgrading into purified acrylic acid.Acrylic acid is manufactured in an acrylic acid synthesis unit by a heterogeneously catalyzed gas phase partial oxidation from propene as a starting material which results in a product gas mixture. Crude acrylic acid is then separated from the product gas mixture in an acrylic acid separation unit by methods such as condensation and absorption. The crude acrylic acid is then further purified in an acrylic acid upgrading unit by methods such as distillation, crystallization, or variants of said methods such as solvent-added distillation, solvent-free distillation, azeotropic distillation and combinations of extraction and distillation. Said methods can be combined in said acrylic acid upgrading unit. A general description of acrylic acid manufacture and purification of crude acrylic acid is disclosed in Ullmann's Encyclopedia of Industrial Chemistry, Chapter "Acrylic acid and derivatives”, T. Ohara et al., pages 6-10 (DOI: 10.1002 / 14356007.a01_161.pub4).A standard method for treatment of waste streams from acrylic acid production is incineration of said waste streams for example in a boiler in which steam can be produced. Thereby, undesired CO2 is formed.Another process for treating acrylic acid production waste streams is disclosed in CN117263793A. The process disclosed therein comprises the following steps: (1) a heavy component diluent blending process; (2) a light component de-aldehyding process; (3) a light component maleic anhydride removal process; optionally, (4) a waste gas recycling process.It is an objective of the present invention to utilize the acrylic acid production waste streams described above in a more environmentally friendly way than incineration and the above-described process comprising four steps.It is a further objective of the present invention to provide a process and an acrylic acid production plant which convert at least a portion of the waste streams into feedstocks for the chemical industry.Summary of the inventionThese problems are solved by a process for utilizing at least one waste stream from an acrylic acid production plant, wherein the acrylic acid production plant comprises a) an acrylic acid production unit, b) an acrylic acid separation unit, and c) an acrylic acid upgrading unit, the process comprising the steps(i) providing a first waste stream W1 , wherein the first waste stream W1 is separated from the acrylic acid separation unit,(ii) providing a second waste stream W2, wherein the second waste stream W2 is separated from the acrylic acid separation unit,(iia) optionally providing a fifth waste stream W5 and / or a sixth waste stream W6 and / or a further feedstock F, wherein said optional fifth waste stream W5 and said optional sixth waste stream W6 are separated from the acrylic acid upgrading unit,(iii) optionally pretreating the first waste stream W1 and / or the second acrylic acid waste stream W2, and / or the optional fifth waste stream W5 and / or the optional sixth waste stream W6 and / or the optional further feedstock F,(iv) subjecting the first waste stream W1 provided in step (i) or optionally after pretreatment in step (iii) and the optional fifth waste stream W5 to a gasification process wherein said gasification process at a temperature between 800 and 1500 °C, comprises at least one gasifier G and thereby forming a gas stream GS1 wherein said gas stream GS1 comprises H2 and CO, wherein said gas stream GS1 is purified in an optional step (ivb) whereby a gas stream GS11 is formed, and(v) subjecting the second waste stream W2 provided in step (ii) or optionally after pretreatment in step (iii) and the optional sixth waste stream W6 to an anaerobic fermentation process AFP in at least one anaerobic fermentation unit AFU and thereby forming a gas stream GS2 wherein said gas stream GS2 comprises CO2 and CH4.These problems are further solved by an acrylic acid production plant comprising an integrated waste stream treatment facility wherein said acrylic acid production plant comprises a) an acrylic acid production unit AAPU, b) an acrylic acid separation unit AASU downstream and fluidically connected to said acrylic acid production unit AAPU, said acrylic acid separation unit AASU purging a first waste stream W1, c) an acrylic acid upgrading unit AAUU downstream and fluidically connected to said acrylic acid separation unit AASU, d) at least one gasifier G downstream and directly or indirectly fluidically connected to said acrylic acid separation unit AASU ande) at least one anaerobic fermentation unit AFU downstream of and directly or indirectly fluidically connected to said acrylic acid separation unit AASU.Further aspects of the present invention will become apparent to the person skilled in the art directly from the foregoing and following description and the examples.Figure 1 shows schematically the process according to the present invention for the first waste stream W1 and the second waste stream W2.Figure 2 shows schematically process according to the present invention for the first waste stream W1 and the second waste stream W2, the optional fifth waste stream W5 and the optional sixth waste stream W6.Figure 3 shows schematically the further utilization of gas stream GS1 (optional step (ivb)), gas stream GS2 (optional step (vi)) and optional gas stream GS3.Figure 4 shows schematically the further utilization of gas stream GS2.Detailed description of the inventionThe present invention is further described below with reference to the embodiments, but the present invention is not limited to these embodiments, and any modifications of these embodiments, combinations of these embodiments or substitutions within the basic spirit of the present invention are still within the scope of the present invention as claimed.Definitions:In the context of the present description and the accompanying claims, the term "about” preferably means a deviation of the thus described value of ±10 %. In the context of the present invention, the term “combinations thereof' is inclusive of one or more of the recited elements. In the context of the present invention, the term “mixture thereof” is inclusive of one or more of the recited elements.“Refuse-derived fuel” (RDF) is defined herein as a fuel produced form various types of waste such as municipal solid waste (MSW), industrial waste or commercial waste. RDF consists largely of combustible components of such waste, as non-recyclable plastics (not including PVC), paper cardboard, labels, and other corrugated materials. These fractions are separated by different processing steps, such as screening, air classification, ballistic separation, separation of ferrous and non-ferrous materials, glass, stones, and other foreign materials and shredding into a uniform grain size, or also pelletized to produce a homogeneous material which can be used as a feedstock for gasification processes (Y. Yang et al., Gasification of refuse-derived fuel from municipal solid waste for energy production: a review, Environmental Chemistry Letters (2021) 19, 2127-2140 (https: / / doi.org / 10.1007 / s10311-020-01177-5).The term “downstream of” is defined herein in respect to a succession of unit operations as located next to on the side which is in the flow direction of fluids passing said succession of unit operations.The term "fluidically connected to” in respect to two or more units is defined herein that a fluid such as a particulate solid, liquids, gases, and mixtures thereof can flow from one of such unit to the other such unit and flow through and / or along such an analytical unit. Two units "fluidically connected to” each other are for example connected by one or more pipes which each other or by screw conveyors or by extruders or by solids pumps."Reactive distillation” is defined herein as a process where the chemical reactor is also the still. In contrast, "solvent- added distillation”, "solvent-free distillation”, "azeotropic distillation”, "distillation” and combinations of "extraction” and "distillation” are not considered as "reactive distillation” herein."Solvent-free distillation” is defined herein as a distillation for which no extra solvent is added to the mixture which is subjected to the distillation process.The process for utilizing waste streams from an acrylic acid production plant according to the present invention is schematically shown in Figures 1 and 2 and is described below in detail.Several processes to produce acrylic acid are known und commercially used. In general, such processes utilize an acrylic acid production plant comprising an acrylic acid production unit AAPU, an acrylic acid separation unit AASU which is downstream and fluidically connected to said acrylic acid production unit AAPU, and an acrylic acid upgrading unit AAUU which is downstream and fluidically connected to said acrylic acid separation unit AASU.In the acrylic acid production unit AAPU, usually two separate reaction steps are utilized. The product stream formed in the acrylic acid production unit AAPU from the starting material(s) SM is a "product gas mixture” PGM which comprises acrylic acid.The product gas mixture PGM formed in the acrylic acid production unit AAPU is then fed into the acrylic acid separation unit AASU which is downstream of and fluidically connected to the acrylic acid production unit AAPU. Crude acrylic acid is then separated from the product gas mixture PGM in an acrylic acid separation unit AASU. Crude acrylic acid CAA is then purified in the acrylic acid upgrading unit AAUU whereby upgraded acrylic acid UAA is formed.The preparation of acrylic acid in the acrylic acid production unit AAPU is described hereinafter in more detail: the gas phase partial oxidation itself can be conducted as described in the prior art. Proceeding from propene as starting material SM, the gas phase partial oxidation can be conducted, for example and preferably, in two successive oxidation stages, as described in EP 0 700 714 A1 and in EP 0 700 893 A1. It is of course also possible to employ for example the gas phase partial oxidations cited in DE 197 40 253 A1 and in DE 197 40 252 A1.In principle, the gas phase partial oxidation can also be conducted as described in documents US 2006 / 0161019, WO 2006 / 092410, WO 2006 / 002703, WO 2006 / 002713, WO 2005 / 113127, DE 10 2004 021 763 A1, EP 1 611 076 A1, WO 2005 / 108342, EP 1 656 335 A1, EP 1 682 478 A1, EP 1 682 477 A1, DE 10 2006 054214 A1, DE 10 2006 024 901 A1, EP 1 611 080 A2, EP 1 734030 A1, DE 10 2006 000 996 A1, DE 10 2005062 026 A1, DE 10 2005 062 010 A1, WO 2007 / 060036, WO 2007 / 051750 and WO 2007 / 042457. The propene source used for this purpose may be polymer grade propene or chemical grade propene according to DE 102 32 748 A1. If the C3 precursor used is propane, the partial oxidation can be also conducted as described in DE 102 45 585 A1.Typically, the acrylic acid-comprising product gas mixture PGM from a heterogeneously catalyzed gas phase partial oxidation of C3 starting materials SM (preferably propene) of acrylic acid with molecular oxygen over catalysts in the solid state as described above may have, for example, the following contents: 1% to 30% by weight of acrylic acid, 0.05% to 10% by weight of molecular oxygen, 1% to 30% by weight of water, > 0% to 5% by weight of acetic acid, > 0% to 3% by weight of propionic acid, > 0% to 1% by weight of maleic acid and / or maleic anhydride, 0% to 2% by weight of acrolein, 0% to 1 % by weight of formaldehyde, > 0% to 1 % by weight of furfurals, > 0% to 0.5% by weight of benzaldehyde, 0% to 1% by weight of propene, and as the remaining amount essentially inert gases, for example nitrogen, carbon monoxide, carbon dioxide, methane and / or propane.Next, the product gas mixture PGM formed in the acrylic acid production unit AAPU is then fed into an acrylic acid separation unit AASU which is downstream of and fluidically connected to the acrylic acid production unit AAPU.The acrylic acid separation unit AASU can utilize different methods for separating crude acrylic acid CAA from the product gas mixture PGM, for example, one or more absorption columns or one or more condensers. A first waste stream W1, a second waste stream W2 and a third waste stream W3 are separated from the product gas mixture PGM in the acrylic acid separation unit AASU.The specific set-up of the acrylic acid separation unit AASU depends on the acrylic acid upgrading method applied in the acrylic acid upgrading unit AAUU and the successive upgrading method employed to obtain upgraded acrylic acid UAA from crude acrylic acid CAA.In a preferred aspect of the present invention, the acrylic acid separation unit AASU comprises one or more absorption columns, more preferably one absorption column, in which a first waste stream W1, a second waste stream W2 and a third waste stream W3 are separated from the product gas mixture PGM. Optionally, the product gas mixture PGM is cooled down in an optional quench unit before entering said absorption column. The optional quench unit may be any of the apparatuses known from this purpose in the prior art (for example an empty column without internals in which the product gas mixture PGM enters said column at the top and the liquid is sprayed into said column via spray nozzles, spray scrubbers, Venturi scrubbers, bubble columns or other apparatuses with surfaces over which liquid trickles), preference being given to using Venturi scrubbers or spray coolers. The absorption columnpreferably comprises at least one bottom section outlet, at least one top section outlet and at least one middle section outlet.In a preferred aspect of the invention, the crude acrylic acid CAA is leaving said absorption column through a middle section outlet, preferably a first middle section outlet. The first waste stream W1 is leaving said absorption column through the bottom section outlet of said absorption column. The second waste stream W2 is leaving said absorption outlet through a second middle outlet of said absorption column wherein said second middle section outlet is closer to the top section outlet of said absorption column than the first middle section outlet. The third waste stream W3 is leaving said absorption column through the top section outlet of said absorption column.The site of introduction for the product gas mixture PGM from the acrylic acid production unit AAPU that has been quenched (or cooled in some other way or not cooled) into the absorption column in this preferred aspect of the present invention is advantageously in the bottom space of that column, which advantageously comprises a centrifugal droplet separator in integrated form and is generally separated from the lowermost separating internal by a first chimney tray which is preferably above the inlet of the column. In that case, first waste stream W1 (= "high boiler fraction” of the product gas mixture PGM) is constantly directed into the bottom of the condensation column via a connecting conduit or via an overflow. In an illustrative and preferred execution variant (which is described exclusively hereinafter without restriction of general ability for implementation), this is the first dual-flow tray of a first series of dual-flow trays that are appropriately arranged equidistantly. The chimney tray functions simultaneously as collecting tray, whereby the first waste stream W1 stays below said chimney tray. The first waste stream W1 is withdrawn continuously and at least a portion thereof is run into the bottom space and therefrom purged from said column. The first series of dual-flow trays is concluded by a second chimney tray (collecting tray). From this second chimney tray, in the first side draw, crude acrylic acid is withdrawn continuously as medium boiler fraction, preferably having a purity of > 90% by weight or > 95% by weight.In the same preferred aspect of the invention, the second waste stream W2 is preferably withdrawn continuously from the third collecting tray in the second side draw. A portion of the second waste stream W2 withdrawn is recycled into the condensation column at the uppermost of the crossflow mass transfer trays. Another portion of the second waste stream W2 withdrawn is cooled by indirect heat exchange, appropriately split, and likewise recycled into the column. A cooled portion is recycled here to the uppermost valve tray (at a temperature of 15 to 30 °C, preferably 20 to 25 °C), and the other cooled portion to a valve tray disposed roughly in the middle between the third collecting tray and the uppermost valve tray (at a temperature of 20 to 35 °C, preferably 25 to 30 °C). The amount of crude acrylic acid CAA present can be separated in accordance with the invention from the residual amount of the second waste stream W2 withdrawn. The second waste stream W2 comprises about 70 to 85 wt.-% water.In the same preferred aspect of the present invention, the constituents that are more volatile than water are drawn off in gaseous form as third waste stream W3 at the top of said column and is normally recycled into the acrylic acidproduction unit AAPU as diluent gas (cycle gas). The portion of the third waste stream W3 is not recycled into the production unit AAPU as diluent gas is normally sent to incineration.In another preferred aspect of the present invention, a portion of water comprised in the second waste stream W2 is removed from the second waste stream W2 in step (ill), for example, in a means suitable for evaporating water from a liquid mixture, such as an evaporator. More preferably, at least 50 wt.-% of the water and most preferably at least 70 wt.-% or 80 wt.-% of the water comprised in the second waste stream W2 are removed from the second waste stream W2 in step (ill). Reducing the water content in the second waste stream W2 reduces the overall volume to be treated in step (v).In case the acrylic acid separation unit AASU which comprises two or more columns, preferably one or more absorption columns, the acrylic acid production waste streams may consist of the first waste stream W1 and the third waste stream W3 only. In all such processes, the first waste stream W1 is purged in one or more (absorption) columns as bottom product and the third waste stream W1 is purged as a gas mixture on one or more (absorption) columns as top product. The further treatment of the first waste stream W1 and the third waste stream W3 is the same as in case of the first waste stream W1 and the third waste stream W3 are purged from an acrylic acid separation unit AASU comprising only one (absorption) column as described above.The crude acrylic acid CAA leaving the acrylic acid separation unit AASU is then fed into the acrylic acid upgrading unit AAUU from which upgraded acrylic acid UAA in the desired purity grade is obtained. Desired purity grades of acrylic acid are for example > 98 % for utilization of acrylic acid in a successive esterification reaction in the production of acrylates and > 99 % for utilization of acrylic acid in the production of polymers. Crude acrylic acid (CAA) has a purity in the range of 60 to 90 %.The acrylic acid upgrading unit AAUU can utilize different methods for purifying the crude acrylic acid CAA into the upgraded acrylic acid UAA, said methods comprise crystallization, solvent-added distillation, solvent-free distillation, azeotropic distillation, reactive distillation, extraction and combinations thereof.Purification methods applied in the acrylic acid upgrading unit AAUU comprise distillation or crystallization. The acrylic acid upgrading unit AAUU is downstream of and fluidically connected to the acrylic acid separation unit AASU.The acrylic acid separation unit AASU preferably comprising one column, preferably one absorption column as described in detail above is preferably combined with an acrylic acid upgrading unit AAUU utilizing either crystallization or distillation as purification method. Said distillation method is preferably a solvent-free distillation method i.e., in which no extra solvent is added.A preferred type of acrylic acid upgrading unit AAUU utilizing crystallization as purification method which is preferably combined in an acrylic acid production plant with an acrylic acid separation unit AASU comprising one absorption column.The crystallization method preferably used is not subject to any restriction in principle. The crystallization can be conducted continuously or batchwise, in one or more stages, up to any degree of purity.The crystallization can be for example executed as a suspension crystallization, as described in column 10 of DE 199 24 532 A1 or in example 1 of DE 102 23 058 A1 (for example in a cooling disk crystallizer as described in WO 2006 / 111565). The acrylic acid crystals formed in suspension crystallization can be separated from the remaining mother liquor in the case of esterification grade acrylic acid in a centrifuge (for example a 2- or 3-stage pusher centrifuge), in which case the crystals removed are advantageously washed on the centrifuge by means of molten pure crystals. If the suspension crystals are separated from the remaining mother liquor by means of a scrubbing column, for example a melt scrubbing column (for example one according to WO 01 / 77056, or DE 101 56 016 A1, or DE 102 23 058 A1, or as described in WO 2006 / 111565, WO 04 / 35514, WO 03 / 41833, WO 02 / 09839, WO 03 / 41832, DE 100 36 881 A1, WO 02 / 55469 and WO 03 / 78378). Crystallization can also be performed as a fractional falling film crystallization, as disclosed in EP 0 616 998 A1.Another method which can be used in an acrylic acid upgrading unit AAUU to purify the crude acrylic acid CAA is solvent-free distillation (i.e., no further solvent is added for the distillation).An acrylic acid upgrading unit AAUU utilizing solvent-free distillation can for example be combined with an acrylic acid separation unit AASU which comprises one or more absorption columns.In a preferred aspect of the present invention, crystallization or solvent-free distillation is used in combination with an acrylic acid separation unit AASU which preferably comprises one absorption column.A preferred aspect of the present invention in which a first waste stream W1, a second waste stream W2 and a third waste stream W3 are separated from the acrylic acid separation unit AASU shown in Figure 1 .Further waste streams may be generated when using an acrylic acid upgrading method selected from the group comprising, preferably consisting of solvent-added distillation, azeotropic distillation, extraction combined with distillation in the acrylic acid upgrading unit AAUU instead of crystallization or solvent-free distillation. The further waste streams which can be generated by said methods and accordingly, are separated from the acrylic acid upgrading unit AAUU are a fourth waste stream W4 which is a gaseous waste stream and is not suited as a feedstock for step (iv) or step (v) in the process according to the present invention, and / or a fifth waste stream W5 which is suited as feedstock in step (iv) of the process according to the present invention, and / or a sixth waste stream W6 which is anaqueous waste stream and which is suited as a feedstock for step (v). This aspect of the present invention is shown in Figure 2.Analytical methods suitable for measuring the calorific value of a feedstock such as a waste stream Wx(x = 1 , 2, 5, 6) comprise combustion of a sample of said feedstock in a bomb calorimeter. Such methods are for example suitable to assess the thermochemical behavior of said feedstock during the gasification reaction and, accordingly, the suitable type of gasifier and gasification process parameters such as temperature, amount, and type of oxidant.Analytical methods suitable for measuring the elemental composition such as the content of chemical elements H, C, 0, N, and S of a feedstock such as a waste stream Wx(x = 1 , 2, 5, 6) comprise CHNX analysis by combustion combined with thermal conductivity detection and / or infrared spectroscopy.Said parameter ranges for waste streams Wxare representative for the above-described acrylic acid production processes conducted in acrylic acid plants comprising a) an acrylic acid production unit AAPU, b) an acrylic acid separation unit AASU, and c) an acrylic acid upgrading unit AAUU.The first waste stream W1 has at least one, preferably all of the following properties:The first waste stream W1 preferably has a calorific value in the range of 5 to 40 MJ / kg, more preferably of 7 to 35 MJ / kg and most preferably of 10 to 30 MJ / kg.The first waste stream W1 preferably has a carbon content in the range of 30 to 80 wt.-%, more preferably 35 to 70 wt.-% and most preferably 40 to 70 wt.-%.The first waste stream W1 preferably has a hydrogen content in the range of 2 to 8 wt.-%, more preferably 3 to 7 wt.- % and most preferably 3.5 to 6 wt.-%.The first waste stream W1 preferably has an oxygen content in the range of 10 to 60 wt.-%, more preferably 15 to 55 wt.-% and most preferably 20 to 50 wt.-%.The first waste stream W1 preferably has a nitrogen content in the range of 0.01 to 5 wt.-%, more preferably 0.025 to2 wt.-% and most preferably 0.05 to 1 wt.-%.The first waste stream W1 preferably has a sulfur content in the range of 0.025 to 5 wt.-%, more preferably 0.05 to3 wt.-% and most preferably 0.1 to 2.5 wt.-%.Said first waste stream W1 is formed by an acrylic acid production process in said acrylic acid production plant.The optional fifth waste stream W5 has at least one, preferably all of the following properties:The optional fifth waste stream W5 preferably has a calorific value in the range of 5 to 40 M J / kg, more preferably of 7 to 35 M J / kg and most preferably of 10 to 30 M J / kg.The optional fifth waste stream W5 preferably has a carbon content in the range of 30 to 80 wt.-%, more preferably 35 to 70 wt.-% and most preferably 40 to 70 wt.-%.The optional fifth waste stream W5 preferably has a hydrogen content in the range of 2 to 8 wt.-%, more preferably 3 to 7 wt.-% and most preferably 3.5 to 6 wt.-%.The optional fifth waste stream W5 preferably has an oxygen content in the range of 10 to 60 wt.-%, more preferably 15 to 55 wt.-% and most preferably 20 to 50 wt.-%.The optional fifth waste stream W5 preferably has a nitrogen content in the range of 0.01 to 5 wt.-%, more preferably 0.025 to 2 wt.-% and most preferably 0.05 to 1 wt.-%.The optional fifth waste stream W5 preferably has a sulfur content in the range of 0.025 to 5 wt.-%, more preferably 0.05 to 3 wt.-% and most preferably 0.1 to 2.5 wt.-%.Said optional fifth waste stream W5 is formed by an acrylic acid production process in said acrylic acid production plant.Next, the first waste stream W1 provided in step (I) and the fifth waste stream W5 optionally provided in step (Ila), optionally pretreated in step (ill) is / are subjected in step (iv) to a gasification process wherein said gasification process comprises at least one gasifier G and whereby a gas stream GS1 is formed.The at least one gasifier G has at least one inlet through which a feedstock is fed into said at least one gasifier G and at least one outlet through which the gas stream GS1 is purged from said at least one gasifier G. Preferably, the at least one gasifier G has more than one inlet. Thereby, more than one feedstock can be fed into the at least one gasifier G through separate inlets. The term "inlet” comprises openings in the at least one gasifier G such as flaps and locks but also annual gaps as part of a burner such as in twin fluid atomizers, pressure nozzles and pressure atomizers.The optional pre-treatment step (ill) is described in the following: the first waste stream W1 and the optional fifth waste stream W5 may comprise particulate matter ("particles”). In this case, the first waste stream W1 and / or theoptional fifth waste stream W5 is / are preferably pre-treated in step (ill) by grinding and / or heating. Methods for grinding and / or heating a feedstock are known to the skilled person and can be adapted as necessary to a given first waste stream W1 and / or the optional fifth waste stream W5. The technical effect of grinding as pretreatment for the first waste stream W1 and / or the optional fifth waste stream W5 is that particles which may cause plugging in pipes and other parts of the downstream equipment are reduced in size and thereby the risk of undesired plugging is minimized. The technical effect of heating as a pre-treatment of the first waste stream W1 and / or the optional fifth waste stream W5 is that the viscosity of the first waste stream W1 and / or the optional fifth waste stream W5 is reduced and thereby, the pumpability and spray ability of the first waste stream W1 and / or of the optional fifth waste stream W5 are improved. Furthermore, undesired polymerization of the first waste stream W1 and / or the optional fifth waste stream W5 can be reduced or avoided.The gasification process of step (iv) comprises at least one gasifier G. A gas stream GS1 is formed in step (iv) from the first waste stream W1 provided in step (i) and the fifth waste stream W5 optionally provided in step (iia) which has / have been optionally pretreated in step (iii).Optionally, at least one further feedstock F is provided in step (iia) and subjected together with the first waste stream W1 and optionally also the fifth waste stream W5 to a gasification process in at least one gasifier G in step (iv).The gasification process of step (iv) is different from "hydrothermal gasification” described, e.g., inWO 2024 / 069082 A1. Such "hydrothermal gasification” is a process in which an aqueous solution is heated above 100 °C (e.g., 350 to 450 °C) in a pressurized vessel in which, after cooling, an aqueous phase and a gas phase are formed. The gas phase formed by the "hydrothermal gasification” disclosed in WO 2024 / 069082 A1 is composed of 40-70 % methane, 5-20 % hydrogen and 20-40 % carbon dioxide.In contrast, the gasification process of step (iv) is a thermochemical conversion process that transforms the waste streams Wxin at least one gasifier G into a combustible gas known as syngas (synthetic gas) through partial oxidation at high temperatures, typically between 800 and 1500 °C, in the presence of a controlled amount of oxygen, steam, or air. The gas formed by the gasification process in step (iv) (gas stream GS1) comprises a mayor portion of carbon monoxide and hydrogen as shown in the examples further below.The temperature in the at least one gasifier G is preferably between 800 and 1500 °C.Optionally, a further feedstock F is subjected to the gasification process in step (iv) wherein said gasification process comprises at least one gasifier G and whereby said further feedstock F is inserted into the at least one gasifier G "together” with the first waste stream W1 provided in step (i) and optionally also the fifth waste stream W5 provided in optional step (iia), optionally pretreated in step (iii). The meaning of "together” depends on the kind of optional further feedstock F and the type of gasifier G employed in step (iv) and is explained in detail below.Preferably, the optional further feedstock F is selected from the group comprising or consisting of biomass, refuse- derived fuel (RDF), pyrolysis oils made from plastic waste, pyrolysis oils made from end of life tires, pyrolysis oils made from biomass, heating oils, vacuum residues, preferably vacuum distillation residues, crude oil residues, heavy crude oils, extra heavy crude oils, tar sand bitumen, visbreaker bottom residues, deasphalter bottom residues, C5 asphalthene fraction, high viscous residues, fuel oils, pyrolysis gasolines, waste oils, used oils, municipal solid waste (MSW), automotive shredder residue (ASR), coal, natural gas, industrial waste streams and mixtures thereof.More preferably, the optional further feedstock F is selected from the group consisting of biomass, refuse-derived fuel (RDF), pyrolysis oils made from plastic waste, pyrolysis oils made from end-of-life tires, pyrolysis oils made from biomass, municipal solid waste (MSW), automotive shredder residue (ASR) and mixtures thereof.The term "biomass” includes but is not limited to wood, wood pellets, wood chips, straw, lignocellulosic biomass, energy crops, algae, bio-based oils, and bio-based fats (preferably hydrated).Biomass is preferably torrefied or converted by pyrolysis into a pyrolysis oil before used in step (iv) as a further feedstock F. Municipal solid waste (MSW) is optionally pre-treated by methods such as drying, shredding, sorting, inert removal and preferably used in step (iv) in form of refuse-derived fuel (RDF). Shredder residues such as automotive shredder residue (ASR) is preferably pre-treated by methods such as sorting, metal removal and the like before used in step (iv) as further feedstock F. Furthermore, torrefied biomass is preferably pre-heated to a temperature such as 200 °C before fed into a gasifier G as a further feedstock F.Liquid further feedstocks F such as bio-based oils and pyrolysis oils are preferably pre-heated and / or pressurized before fed into the gasifier G. In case the gasifier G is a plasma gasifier, the liquid further feedstock F is preferably pressurized to > 1 bar(abs.), more preferably to > 2 bar(abs.) and most preferably to about 4 bar(abs.) before fed into the gasifier G. In case the gasifier G is an entrained flow gasifier, the liquid further feedstock F is preferably pressurized to > 10 bar(abs.), more preferably > 20 bar(abs.) and most preferably > 40 bar(abs.) before fed into the gasifier G. Suitable means for pre-heating and / or pressurizing liquid feedstocks for feeding into a gasifier are known in the art, comprise for example flaps and locks but also annual gaps as part of a burner such as in twin fluid atomizers, pressure nozzles and pressure atomizers, and can be adapted to a given further feedstock F and / or gasifier G type by the skilled person.In case the gasifier G is an entrained flow gasifier, solid further feedstocks F such as municipal solid waste (MSW), refuse-derived fuel (RDF), wood chips, wood pellets and the like, said further feedstock is preferably pressurized e.g., in a lock before fed into the gasifier G.The at least one gasifier G is selected from entrained flow gasifiers and plasma gasifiers. Preferably, the at least one gasifier G is a plasma gasifier. More preferably, the at least one gasifier G is a plasma fixed-bed gasifier.An overview of gasifiers G, especially entrained flow gasifiers G and plasma gasifiers G is for example provided in James G. Speight, Handbook of Gasification Technology, Scrivener Publishing and Wiley, 2020, chapter 8.4.2, pages 259 to 262.The first waste stream W1 and the optional fifth waste stream W5, optionally pretreated in step (ill), can be fed into the gasifier G separately or be mixed before to form a waste stream mixture WM and then the mixture WM is fed into the gasifier G. The mixture WM can have a lower viscosity than the individual waste stream W1 and / or the fifth waste stream W5 and thereby feeding a waste stream mixture WM requires simpler equipment than feeding individual waste streams W1 and optionally also the fifth waste stream W5 into the gasifier G. Feeding a mixture WM into the gasifier G can also result in an improved atomization of the feedstock in the gasifier G compared to feeding waste stream W1 and the optional fifth waste stream W5 into the gasifier G. Thereby, the residence time and formation of coke inside the gasifier G can be reduced.The optional further feed F is preferably fed separately into the gasifier G, i.e., not mixed with the first waste stream W1 and the optional fifth waste stream W5 before being fed into the gasifier G. Thereby, variations in mass flow, calorific value and other properties of the first waste stream W1 can be better balanced and as a result a steady operation of the gasifier G maintained. The optional further feedstock F is preferably fed into the gasifier G by means preferably selected from lock, screw conveyor, hopper, and flap. Most preferably, the optional further feedstock F is selected from the group consisting of torrefied biomass, pyrolysis oil and bio-based oils wherein the pyrolysis oil can be manufactured by pyrolysis from mixed plastic waste (MPW), end of life tires (ELT) and biomass. Such optional feedstocks F have more homogenized properties such as calorific value compared to, for example, municipal solid waste (MSW).In one aspect of the present invention, a CO2 waste stream from one or more chemical processes such as CO2 capture by absorption is also co-fed into the at least one gasifier G.Solid fuel particles are injected in an entrained flow gasifier G in a high-velocity stream of gas and are heated to high temperatures (typically between 800 and 1500 °C) in the presence of oxygen and / or steam. The solid particles are provided by the further feedstock F and the first waste stream W1 is preferably transported in downdraft mode.In case the at least one gasifier G in step (iv) is an entrained flow gasifier, the first waste stream W1 and the optional fifth waste stream W5 is / are preferably compressed up to 40 bar(abs.) or higher before fed into the at least one gasifier G.The temperature inside the entrained flow gasifier G preferably ranges from 800 to 1500 °C, more preferably from 1000 to 1450 °C and most preferably from 1100 to 1400 °C. The pressure inside the entrained flow gasifier preferably ranges from 1 to 55 bar(abs.), more preferably from 5 to 50 bar(abs.) and most preferably from 20 to 45 bar(abs.).Addition of a further feedstock F is preferred because thereby the desired constant operation conditions in the entrained flow gasifier can be maintained and synthesis gas having the desired molar ratio CO : H2 is formed.Preferably, the first waste stream W1 and the optional further feedstock F are fed into the entrained flow gasifier via at least one burner whereby said at least one burner comprises one annular gap for the waste stream W1 and a separate annular gap through which the optional further feedstock F is fed. Steam, preferably mixed with oxygen is cofed into the entrained flow gasifier through a separate annular gap in said at least one burner.Plasma gasification is a high-temperature waste treatment process that uses plasma, a gas composed of highly charged particles, to break down organic matter into a gas. In this process, the first waste stream W1 and the optional fifth waste stream W5 is / are fed into a plasma reactor, preferably, the first waste stream W1 and the optional fifth waste stream W5 is / are fed into the plasma reactor, where it is exposed to an electric arc or microwave radiation or at least one plasma torch, which ionizes the waste stream(s) and creates a plasma. Preferably, the plasma is generated by means of at least one plasma torch, more preferably, the plasma is generated by means of at least two plasma torches. Most preferably, the plasma gasifier comprises one to three plasma torches in the part of the gasifier where the first waste stream W1 and the fifth waste stream W5 is / are fed onto the plasma gasifier and one or two plasma torches in the part of the plasma gasifier where the gas stream GS1 leaves the plasma gasifier (most preferably in arrangement which forces the gas stream GS1 to pass said one or two plasma torches). The high temperatures inside the plasma gasifier, which can reach up to about 10000 K, cause the first waste stream W1 and the optional fifth waste stream W5 to vaporize and break down into the constituent components, including hydrogen, carbon monoxide, and methane.In case the at least one gasifier G in step (iv) is a plasma gasifier, the first waste stream W1 and the optional fifth waste stream W5 is / are preferably compressed up to 4 bar(abs.) before fed into the at least one gasifier G.The temperature of the gas leaving the plasma gasifier is preferably in the range of 1100 to 1400 °C, most preferably around 1300 °C. The pressure of the gas leaving the plasma gasifier is preferably at least 0.7 bar(abs.) and more preferably at least 1 bar(abs.). The residence time of the reactants inside the plasma gasifier is at least 2 to 3 s. The plasma is preferably generated from a gas selected from the group comprising CO2, steam, O2, air and mixtures thereof. More preferably, the plasma is generated from a CO2, steam or a mixture of CO2 and steam.The first waste stream W1 and the optional fifth waste stream W5 or a waste stream mixture WM is preferably fed into the plasma gasifier through an opening separate of the opening through which the optional further feedstock F is fed. Steam is preferably fed to the plasma gasifier through still another opening.Optionally the process according to the present invention comprises a further step (ivb) wherein said further step (ivb) is selected from the group comprising or consisting of cleaning the gas stream GS1 and thereby forming gas stream GS11, separating H2 and CO comprised in gas stream GS1 or GS11 from each other, compressing at leastone gas stream selected from gas stream GS11, H2 separated from gas stream GS1, H2 separated from gas stream GS11, CO separated from gas stream GS1, CO separated from gas stream GS11 and combinations thereof. Preferably, said step (ivb) comprises, in this order, cleaning gas stream GS1 and thereby forming gas stream GS11, separating H2 and CO comprised in gas stream GS11 and compressing at least one of H2 and CO separated from gas stream GS11.The optional further process steps (ivb) and (vi) are schematically shown in Figure 3.Typical impurities in the gas stream GS1 comprise chlorides, sulfur-containing organic compounds such as sulfur dioxide, trace heavy metals (e.g., as respective salts), tars / condensable hydrocarbons and particulate residues. Various chemical and / or physical methods for removal of such impurities from said gas stream GS1 such as filtration, scrubbing, condensation and ab- / adsorption are known and can be chosen and adapted according to the type and respective concentration of the impurities in said gas stream GS1 and the tolerance to such impurities in a further process FP1 for which the gas stream GS11 is used. Some selected methods for removal of impurities from said gas stream GS1 will be discussed in more detail. One or more of said methods can also be implemented into the optional gas treatment unit GTU. However, this selection of methods is not limiting the scope of the present invention.Other gaseous substances such as HOI and H2S are formed and / or separated from the gas stream GS1 in the optional gas treatment unit GTU. Impurities are removed from the gas stream GS1 and a gas stream GS11 having a first molar ratio H2 : CO is obtained.Particulate impurities can be removed from the gas stream GS1 by a cyclone and / or filters, chlorides by wet scrubbing, trace heavy metals, catalytic hydrolysis for converting sulfur-containing organic compounds to H2S and acid gas removal for extracting sulfur-containing gases such as H2S. Bulky and (fine) particles such as dust in the gas stream GS1 may also be removed with a quench in a soot water washing unit.Particulate impurities can be optionally removed from the gas stream GS1 directly by a cyclone and / or filters after the gas stream GS1 leaves the gasifier. Hence, the removal of particles from the gas stream GS1 can be part of a gasifier and / or part of the optional gas treatment unit GTU which is fluidically connected to the at least one gasifiers G.Fine particles can be optionally removed from the raw synthesis gas directly with filters after the gas stream GS1 leaves the at least one gasifier G. Hence, the removal of fine particles from the gas stream GS1 can be part of the at least one gasifier G and / or part of the optional gas treatment unit GTU which is fluidically connected to the at least one gasifier G.The optional gas treatment unit GTU preferably comprises a washing unit for removing CO2 from the gas stream GS1. Most preferably, said washing unit is an "amine wash” or a "methanol” wash which uses one or more aminecompounds such as alkanolamines or methanol to absorb CO2. Such washing units are known in the art and can be adapted for removal of CO2 from a gaseous stream GS1 by the skilled person.CO and / or H2 are optionally separated from the gas stream GS1. CO can be separated from the gas stream GS1 in a synthesis gas separation unit which is, optionally, downstream of and fluidically connected to the at least one gasifier G. CO can be separated from gas stream GS1 by cryogenic separation methods, commonly referred to as a "cold box” which makes use of the different boiling points of CO and H2. H2 can be separated using ^-selective membranes thorough which H2 permeates and is thereby separated from the GS1 stream.The gas stream GS1 has a first molar ratio H2 : CO. Optionally, the gas stream GS1 is then preferably subjected to a water-gas shift reaction in a water-gas shift unit. Thereby, the H2 content in the gas stream GS1 is increased by reacting a portion of the CO of the gas stream GS1 with water to form additional H2 and CO2 and thereby gas stream GS11 having a second molar ratio H2 : CO is formed and leaves the water-gas shift unit. The H2 content in said gas stream GS11 leaving the water-gas shift unit and having a second molar ratio H2 : CO is higher than in said gas stream GS1 leaving the at least one gasifier having a first molar ratio H2 : CO. The hydrogen content in gas stream GS1 can for example also be increased by adding hydrogen provided by another source such as hydrogen formed by electrolysis of water, preferably using electrical energy from a renewable source such as solar and / or wind energy.The water-gas shift reaction will operate with a variety of catalysts (such as copper-zinc-aluminum catalysts and chromium or copper promoted iron-based catalysts) in the temperature range between about 200 °C and about 480 °C.The gas stream GS11 is optionally compressed, preferably, in case the first waste stream W1 and the optional fifth waste stream W5 was / were converted to gas stream GS1 in a plasma gasifier. In this case, gas stream GS11 is preferably compressed to a pressure in the range 1.5 to 4 bar(abs.).Optionally, the gas stream GS1 and / or the gas stream GS11 and / or H2 separated from gas stream GS1 and / or GS11 and / or CO separated from gas stream GS1 and / or GS11 are / is then subjected to a further process FP1 selected from the group comprising methanization, alcohol synthesis (preferably methanol synthesis) and Fischer-Tropsch synthesis whereby at least one first product stream PS1 is formed. The gas stream GS11 can also be used as a fuel gas Said optional further processes FP1 are briefly described below:Optionally, the gas stream GS1 and / or the gas stream GS11 can be converted into methane by a methanation reaction. The methanation reaction is described by chemical reaction schemes (1) and (2):CO + 3H2-> CH4+ H2O (1)CO2+ 4H2-> CH4+ 2H2O (2)The methanation reaction and suitable methanation units are for example described in S. Rdnsch, J. Schneider, S. Matthischke, M. Schluter, M. Gdtz, J. Lefebvre, P. Prabhakaran, S. Bajohr: Review on methanation - From fundamentals to current projects; Fuel 166 (2016) 276-296 and can be selected and adapted by the skilled person.The methanation reaction is for example a catalytic reaction using nickel on alumina catalysts, preferably a honeycomb shape catalyst, at 1 to 70 bar and 200 to 700 °C, preferably 5 to 60 bar, more preferably 10 to 45 bar and preferably 200 to 550 °C, more preferably 10 to 45 bar.Alcohols such as methanol are another chemical product which can be manufactured from the gas stream GS11 by an optional further process FP1. The most preferred, methanol, is produced from synthesis gas by a catalytic gas phase reaction at about 5 to 10 MPa and a temperature of about 200 °C to about 300 °C using a catalyst in a low- pressure methanol process in e.g., adiabatic reactors or quasi-isothermal reactors. The catalyst is for example a mixture of copper and zinc oxides, supported on alumina. The methanol synthesis and various options thereof suitable to be combined with the production system according to the present invention are disclosed in Ullmann's Encyclopedia of Industrial Chemistry (2012), Chapter "Methanol”, p. 3 to 12.The gas stream GS11 can also optionally be converted into hydrocarbons such as light synthetic crude oil in an optional Fischer-Tropsch (FT) reaction unit by the FT process. Such hydrocarbons are also denoted "Fischer-Tropsch hydrocarbons”. The light synthetic oil can be further converted by hydrocracking and / or isomerization to naphtha, light olefins, or diesel fuel. For production of gasoline and light olefins, the FT process is operated in a temperature range of about 330 °C to about 350 °C and a pressure of about 2.5 MPa (high-temperature FT-process), for production of waxes and / or diesel fuel, in a temperature range of about 220 °C to about 250 °C and a pressure of about 2.5 MPa to about 4.4 MPa (low-temperature FT-process). Suitable reactors for low-temperature FT-processes comprise tubular fixed-bed reactors and slurry bed reactors. Suitable reactors for high-temperature FT-processes comprise circulating fluidized-bed reactors and SAS (Sasol advanced synthol) reactors. Iron- and / or cobalt-based catalysts are used for the FT-process. The Fischer-Tropsch synthesis and various options thereof suitable to be combined with the production system according to the present invention are disclosed in Ullmann's Encyclopedia of Industrial Chemistry (2012), Chapter "Coal Liquefaction”, p. 20 to 33.In one aspect of the present invention, the gas stream GS11 is converted into methanol for example by a method described above. Next, the methanol is converted into propene by a methanol-to-propene (MTP) synthesis which are for example disclosed in M. Khanmohammadi, Sh. Amani, A. Bagheri Garmarudi, A. Niaei "Methanol-to-propylene process: Perspective of the most important catalysts and their behavior” Chinese Journal of Catalysis 37 (2016) 325-339 (DOI: 10.1016 / S1872-2067(15)61031 -2). Next, the propene is used as the C3 feedstock in an acrylic acid synthesis unit and converted into crude acrylic acid as described above. Accordingly, in this aspect of the present invention, the first waste stream W1 and the optional fifth waste stream W5 is / are utilized as a feedstock for the manufacture of acrylic acid.Preferably, in case the optional further feedstock F is selected from the group comprising municipal solid waste (MSW), shredder residues such as automotive shredder residue (ASR), coal, (i.e., "coarse” further feedstocks CF) said optional co-feedstock is preferably subjected to a pre-treatment whereby said optional further feedstock is converted into a secondary further feedstock SF in a pre-gasification process, which secondary further feedstock SF is then co-fed into the gasification process in step (iv) together with the first acrylic acid waste stream W1 (and / or the first acrylic acid waste stream W1 pretreated in step (iii) and / or also the optional fifth waste stream W5). The pre-gas- ification process preferably comprises at least one fluidized bed gasifier in which the optional further feedstock F2 is converted, preferably in the presence of oxygen and / or steam and more preferably in addition to oxygen and / or steam in the presence of CO2, into a secondary further feedstock SF, said SF comprising crude synthesis gas, tar oil, soot, coke, methane and higher hydrocarbons. Said secondary further feedstock SF is then co-fed into the at least one gasifier of the gasification process in step (iv).In a fluidized bed gasifier, the particles of the at least one further feedstock F2 in an oxygen-rich gas so the resulting bed within the gasifier acts as a fluid. The at least one further feedstock F2 preferably enters the fluidized-bed gasifier at the side of the reactor, while steam and an oxidant (e.g., oxygen, air, preferably: oxygen) enter near the bottom with enough velocity to fully suspend or fluidize the reactor bed. The process temperature in said fluidized-bed gasifier is preferably > 700 °C. The weight ratio "steam : further feedstock F2” is preferably > 0.25, the weight ratio O2 : further feedstock F2 preferably ranges from 0.1 : 1 to 1 : 1 . The further feedstock F2 is preferably fed into the fluidized-bed gasifier at a pressure of 0 to 20 bar(abs.).A second waste stream W2 is provided in step (ii). The second waste stream W2 is an aqueous waste stream which comprises water. The second waste stream W2 is separated from the acrylic acid separation unit AASU as described above.Optionally, a sixth waste stream W6 which is also an aqueous waste stream is provided in step (iia). The optional sixth waste stream W6 is separated from the acrylic acid upgrading unit AAUU as described above.The parameter ranges disclosed for waste streams Wxherein represent the respective composition of said waste streams prior to any further treatment such as reducing the water content of said aqueous waste stream W2 and / or W6.The second waste stream W2 has at least one, preferably all the following properties:The second waste stream W2 preferably has a calorific value in the range of 1 to 40 MJ / kg, more preferably of 2 to 30 MJ / kg and most preferably of 3 to 15 MJ / kg.The second waste stream W2 preferably comprises less than 90 wt.-% water, more preferably less than 70 wt.-% water and most preferably less than 50 wt.-% water.The second waste stream W2 preferably has a carbon content in the range of 1 to 30 wt.-%, more preferably 1 .5 to 25 wt.-% and most preferably 2 to 20 wt.-%.The second waste stream W2 preferably has a hydrogen content in the range of 2 to 20 wt.-%, more preferably 3 to 18 wt.-% and most preferably 5 to 15 wt.-%.The second waste stream W2 preferably has an oxygen content in the range of 50 to 97 wt.-%, more preferably 57 to95.5 wt.-% and most preferably 70 to 93 wt.-%.The second waste stream W2 is formed by an acrylic acid production process described in detail further above in said acrylic acid production plant described in detail further above.The optional sixth waste stream W6 has at least one, preferably all the following properties:The optional sixth waste stream W6 preferably has a calorific value in the range of 1 to 40 MJ / kg, more preferably of2 to 30 MJ / kg and most preferably of 3 to 15 MJ / kg.The optional sixth waste stream W6 preferably comprises less than 90 wt.-% water, more preferably less than 70 wt.- % water and most preferably less than 50 wt.-% water.The optional sixth waste stream W6 preferably has a carbon content in the range of 1 to 30 wt.-%, more preferably1 .5 to 25 wt.-% and most preferably 2 to 20 wt.-%.The optional sixth waste stream W6 preferably has a hydrogen content in the range of 2 to 20 wt.-%, more preferably3 to 18 wt.-% and most preferably 5 to 15 wt.-%.The optional sixth waste stream W6 preferably has an oxygen content in the range of 50 to 97 wt.-%, more preferably 57 to 95.5 wt.-% and most preferably 70 to 93 wt.-%.The optional sixth waste stream W6 is formed by an acrylic acid production process described in detail further above in said acrylic acid production plant described in detail further above.The second waste stream W2 and / or the optional sixth waste stream W6 may comprise substances which are not desired in an anaerobic fermentation process. Formaldehyde for example is harmful to the bacteria employed in such anaerobic fermentation and, accordingly are preferably removed from said waste streams if present therein. Acroleinwhich also may be comprised in the second waste stream W2 and / or the optional sixth waste stream W6 is known to inhibit anaerobic fermentation processes and is, preferably removed from said waste streams if comprised therein.Methods suitable for removal of said harmful substances from the second waste stream W2 and / or the optional sixth waste stream W6 comprise evaporation of harmful substances from said waste stream(s), iron-carbon micro electrolysis, oxidation with H2O2, catalytic wet air oxidation, treatment of said waste stream(s) with O3 and combinations thereof. Preferred is a combination of a) evaporation and b) one of said oxidation methods. Such methods are known in the art and can be adapted by the skilled person accordingly.The second waste stream W2 and / or the optional sixth waste stream W6 is / are also preferably pre-treated in step (ill) by reducing at least a portion of the water comprised in said waste stream(s). The amount of water comprised in the optional second waste stream W2 and / or waste stream W6, means for reducing the amount of water therein by e.g., evaporation and preferred water contents in the second waste stream W2 and / or the optional sixth waste stream W6 after reduction of the water content and the desired effect of such a water content reduction are described above.In some cases, the second waste stream W2 and / or the optional sixth waste stream W6 may require pretreatment to remove impurities, adjust pH, or enhance the accessibility of the organic compounds for the anaerobic fermentation in step (v) . The skilled person knows how to identify such cases and then how to pretreat the second waste stream W2 and / or the optional sixth waste stream W6 for the successive anaerobic fermentation process in step (v).The second waste stream W2 and the optional sixth waste stream W6 is / are subjected in step (v) to an anaerobic fermentation process AFP in an anaerobic fermentation unit AFU.The second waste stream W2 and the optional sixth waste stream W6 is / are treated in the anaerobic fermentation unit AFU in the absence of oxygen with bacteria suited for anaerobic fermentation. Thereby, a product gas stream GS2 comprising CH4 and CO2, and a sludge S are formed.Anaerobic fermentation units AFU and anaerobic fermentation processes AFP suitable for step (v) are not restricted to particular units and / or particular processes and can, hence, be selected and adapted by the skilled person.Anaerobic first fermentation processes FP1 and suitable microorganisms are for example disclosed in A. Aivasidis, Ullmann's Encyclopedia of Industrial Chemistry, "Wastewater, 3. Anaerobic Biological Treatment”, pages 639 to 663 (DOI: 10.1002 / 14356007.o28_o09), 2012.The sludge S formed from the second waste stream W2 and the optional sixth waste stream W6 is / are optionally then treated by an aerobic fermentation process in an aerobic fermentation unit whereby a fermentation product comprising CO2 and water is formed. Aerobic second fermentation processes FP2 and suitable types of microorganismsare disclosed in L. Telgmann et al., Ullmann's Encyclopedia of Industrial Chemistry, "Wastewater, 2. Aerobic Biological Treatment”, especially pages 42 to 52 (DOI: 10.1002 / 14356007.o28_o08.pub2), 2019.The gas stream GS2 can be fed in optional step (vi) into a fermentation product upgrading unit FUU in which the gas stream GS2 is converted into chemical products which leave said fermentation product upgrading unit FUU as gas stream GS22.The fermentation product upgrading unit FUU is downstream of and fluidically connected to the fermentation unit FU. The optional further process steps (ivb) and (vi) are schematically shown in Figure 3.Preferably, the fermentation product upgrading unit FUU is selected from the group comprising steam reforming unit SRU, dry reforming unit DRU and hydrocarbon pyrolysis unit HPU in which the gaseous stream GS2 is used as a feedstock or co-feedstock for steam reforming (whereby stream GS22a is formed), dry reforming (whereby stream GS22b is formed), or methane pyrolysis (whereby stream GS22c is formed), respectively. The further processing of gas stream GS2 in different fermentation product upgrading units FUU is schematically shown in Figure 4. These processes and the corresponding units are described below.In one aspect of the present invention, at least a portion of the gas stream GS2 is fed into a steam reforming unit SRU and subjected to a steam reforming process whereby a gas stream GS22a is formed (Figure 4a)). Said gas stream GS22a is a synthesis gas stream comprising H2 and CO.The steam reforming process can be simplified to a reaction schema according to formula 3:CH4+ H2O -> CO + 3H2(3).Gaseous stream GS2 can be used as sole feedstock together with steam in a steam reforming unit SRU for a steam reforming process in which gaseous stream GS2 and steam are converted into synthesis gas. Preferably, gaseous steam GS2 is mixed with another gaseous hydrocarbon, more preferably with natural gas and / or methane, most preferably with bio-methane, and is fed together with steam into said steam reforming unit SRU. The steam reforming unit SRU is downstream of and fluidically connected to the fermentation unit FU.In the steam methane reforming process, steam and methane react in the presence of a heterogeneous catalyst, preferably a nickel-based catalyst on a substrate such as an alumina substrate, at elevated temperatures and pressure. The metal loading in the catalyst, preferably the nickel loading is typically 5 to 30 wt.-%, the support is preferably a a-AI2O3 based ceramic support. The reaction is typically conducted at 600 to 800 °C but can also be conducted at higher temperatures such as 900 °C or higher.Steam reforming processes and conditions applicable in the process according to the present invention are for example disclosed in Ullmann's Encyclopedia of Industrial Chemistry, chapter "Gas Production, 2. Processes”, R. Reimert et al., pages 426-433, 2012 (DOI: 10.1002 / 14356007.O12_o01 ).In one aspect of the present invention, at least a portion of the gas stream GS2 is fed into a dry reforming unit DRU and subjected to a dry reforming process whereby a gas stream GS22b is formed (Figure 4 b)). Said gas stream GS22b is a synthesis gas stream comprising H2 and CO. The dry reforming unit DRU is downstream of and fluidically connected to the fermentation unit FU.The dry reforming process can be simplified to a reaction schema according to formula 4:CH4+ CO2-> 2CO + 2H2(4).Dry reforming utilizes a heterogeneous catalyst such as at least one metal selected from Ni, Ru, Rh, Pd, Ir, Pt or Co, on an oxide support, such as SiO2, AI2O3, MgO, TiO2, CaO, CeO2, ZrO2, or l_a2O3.Fixed bed and fluidized bed reactors can be used for the dry reforming of gas stream GS2 (optionally together with a co-feed such as another gaseous hydrocarbon, more preferably with natural gas and / or methane, most preferably with bio-methane). Additional CO2is co-fed into the dry reforming unit DRU if required to obtain a desired molar ratio H2: CO (see formula 2). Said additional CO2is preferably selected from CO2provided by a CCS and / or CCU process or any other chemical process in which CO2is formed such as a water-gas shift reaction.Dry-reforming processes suitable for gas stream GS2 are for example described in Catalytic Technology for Carbon Dioxide Reforming of Methane to Synthesis Gas, Mun-Sing Fan, Ahmad Zuhairi Abdullah, and Subhash Bhatia, ChemCatChem 2009, 1, 192 - 208 (DOI: 10.1002 / cctc.200900025) and Ullmann's Encyclopedia of Industrial Chemistry, chapter "Gas Production, 2. Processes”, R. Reimert et al., pages 433-434 and 436, 2012 (DOI: 10.1002 / 14356007. o12_o01).In one aspect of the present invention, at least a portion of the gas stream GS2 is fed into a hydrocarbon pyrolysis unit HPU and subjected to a hydrocarbon pyrolysis whereby a gas stream GS22c is formed (Figure 4c)). Said gas stream GS22c comprises H2. The hydrocarbon pyrolysis unit HPU is downstream of and fluidically connected to the fermentation unit FU.The gas stream GS2 comprising CH4 and CO2or a portion thereof is fed into the hydrocarbon pyrolysis unit HPU preferably with a pressure in the range of 1 to 15 bar. Optionally, the gas stream GS2 is compressed after leaving the fermentation unit FU, for example in screw compressor.In hydrocarbon pyrolysis, mainly named methane pyrolysis (reaction equation (1)), hydrogen is obtained from methane comprised in stream GS2. CO2comprised in stream GS2 is converted together with methane comprised therein to a mixture of H2and CO.As a co-feedstock, natural gas, synthetic methane, bio-methane, industrial off gas, e.g., cracker off gas, biogas or sewage gas can be fed into the hydrocarbon pyrolysis unit HPU together with gas stream GS2.The generic term hydrocarbon pyrolysis covers a wide range of different process technologies. Applicable to the process according to the present invention are: plasma pyrolysis (for example WO2015116797, WO2015116800), metal melting / metal salt melting processes (for example W02020161192, WO2021183959), moving bed processes (for example US 2982622, WO 2019 / 145279 and WO 2020 / 200522), fluidized bed catalytic processes, partial combustion processes (for example W02020118417 and US20220185664).They differ in the form of the energy used (thermal, electrical, etc.), the process conditions (temperature, pressure, etc.), the catalysts and / or auxiliary materials used, the process flow and the technical readiness level (TRL). Furthermore, the solid carbon type generated in the hydrocarbon decomposition depends on the reaction conditions, reactor and heating technology.The pyrolysis process is preferably heated electrically, even more preferably by resistive heating (Joule heating) of the substrate material as described for example in US 2982622, WO 2019 / 145279 and WO 2020 / 200522.The hydrocarbon pyrolysis using gas stream GS2 and an optional co-feed is most preferably conducted in a moving or fixed bed reactor, wherein the bed contains as substrates preferably carbon materials, metals, ceramics, and a mixture thereof, preferably at temperatures ranging from 500 to 2000 °C, preferably ranging from 1000 to 1600 °C, even more preferably ranging from 1200 to 1500 °C, and at pressures ranging from 1 to 100 bar, preferably from 5 to 50 bar. The decomposition can either be realized as fixed bed, preferably in a cyclical operation mode, preferably including a production and a regeneration mode as described for example in WO 2018 / 083002, or in a moving bed as described for example in US 2982622, WO 2019 / 145279 and WO 2020 / 200522.Most preferably, the substrate is guided in form of a moving bed through the reaction chamber, with the gas stream GS2 and optionally the co-feed being passed advantageously in countercurrent to the substrate. For this purpose, the reaction chamber is preferably rationally designed as a vertical reactor, which means that the movement of the moving bed is gravity driven. Flow through the moving bed is taking place, advantageously, homogeneously, and uniformly (see for example WO 2013 / 004398, WO 2019 / 145279 and WO 2020 / 200522). The gas stream GS2, optionally together with the co-feed is / are preferably introduced via the bottom of the reactor, preferably having a temperature of 10 to 200°C. The substrate is preferably introduced via the top of the reactor, preferably having a temperature of 10 to 200°C. Hydrogen is preferably taken off via the top of the reactor, preferably having a temperature of 10 to 200°C. The granular pyrolytic carbon is preferably taken off via the bottom of the reactor, preferably having a temperature of 10 to 200°C.Preferably the hydrogen formed in the hydrocarbon pyrolysis unit HPU is used to produce (i) MeOH, (ii) CH4, (iii) NH3, (iv) synthesis gas, (v) for hydrogenation reaction, (vi) downstream products like aromatics, ketones (e.g.,cyclododecanone), aldehydes (e.g., hexanal), cyclic hydrocarbons (e.g., cyclohexane), amins (e.g., butylamine, propylamine), alcohols (e.g.,e butanol, heptanol, butanediol, menthol).Optionally, a third waste stream W3 and / or an optional fourth waste stream W4 is / are also treated in the process according to the present invention. The third waste stream W3 is a gaseous waste stream which originates from the acrylic acid separation unit AASU as the volatile head product of e.g., a condenser or an absorption column.The third waste stream W3 has at least one, preferably all of the following properties:A carbon content of 0.5 to 8 wt.-%, a hydrogen content of 0.1 to 1 wt.-%, an oxygen content of 5 to 95 wt.-%, a nitrogen content of 0 to 95 wt.-% and a sulfur content of 0 to 4 wt.-%, wherein the sum of carbon content, hydrogen content, oxygen content, nitrogen content and sulfur content is at least 95 wt.-%. Said third waste stream W3 is formed by an acrylic acid production process in said acrylic acid production plant.The optional fourth gas stream W4 is a gaseous waste stream which originates from the acrylic acid upgrading unit AAUU.The fourth waste stream W4 has at least one, preferably all of the following properties:A carbon content of 0.5 to 8 wt.-%, a hydrogen content of 0.1 to 1 wt.-%, an oxygen content of 5 to 95 wt.-%, a nitrogen content of 0 to 95 wt.-% and a sulfur content of 0 to 4 wt.-%, wherein the sum of carbon content, hydrogen content, oxygen content, nitrogen content and sulfur content is at least 95 wt.-%. Said fourth waste stream W4 is formed by an acrylic acid production process in said acrylic acid production plant.Due to the low concentration of carbonaceous components in the third waste stream W3 and / or the fourth waste stream W4, processing by a method such as gasification or fermentation is not suitable. Accordingly, the third waste stream W3 and / or the optional fourth waste stream W4 is / are optionally incinerated in an optional incineration unit IU whereby the third waste stream W3 and / or the optional fourth waste stream W4 is / are converted into steam and CO2 which are emitted from the incineration unit IU as a gaseous stream GS3.Preferably, the gaseous stream GS3 is then treated in a carbon capture unit CCU whereby CO2 is separated from gaseous stream GS3 as gaseous stream GS33a and the gaseous stream GS33b leaving the carbon capture unit CCU consists mostly of steam. The CO2 separated in the optional carbon capture unit CCU can be for example se- quested by methods known in the art of utilized as a co-feedstock, e.g., in the gasifier G and / or the optional fixed bed gasifier FBG and / or in the optional dry-reforming unit DRU and / or other processes.Separation of CO2 from a gaseous stream such as GS33 is a known process and is for example disclosed in S. Topham, A. Bazzanella, S. Schiebahn, S. Luhr, L. Zhao, A. Otto, D. Stolten, Ullmann's Encyclopedia of IndustrialChemistry, Chapter "Carbon Dioxide”, 2014, pages 24 to 37 (10.1002 / 14356007. a05_165.pub.2). The skilled person knows how to adapt such known processes to the composition, pressure and other parameters of the gaseous stream GS33 to separate the desired portion of CO2 therefrom.The above-described optional incineration and separation of CO2 from gaseous stream GS3 further improves the process according to the present invention for example in terms of product carbon food print (PCF).In another aspect of the present invention, the gas stream GS1 obtainable by or formed in step (iv) and / or gas stream GS11 obtainable by or formed in optional step (ivb) and / or gas stream GS2 obtainable by or formed in optional step (vi) is converted to obtain a product.The publication Prior Art Disclosure; Issue 684; paragraphs

[1000] to

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

[1000] to

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

[1000] to

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

[1000] to

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

[2001] to

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

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

[2009] and

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

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

[3035] to

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

[3008] to

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

[3001] to

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

[3006] to

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

[3045] to

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

[3056] to

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

[6007] entitled "Binders for fiber bonding”, section

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

[8000] to

[8005] of Reference RF1.The present invention also concerns an acrylic acid production plant comprising an integrated waste stream treatment facility wherein said acrylic acid production plant comprises a) an acrylic acid production unit AAPU, b) an acrylic acid separation unit AASU which is downstream of and fluidically connected to the acrylic acid production unit AAPU, c) an acrylic acid upgrading unit AAUU which is downstream of and fluidically connected to the acrylic acid separation unit AASU, d) at least one gasifier G which is downstream of and preferably directly or indirectly fluidically connected to the acrylic acid separation unit AASU and e) at least one anaerobic fermentation unit AFU downstream of and directly or indirectly fluidically connected to said acrylic acid separation unit AASU.This acrylic acid plant is shown schematically in Figure 1. An acrylic acid production plant releasing at least one further waste stream selected from W4, W5 and W6 is shown in Figure 2.The components of the respective units AAPU, AASU, AAUU, G and AFU as disclosed above also apply to the acrylic acid production plant according to the present invention.The respective outlet for the first waste stream W1 of the acrylic acid separation unit AASU and the optional fifth waste stream W5 of the acrylic acid upgrading unit AAUU can be directly or indirectly fluidically connected to the respective inlet of the at least one gasifier G."Directly” is defined as fluidically connected by a suitable means such as a pipe. Accordingly, respective outlet for the first waste stream W1 of the acrylic acid separation unit AASU and the optional fifth waste stream W5 of the acrylic acid upgrading unit AAUU is / are fluidically connected by a suitable means such as a pipe with the respective inlet of the at least one gasifier G."Indirectly” is defined as interrupted by e.g., an additional unit for pre-treating the respective feedstock, storage tank(s), transporting the first waste stream W1 and the optional fifth waste stream W5 or the waste stream mixture WM from an acrylic acid production plant to the at least one gasifier G for example by truck or train. Accordingly, "indirectly” means for example that the respective outlet for the first waste stream W1 of the acrylic acid separation unit AASU and the optional fifth waste stream W5 of the acrylic acid upgrading unit AAUU is / are fluidically connected to the inlet of a feedstock pre-treatment unit for first waste stream W1 and the optional fifth waste stream W5, which is downstream of the acrylic acid separation unit AASU and the acrylic acid upgrading unit AAUU, and the outlet of the feedstock pre-treatment unit is fluidically connected to the respective inlet of the at least one gasifier G which is downstream of the pre-treatment unit.The same definitions for "directly” and "indirectly” apply for the second waste stream W2 and the optional sixth waste stream W6 with the sole difference that the "at least one gasifier G” is replaced by "the at least one anaerobic fermentation unit AFU.Various waste streams formed during production of acrylic acid from propene can be treated in the process and the acrylic acid production plant according to the present invention in a more efficient and sustainable way than utilizing conventional processes such as incineration.The present invention is further illustrated by the following set of embodiments and combinations of embodiments resulting from the dependencies and back-references as indicated. In particular, it is noted that in each instance where a range of embodiments is mentioned, for example in the context of a term such as "The method of any of embodiments 1 to 3", every embodiment in this range is meant to be explicitly disclosed for the skilled person, i.e. the wording of this term is to be understood by the skilled person as being synonymous to "The method of any of embodiments 1 , 2 and 3". Further, it is explicitly noted that the following set of embodiments represents a suitably structured part of the general description directed to preferred aspects of the present invention, and thus, suitably supports the claims of the present invention.1. Process for utilizing at least one waste stream from an acrylic acid production plant, wherein the acrylic acid production plant comprises a) an acrylic acid production unit, b) an acrylic acid separation unit, and c) an acrylic acid upgrading unit, the process comprising the steps(I) providing a first waste stream W1 , wherein the first waste stream W1 is separated from the acrylic acid separation unit,(ii) providing a second waste stream W2, wherein the second waste stream W2 is separated from the acrylic acid separation unit,(iia) optionally providing a fifth waste stream W5 and / or a sixth waste stream W6 and / or a further feedstock F, wherein said optional fifth waste stream W5 and said optional sixth waste stream W6 are separated from the acrylic acid upgrading unit,(ill) optionally pretreating the first waste stream W1 and / or the second acrylic acid waste stream W2, and / or the optional fifth waste stream W5 and / or the optional sixth waste stream W6 and / or the optional further feedstock F,(iv) subjecting the first waste stream W1 provided in step (I) or optionally after pretreatment in step (ill) and the optional fifth waste stream W5 to a gasification process wherein said gasification process at a temperature between 800 and 1500 °C, comprises at least one gasifier G and thereby forming a gasstream GS1 wherein said gas stream GS1 comprises H2 and CO, wherein said gas stream GS1 is purified in an optional step (ivb) whereby a gas stream GS11 is formed, and(v) subjecting the second waste stream W2 provided in step (ii) or optionally after pretreatment in step (ill) and the optional sixth waste stream W6 to an anaerobic fermentation process AFP in at least one anaerobic fermentation unit AFU and thereby forming a gas stream GS2 wherein said gas stream GS2 comprises CO2 and CH4.2. Process according to embodiment 1 wherein the first waste stream W1 has at least one, preferably all of the following properties: a) a calorific value in the range of 5 to 40 MJ / kg, more preferably of 7 to 35 MJ / kg and most preferably of 10 to 30 MJ / kg, b) a carbon content in the range of 30 to 80 wt.-%, more preferably 35 to 70 wt.-% and most preferably 40 to 70 wt.-%, c) a hydrogen content in the range of 2 to 8 wt.-%, more preferably 3 to 7 wt.-% and most preferably 3.5 to 6 wt.-%, d) an oxygen content in the range of 10 to 60 wt.-%, more preferably 15 to 55 wt.-% and most preferably 20 to 50 wt.-%, e) a nitrogen content in the range of 0.01 to 5 wt.-%, more preferably 0.025 to 2 wt.-% and most preferably 0.05 to 1 wt.-%, f) a sulfur content in the range of 0.025 to 5 wt.-%, more preferably 0.05 to 3 wt.-% and most preferably 0.1 to 2.5 wt.-%, wherein said first waste stream W1 is formed by an acrylic acid production process in said acrylic acid production plant.3. Process according to embodiments 1 or 2 wherein the second waste stream W2 has at least one, preferably all of the following properties: a) a calorific value in the range of 1 to 40 MJ / kg, more preferably of 2 to 30 MJ / kg and most preferably of 3 to 15 MJ / kg, b) comprises less than 90 wt.-% water, more preferably less than 70 wt.-% water and most preferably less than 50 wt.-% water, c) a carbon content in the range of 1 to 30 wt.-%, more preferably 1 .5 to 25 wt.-% and most preferably 2 to 20 wt.-%, d) a hydrogen content in the range of 2 to 20 wt.-%, more preferably 3 to 18 wt.-% and most preferably 5 to 15 wt.-% and e) an oxygen content in the range of 50 to 97 wt.-%, more preferably 57 to 95.5 wt.-% and most preferably 70 to 93 wt.-%, wherein said second waste stream W2 is formed by an acrylic acid production process in said acrylic acid production plant.Process according to any one of embodiments 1 to 3 wherein the acrylic acid separation unit comprises at least one absorption column or at least one condensation unit and wherein the first waste stream W1, the second waste stream W2 and the third waste stream W3 are purged from said at least one absorption column or said at least one condensation unit. Process according to any one of embodiments 1 to 4 wherein the acrylic acid upgrading unit comprises a method selected from the group consisting of solvent-added distillation, solvent-free distillation, azeotropic distillation, extraction combined with distillation and wherein at least one of the further waste streams W4, W5 and W6 is purged from said acrylic acid upgrading unit. Process according to embodiment 5 wherein the optional fifth waste stream W5 has at least one, preferably all of the following properties: a) a calorific value in the range of 5 to 40 MJ / kg, more preferably of 7 to 35 MJ / kg and most preferably of 10 to 30 MJ / kg, b) a carbon content in the range of 30 to 80 wt.-%, more preferably 35 to 70 wt.-% and most preferably 40 to 70 wt.-%, c) a hydrogen content in the range of 2 to 8 wt.-%, more preferably 3 to 7 wt.-% and most preferably 3.5 to 6 wt.-%, d) an oxygen content in the range of 10 to 60 wt.-%, more preferably 15 to 55 wt.-% and most preferably 20 to 50 wt.-%, e) a nitrogen content in the range of 0.01 to 5 wt.-%, more preferably 0.025 to 2 wt.-% and most preferably 0.05 to 1 wt.-% and f) a sulfur content in the range of 0.025 to 5 wt.-%, more preferably 0.05 to 3 wt.-% and most preferably 0.1 to 2.5 wt.-%, wherein said optional fifth waste stream W5 is formed by an acrylic acid production process in said acrylic acid production plant. Process according to any one of embodiments 5 or 6 wherein said optional sixth waste stream W6 has at least one, preferably all of the following properties: a) a calorific value in the range of 1 to 40 MJ / kg, more preferably of 2 to 30 MJ / kg and most preferably of 3 to 15 MJ / kg, b) comprises less than 90 wt.-% water, more preferably less than 70 wt.-% water and most preferably less than 50 wt.-% water, c) a carbon content in the range of 1 to 30 wt.-%, more preferably 1 .5 to 25 wt.-% and most preferably 2 to 20 wt.-%,d) a hydrogen content in the range of 2 to 20 wt.-%, more preferably 3 to 18 wt.-% and most preferably 5 to15 wt.-% and e) an oxygen content in the range of 50 to 97 wt.-%, more preferably 57 to 95.5 wt.-% and most preferably 70 to 93 wt.-%, wherein said optional sixth waste stream W6 is formed by an acrylic acid production process in said acrylic acid production plant.8. Process according to any one of embodiments 1 to 7 wherein the first waste stream W1 and / or the optional fifth waste stream W5 is / are pre-treated by a method selected from the group comprising or consisting of heating, grinding, mixing, pumping and combinations thereof.9. Process according to any one of embodiments 1 to 8 wherein the second waste stream W2 and / or the optional sixth waste stream W6 is / are pretreated by a method selected from the group comprising or consisting of heating, mixing, pumping, evaporation of substances harmful for anaerobic fermentation, iron-carbon micro electrolysis, oxidation with H2O2, catalytic wet air oxidation, treatment of said waste stream(s) with O3 and combinations thereof.10. Process according to any one of embodiments 1 to 9 wherein said at least one gasifier G is selected from plasma gasifier and entrained flow gasifier.11 . Process according to any one of embodiments 1 to 10 wherein the at least one gasifier G is a fixed-bed plasma gasifier.12. Process according to any one of embodiments 1 to 11 wherein a further feedstock F is subjected to a gasification process in step (iv), whereby said further feedstock F is inserted into the at least one gasifier G together with the first waste stream W1 provided in step (I) and with the optional fifth waste stream W5, and / or with the first waste stream W1 and / or optional fifth waste stream W5 pretreated in step (ill).13. Process according to embodiment 12 wherein the further feedstock F is selected from the group comprising biomass, refuse-derived fuel (RDF), pyrolysis oils made from plastic waste, pyrolysis oils made from end of life tires, pyrolysis oils made from biomass, heating oils, vacuum residues, vacuum distillation residues, crude oil residues, heavy crude oils, extra heavy crude oils, tar sand bitumen, visbreaker bottom residues, deasphal- ter bottom residues, C5 asphalthene fraction, high viscous residues, fuel oils, pyrolysis gasolines, tire pyrolysis oils (TPO), waste oils, used oils, municipal solid waste (MSW), automotive shredder residue (ASR), coal, natural gas, industrial waste streams and mixtures thereof.14. Process according to any one of embodiments 12 or 13 wherein the weight ratio (first waste stream W1 and optionally co-fed fifth waste stream W5) : (further feedstock F) preferably ranges from 1 : 1 to 1 : 10, more preferably from 1 : 2 to 1 : 10 and most preferably from 1 : 5 to 1 : 10.15. Process according to any one of embodiments 1 to 14 wherein the gas stream GS1 formed in step (iv) comprises CO, CO2 and H2.16. Process according to embodiment 15 wherein the molar ratio CO : H2 in the gas stream GS1 formed in step(iv) preferably ranges from 0.5 : 1 to 1 : 0.5, more preferably from 0.8 : 1 to 1 : 0.8 and most preferably is about 1 : 1.17. Process according to embodiment 15 or 16 wherein the gas stream GS1 formed in step (iv) preferably comprises < 15 Vol.-% CO2, more preferably < 10 Vol.-% CO2 and most preferably < 8 Vol.-% CO2.18. Process according to any one of embodiments 1 to 17 wherein the process comprises a further step (ivb) said further step (ivb) selected from the group comprising or consisting of cleaning gas stream GS1 and thereby forming gas stream GS11, separating H2 and CO comprised in gas stream GS1 and / or GS11 from each other, compressing at least one of the aforementioned gas streams, and combinations thereof.19. Process according to embodiment 18 wherein step (ivb) comprises, in this order, cleaning gas stream GS1 , d thereby forming gas stream GS11, separating H2 and / or CO from gas stream GS11 and compressing at least one of H2 and CO separated from said gas stream GS11 .20. Process according to any one of embodiments 1 to 19 wherein steam is co-fed into the at least one gasifier G in step (iv).21 . Process according to embodiment 20 wherein the weight ratio "(first waste stream W1 and optionally co-fed fifth waste stream W5 and optionally co-fed further feedstock F) : steam” preferably ranges from 1 : 1 to 10 : 1, more preferably from 2 : 1 to 10 : 1 and most preferably from 5 : 1 to 10 : 1 or higher.22. Process according to any one of embodiments 1 to 21 wherein the at least one gasifier G is an entrained flow gasifier and wherein oxygen and steam are co-fed in step (iv).23. Process according to any one of embodiments 1 to 22 wherein the at least one gasifier G is a plasma gasifier utilizing a plasma and wherein said plasma is formed from one or more sources selected from the group comprising or consisting of H2O, CO2, O2 and air.24. Process according to embodiment 23 wherein the plasma is formed by a method selected from the group comprising or consisting of microwave radiation, electrical arc and plasma torch.25. Process according to embodiment 23 or 24 wherein the plasma is formed by at least one plasma torch.26. Process according to any one of embodiments 1 to 25 wherein a third waste stream W3 is purged from the acrylic acid separation unit and wherein said waste stream W3 is a gaseous waste stream.27. Process according to embodiment 26 wherein the third waste stream W3 preferably comprises 0 to 6 wt.-% carbon, 0 to 12 wt.-% hydrogen, 0 to 95 wt.-% oxygen, 0 to 95 wt.-% nitrogen and 0 to 4 wt.-% sulfur, wherein the sum of carbon, hydrogen, oxygen, nitrogen and sulfur is at least 95 wt.-%.28. Process according to any one of embodiments 1 to 27 wherein a fourth waste stream W4 is purged from the acrylic acid upgrading unit and wherein said waste stream W4 is a gaseous waste stream.29. Process according to embodiment 28 wherein the fourth waste stream W4 preferably comprises 0 to 6 wt.-% carbon, 0 to 12 wt.-% hydrogen, 0 to 95 wt.-% oxygen, 0 to 95 wt.-% nitrogen and 0 to 4 wt.-% sulfur, wherein the sum of carbon, hydrogen, oxygen, nitrogen and sulfur is at least 95 wt.-%.30. Process according to any one of embodiments 26 to 29 wherein the third waste stream W3 and optionally the fourth waste stream W4 is / are treated by at least one method selected from incineration in an incineration unit IU, regenerative thermal oxidation (RTO) and catalytic oxidation.31 . Process according to any one of embodiments 1 to 30 wherein the gas stream GS11 or H2 and / or CO formed therefrom is subjected to a further process FP1 selected from the group comprising CO / H2 splitting, methani- zation, alcohol synthesis (preferably methanol synthesis), and Fischer-Tropsch synthesis whereby at least one first product stream PS1 is formed.32. Process according to any of embodiments 1 to 31 wherein the gas stream GS2 formed in step (v) is subjected to a fermentation product upgrading unit FUU in an optional step (vi) whereby a gas stream GS22 is formed.33. Process according to embodiments 32 wherein the fermentation product upgrading unit FUU is selected from the group comprising or consisting of steam reforming unit, dry reforming unit, and hydrocarbon pyrolysis unit.34. Process according to any one of embodiments 1 to 33, comprising the step:- converting the gas stream GS1 obtainable by or formed in step (iv) and / or gas stream GS11 obtainable by or formed in optional step (ivb) and / or gas stream GS22 obtainable by or formed in optional step (vi) to obtain a product.35. Process according to embodiment 34, wherein the product is selected from:I) building block or monomer; orii) polymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; or ill) cleaning polymer, cleaning surfactant, descaling compound, cleaning biocide or composition or formulation thereof; or iv) agrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; or v) active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, human food additive, dietary supplements, aroma chemical or 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 polyol, polymeric dispersant for inorganic binder compositions, unsaturated polyester polyol or 100% curable composition; or vii) cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or composition or formulation thereof; or viii) polymer B, polymer composition B, coating composition, other functional composition, foil, molded body, coating or coated substrate. Process according to embodiments 34 or 35, wherein the content of the gas stream GS1 obtainable by or formed in step (iv) and / or at least one of the gas stream GS11 obtainable by or formed in step (ivb) and / or gas stream GS22 obtainable by or formed in optional step (vi) in the product is 1 weight-% or more, preferably 2 weight-% or more, more preferably 5 weight- % or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and / or wherein the content of the gas stream GS1 obtainable by or formed in step (iv) and / or at least one of the gas stream GS11 obtainable by or formed in step (ivb) and / or gas stream GS22 obtainable by or formed in optional step (vi) in the product is 100 weight- % or less, preferably 95 weight-% or less, more preferably 90 weight-% or less, more preferably 50 weight-% or less, more preferably 25 weight-% or less, more preferably 10 weight-% or less; and preferably wherein the content is determined based on identity preservation and / or segregation and / or mass balance and / or book and claim chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard. Acrylic acid production plant comprising an integrated waste stream treatment facility wherein said acrylic acid production plant comprises a) an acrylic acid production unit AAPU, b) an acrylic acid separation unit AASU downstream and fluidically connected to said acrylic acid production unit AAPU, said acrylic acid separation unit AASU purging a first waste stream W1, c) an acrylic acid upgrading unit AAUU downstream and fluidically connected to said acrylic acid separation unit AASU,d) at least one gasifier G downstream and directly or indirectly fluidically connected to said acrylic acid separation unit AASU and e) at least one anaerobic fermentation unit AFU downstream of and directly or indirectly fluidically connected to said acrylic acid separation unit AASU.38. Acrylic acid production plant according to embodiment 37 wherein the at least one gasifier G is directly or indirectly fluidically connected to the first waste stream W1 of the acrylic acid separation unit AASU.39. Acrylic acid production plant according to embodiments 37 or 38 wherein the at least one anaerobic fermentation unit AFU is directly or indirectly fluidically connected to the second waste stream W2 of the acrylic acid separation unit AASU.40. Acrylic acid production plant according to any one of embodiments 37 to 39 wherein the acrylic acid upgrading unit AAUU comprises a method selected from the group consisting of crystallization and distillation.41 . Acrylic acid production plant according to embodiment 37 or 40 wherein the acrylic acid upgrading unit AAUU comprises a method selected from the group consisting of solvent-added distillation, solvent-free distillation, azeotropic distillation, reactive distillation, extraction, and combinations thereof wherein said acrylic acid upgrading unit AAUU purges at least one of waste streams W5 and W6.42. Acrylic acid production plant according to embodiment 41 wherein the at least one gasifier G is directly or indirectly fluidically connected to the fifth waste stream W5.43. Acrylic acid production plant according to embodiments 41 or 42 wherein the at least one anaerobic fermentation unit AFU is directly or indirectly fluidically connected to the sixth waste stream W6.44. Use of an acrylic acid production plant according to any one of embodiments 37 to 43 for the process according to any one of embodiments 1 to 33.45. A computer program comprising instructions which, when the program is executed by the plant according to any one of embodiments 37 to 43, cause the plant to perform the process according to any one of embodiments 1 to 33.The invention will be further explained by the following non-limiting examples.Examples General descriptionA gasification agent (steam) was injected into the gasifier G, enabling a plasma gasification reaction at a temperature of 1350 °C (Examples 1 and 2) or an entrained flow gasification at 1350 °C (Examples 3 and 4). A plasma was formed in case of plasma gasification from the inserted steam at the plasma torch outlets of the gasifier G. The plasma generation was performed by electric energy with a power given for the individual examples. The resulting raw synthesis gas (stream GS1), comprising CO, H2O, CO2, H2 and optionally ash or dust, which left the gasifier G via the gas outlet of the gasifier G was washed and dried to reduce the amount of water and ash comprised therein. Slag was removed from the gasifier G directly. After washing and drying, the gas stream GS1 had a temperature of 25 °C and was subjected to acid gas removal, by amine scrubbing, to separate acids such as CO2. The composition and normalized mass flow of the respective gas stream GS11 is given in the tables below.Table 1: Results from examples 1 to 4. feed stream: mass flow steam: gasifier G, GS11 composition pressure mass flow el. power con- temperature pressure sumption per composition temperature kg GS2 producedExample 1 W1 2.40 kg feed / kg 1.68 kg plasma 67.1 Vol.-% H2GS11 kg / h steam / kg GS2 7.4kW / kg 30.0Vol.-%C01 bar(abs.) 5.4 bar(abs.) GS2 rest steam100 °C 180 °C23.7 wt.-% C 8.4 wt.-% H67.9 wt.-% 0Example 2 W1 0.94 kg feed / kg 3.75 kg plasma 14.5Vol.-%H2GS11 kg / h steam / kg GS2 9.7 kW / kg 78.4Vol.-%C01 bar(abs.) 5.4 bar(abs.) GS2 rest steam100 °C 180 °C61.6wt.-%C 5wt.-%H 31.4wt.-%0Example 3 W1 +F(=tor- 0.66 kg feed / kg steam: entrained flow 36.3 Vol. -%H2refiedwood) GS11 kg / h 0.06kg gasification 61.8Vol.-%C047 bar(abs.) steam / kg GS2 rest steam100 °C 70 bar(abs.)62.2 wt.-% C 400 °C5.2 wt.-% H Oxygen:21.3 wt.-% 0 0.4 kg O2 / kg11.2 wt.-% ash GS247 bar(abs.) 25 °CExample 4 W1 +F(=tor- 0.63 kg feed / kg steam: entrained flow 44.9 Vol. -%H2refiedwood) GS11 kg / h 0.25 kg gasification 54.4 Vol. -% CO47 bar(abs.) steam / kg GS2 rest steam100 °C 70 bar(abs.)64.9 wt.-% C 400 °C5.0 wt.-% H Oxygen:18.3 wt.-% 0 0.2 kg O2 / kg11.7 wt.-% ash GS247 bar(abs.)25 °C

Claims

Claims1. Process for utilizing at least one waste stream from an acrylic acid production plant, wherein the acrylic acid production plant comprises a) an acrylic acid production unit, b) an acrylic acid separation unit, and c) an acrylic acid upgrading unit, the process comprising the steps(I) providing a first waste stream W1 , wherein the first waste stream W1 is separated from the acrylic acid separation unit,(ii) providing a second waste stream W2, wherein the second waste stream W2 is separated from the acrylic acid separation unit,(iia) optionally providing a fifth waste stream W5 and / or a sixth waste stream W6 and / or a further feedstock F, wherein said optional fifth waste stream W5 and said optional sixth waste stream W6 are separated from the acrylic acid upgrading unit,(ill) optionally pretreating the first waste stream W1 and / or the second acrylic acid waste stream W2, and / or the optional fifth waste stream W5 and / or the optional sixth waste stream W6 and / or the optional further feedstock F,(iv) subjecting the first waste stream W1 provided in step (I) or optionally after pretreatment in step (ill) and the optional fifth waste stream W5 to a gasification process at a temperature between 800 and1500 °C, wherein said gasification process comprises at least one gasifier G and thereby forming a gas stream GS1 wherein said gas stream GS1 comprises H2 and CO, wherein said gas stream GS1 is purified in an optional step (ivb) whereby a gas stream GS11 is formed, and(v) subjecting the second waste stream W2 provided in step (ii) or optionally after pretreatment in step (ill) and the optional sixth waste stream W6 to an anaerobic fermentation process AFP in at least one anaerobic fermentation unit AFU and thereby forming a gas stream GS2 wherein said gas stream GS2 comprises CO2 and CH4.

2. Process according to claim 1 wherein the first waste stream W1 has at least one, preferably all of the following properties: a) a calorific value in the range of 5 to 40 MJ / kg, more preferably of 7 to 35 MJ / kg and most preferably of 10 to 30 MJ / kg, b) a carbon content in the range of 30 to 80 wt.-%, more preferably 35 to 70 wt.-% and most preferably 40 to 70 wt.-%, c) a hydrogen content in the range of 2 to 8 wt.-%, more preferably 3 to 7 wt.-% and most preferably 3.5 to 6 wt.-%,d) an oxygen content in the range of 10 to 60 wt.-%, more preferably 15 to 55 wt.-% and most preferably 20 to 50 wt.-%, e) a nitrogen content in the range of 0.01 to 5 wt.-%, more preferably 0.025 to 2 wt.-% and most preferably 0.05 to 1 wt.-%, f) a sulfur content in the range of 0.025 to 5 wt.-%, more preferably 0.05 to 3 wt.-% and most preferably 0.1 to 2.5 wt.-%, wherein said first waste stream W1 is formed by an acrylic acid production process in said acrylic acid production plant.

3. Process according to claims 1 or 2 wherein the second waste stream W2 has at least one, preferably all of the following properties: a) a calorific value in the range of 1 to 40 MJ / kg, more preferably of 2 to 30 MJ / kg and most preferably of 3 to 15 MJ / kg, b) comprises less than 90 wt.-% water, more preferably less than 70 wt.-% water and most preferably less than 50 wt.-% water, c) a carbon content in the range of 1 to 30 wt.-%, more preferably 1 .5 to 25 wt.-% and most preferably 2 to 20 wt-%, d) a hydrogen content in the range of 2 to 20 wt.-%, more preferably 3 to 18 wt.-% and most preferably 5 to15 wt.-% and e) an oxygen content in the range of 50 to 97 wt.-%, more preferably 57 to 95.5 wt.-% and most preferably 70 to 93 wt.-%, wherein said second waste stream W2 is formed by an acrylic acid production process in said acrylic acid production plant.

4. Process according to any one of claims 1 to 3 wherein the first waste stream W1 is pre-treated by a method selected from the group comprising or consisting of heating, grinding, mixing, pumping and combinations thereof.

5. Process according to any one of claims 1 to 4 wherein the second waste stream W2 is pretreated by a method selected from the group comprising or consisting of heating, mixing, pumping, evaporating and combinations thereof.

6. Process according to any one of claims 1 to 5 wherein said at least one gasifier G is selected from plasma gasifier and entrained flow gasifier.

7. Process according to any one of claims 1 to 6 wherein a further feedstock F is subjected to a gasification process in step (iv), whereby said further feedstock F is inserted into the at least one gasifier G together with the first waste stream W1 provided in step (I) and with the second waste stream W2 optionally provided in step (ii), and / or with the first waste stream W1 and / or second waste stream W2 pretreated in step (ill).

8. Process according to claim 7 wherein the further feedstock F is selected from the group comprising biomass, refuse-derived fuel (RDF), pyrolysis oils made from plastic waste, pyrolysis oils made from end of life tires, pyrolysis oils made from biomass, heating oils, vacuum residues, preferably vacuum distillation residues, crude oil residues, heavy crude oils, extra heavy crude oils, tar sand bitumen, visbreaker bottom residues, deasphalter bottom residues, C5 asphalthene fraction, high viscous residues, fuel oils, pyrolysis gasolines, tire pyrolysis oils (TPO), waste oils, used oils, municipal solid waste (MSW), automotive shredder residue (ASR), coal, natural gas, industrial waste streams and mixtures thereof.

9. Process according to any one of claims 7 or 8 wherein the weight ratio (first waste stream W1 and optionally co-fed fifth waste stream W5) : (further feedstock F) preferably ranges from 1 : 1 to 1 : 10, more preferably from 1 : 2 to 1 : 10 and most preferably from 1 : 5 to 1 : 10.

10. Process according to any one of claims 1 to 9 wherein the process comprises a further step (ivb) said further step (ivb) selected from the group comprising or consisting of cleaning, separating H2 and CO from each other, compressing and combinations thereof.11 . Process according to any of claims 1 to 10 wherein the gas stream GS2 formed in step (v) is subjected to a fermentation product upgrading unit FUU in a step (vi) whereby a gas stream GS22 is formed.

12. Process according to claim 11 wherein the fermentation product upgrading unit FUU is selected from the group comprising or consisting of steam reforming unit, dry reforming unit, and hydrocarbon pyrolysis unit.

13. Process according to any one of claims 1 to 12, comprising the step:- converting the gas stream GS1 obtainable by or formed in step (iv) and / or gas stream GS11 obtainable by or formed in optional step (ivb) and / or gas stream GS22 obtainable by or formed in optional step (vi) to obtain a product.

14. Process according to claim 13, wherein the product is selected from:I) building block or monomer; or ii) polymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; or ill) cleaning polymer, cleaning surfactant, descaling compound, cleaning biocide or composition or formulation thereof; or iv) agrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; or v) active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, human food additive, dietary supplements, aroma chemical or aroma composition; orvi) aqueous polymer dispersion, preferably polyurethane or polyurethane - poly(meth)acrylate hybrid polymer dispersion, emulsion, binder for paper and fiber coatings, UV-curable acrylic polymer for hot melts and coatings polyisocyanates, hyperbranched polyester polyol, polymeric dispersant for inorganic binder compositions, unsaturated polyester polyol or 100% curable composition; or vii) cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or composition or formulation thereof; or viii) polymer B, polymer composition B, coating composition, other functional composition, foil, molded body, coating or coated substrate.

15. Acrylic acid production plant comprising an integrated waste stream treatment facility wherein said acrylic acid production plant comprises a) an acrylic acid production unit AAPU, b) an acrylic acid separation unit AASU downstream and fluidically connected to said acrylic acid production unit AAPU, said acrylic acid separation unit AASU purging a first waste stream W1, c) an acrylic acid upgrading unit AAUU downstream and fluidically connected to said acrylic acid separation unit AASU, d) at least one gasifier G downstream and directly or indirectly fluidically connected to said acrylic acid separation unit AASU and e) at least one anaerobic fermentation unit AFU downstream of and directly or indirectly fluidically connected to said acrylic acid separation unit AASU.

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