Method for gasification of polymeric recyclable materials for the low-emission supply of carbon monoxide usable for the production of phosgene

Abstract

The invention relates to a method according to claim 1 for the low-emission production of carbon monoxide (CO) for the production of phosgene, from which, for example, polycarbonates or organic isocyanates, and polyurethanes therefrom, can be produced using a process for the partial oxidation with gasification of polymeric recyclable materials. The invention further relates to a device that can be used for this purpose and to the use of said gasification process and / or polymeric recyclable materials to provide carbon monoxide for the production of phosgene.

Description

[0001] Process for the gasification of polymeric recyclable materials for low-emission

[0002] Provision of carbon monoxide usable for the production of phosgene

[0003] The invention relates to a process for the low-emission production of carbon monoxide (CO) for the production of phosgene, from which, for example, polycarbonates or organic isocyanates and, therefrom, polyurethanes can be produced, using a process for partial oxidation with gasification of valuable polymeric materials. Furthermore, the invention relates to a device usable for this purpose and the use of said gasification process or the valuable polymeric materials to provide carbon monoxide for the production of phosgene.

[0004] At the end of their service life, products containing polymer materials are replaced with new ones and usually scrapped. The total amount of resulting plastic waste increases every year. Approximately 60% of the total is disposed of by incineration and landfilling. Incineration releases CO2 into the air, which contributes to global warming. Due to its low density, plastic waste in landfills takes up a large volume and can also contribute to general pollution in rivers and oceans. For this reason, it is important to develop an efficient recycling method that can solve the waste problem and simultaneously conserve fossil resources. Due to the growing plastics market, it is important to develop recycling technologies for all polymer classes in order to both reduce CO2 emissions and conserve fossil fuels.

[0005] The processes for recycling plastic waste can be roughly divided into 3 categories:

[0006] (1) Mechanical recycling: In this process, the plastic waste is melted down as it is and can then be reused. This is not possible for polyurethane elastomers.

[0007] (2) chemical and thermochemical recycling: Here, the plastic waste is depolymerized into monomers or decomposed into smaller molecules to obtain useful chemical raw materials and (3) thermal recycling, in which the plastic waste is converted into exhaust gas and thermal energy.

[0008] The chemical raw materials obtained from thermochemical recycling can be used to synthesize new synthetic resins or other chemical products.

[0009] One raw material for the production of polyurethane polymers or polycarbonate polymers is carbon monoxide, which is converted with chlorine gas to phosgene. Carbon monoxide and hydrogen are conventionally obtained from natural gas or coal using reforming processes, and chlorine is obtained from electrolysis using electricity generated using fossil fuels such as oil, coal, or natural gas. This process produces a significant amount of CO2.

[0010] It is an object of this invention to provide a more sustainable process for carbon monoxide production. The "sustainability" of a process is understood by those skilled in the art, applying the UN definition of sustainability ("sustainable development") according to the Brundtland Report of the "World Commission on Environment and Development", to mean that the implementation of the process in the present makes as little or no contribution as possible to ensuring that future generations of humanity will no longer be able to meet their own needs, in particular needs with regard to the use of resources such as fossil fuels and in particular with regard to the conservation of habitats, such as the protection of the Earth's atmosphere.

[0011] The invention therefore aims to make the production of carbon monoxide more sustainable than the production methods known from the state of the art, whereby this solution should be as easy as possible to integrate into existing production lines.

[0012] In this context, it is an object of the present invention to reduce CCh emissions during the provision of carbon monoxide.

[0013] Carbon monoxide can be produced from various sustainable processes. For example, through a reformer process, in which natural gas from a fossil source is fed in, along with biomethane, carbon dioxide, and / or hydrogen. The energy required for the reformer process is generated from the combustion of natural gas, biomethane, hydrogen, or through electrical heating. Furthermore, CO2 can be produced from CO2 and H2 in the reverse water gas shift reaction, with the hydrogen coming from water electrolysis. Another option is the electrochemical reduction of CO2 to CO2.

[0014] However, according to the process of the invention, CO is produced from used polymer waste fractions and oxygen gas by gasification with partial oxidation (hereinafter also referred to as gasification). By using polymer-containing waste fractions, which can, for example, consist predominantly of polyurethane- or polycarbonate-containing waste fractions (hereinafter referred to as polymer waste fraction), polycarbonate material or isocyanates and the resulting new polyurethane material can be produced with improved sustainability. Part of the carbon is recycled in the process.

[0015] The process according to the invention causes the polymer waste fraction and oxygen to undergo a partial oxidation reaction, resulting in a product gas mixture containing hydrogen and CO, and optionally by-products. By-products include, in particular, hydrocarbons with 1 to 8 carbon atoms. CO2 and water vapor are also present in the product gas mixture.

[0016] As a further by-product, a residual fraction that cannot be further processed is obtained from the gasification process.

[0017] The temperature required for gasification is at least partially achieved by partial combustion (partial oxidation) of the polymer waste fraction with an oxygen-containing gas.

[0018] To achieve at least one of the above-mentioned objects, the invention firstly provides a process for providing carbon monoxide for the preparation of phosgene, preferably for the preparation of phosgene for the synthesis of organic isocyanate compounds, comprising at least the following steps: a) providing an oxygen-containing gas stream comprising at least 50% by weight.-% oxygen gas, b) partial oxidation of material containing at least one polymeric, organic compound, wherein said material is introduced into a reactor of a device and treated there at least by supplying said oxygen-containing gas stream and heat at at least 400°C to form a product gas and the resulting product gas, optionally after at least one further partial oxidation step of the product gas, is discharged from the device as a carbon monoxide-containing product gas stream together with particulate solid dispersed therein; c) the carbon monoxide-containing product gas stream is fed to a purification step in which at least c) the carbon monoxide-containing product gas stream is fed to a washing step for separating solid, in which.

[0019] (i) water is brought into contact with the carbon monoxide-containing product gas stream, whereby the particulate solid dispersed in the carbon monoxide-containing product gas stream forms a slag and this slag is removed and discharged,

[0020] (ii) the carbon monoxide-containing product gas stream purified of particulate solids is discharged; c2) a carbon monoxide-containing product gas stream purified of particulate solids by a washing step is fed to at least one water separation unit in a drying step, water is separated off, and the resulting carbon monoxide-containing product gas stream is discharged; c3) a carbon monoxide-containing product gas stream purified by water separation is fed to at least one carbon dioxide separation unit, carbon dioxide is separated off, and the resulting carbon monoxide-containing product gas stream and carbon dioxide are discharged; c4) a carbon monoxide-containing product gas stream purified by carbon dioxide separation is fed to at least one carbon monoxide separation unit, carbon monoxide is separated off, and the resulting carbon monoxide and a hydrogen gas-containing residual gas are discharged;c5) optionally, a hydrogen gas-containing residual gas separated by said separation unit is fed to a residual gas treatment plant, hydrogen gas is separated, and hydrogen gas and a tail gas are discharged; d) optionally, phosgene synthesis is carried out by reacting at least chlorine gas and carbon monoxide, wherein at least the carbon monoxide from the separation unit is reacted to separate carbon monoxide, and phosgene is discharged.

[0021] A solid is known to be "particulate" if it exists in the form of a granular mixture of a large number of loose, solid particles of the substance in question, which in turn includes so-called grains. A grain is a term used to describe the particulate components of powders (grains are the loose, solid particles), dusts (grains are the loose, solid particles), granules (loose, solid particles are agglomerates of several grains), and other granular mixtures.

[0022] An "organic compound" contains at least one covalent carbon-hydrogen bond in its molecule. An organic isocyanate is therefore an organic substance that, as a chemical compound, contains at least one isocyanate group and at least one covalent carbon-hydrogen bond in its molecule. An organic amine is defined mutatis mutandis.

[0023] A “polymeric compound” is a molecule with a relative molar mass (Mw) of at least 2000 g / mol, the chemical structure of which predominantly comprises multiply repeating structural units derived from one or more different molecules of lower relative molar mass. Unless explicitly stated otherwise, the average molar masses stated for polymers or polymeric compounds in this application are always weight-average molar masses Mw, which can generally be determined by gel permeation chromatography using an RI detector, with the measurement conveniently being carried out against an external standard. The person skilled in the art understands “renewable energy” to mean energy from a non-exhaustive energy source, such as wind energy, hydropower, bioenergy (e.g., power generation from biogas or biomass) or solar energy.Therefore, wind power, solar energy, hydropower or a mixture of these are particularly suitable as renewable energies.

[0024] A "reactor" is a volume in which a chemical transformation, such as the partial oxidation of a polymeric, organic compound of a material, takes place. For partial oxidation, this could be, for example, the volume of a heated vessel containing the material.

[0025] The oxygen-containing gas stream provided contains at least 50 wt.% oxygen gas. Preferably, the oxygen-containing gas stream contains at least 60 wt.% oxygen gas, more preferably at least 75 wt.% oxygen gas.

[0026] The oxygen gas required for this can be taken, for example, from a water electrolysis plant or an air separation plant, which supplies the nitrogen, particularly in the production of ammonia. Thus, the value chain of the aforementioned polymers can be closed with respect to the carbon from carbon monoxide. In a preferred embodiment of the process, to provide the oxygen-containing gas stream, water is electrolyzed to obtain oxygen gas and hydrogen gas, and the oxygen gas from this electrolysis (22) is used to provide the oxygen-containing gas stream.

[0027] Water electrolysis can be carried out using state-of-the-art systems. Well-known and commercially available systems include both alkaline water electrolysis and polymer electrolyte-based electrolysis, known as PEM electrolysis. The principles of water electrolysis are described in Chapter 6.3.4 of Volkmar M. Schmidt's "Electrochemical Process Engineering" (2003, Wiley-VCH-Verlag; ISBN 3-527-29958-0).

[0028] In addition to introducing the oxygen-containing gas stream, it may be preferable according to the invention to additionally introduce gaseous water into the at least one partial oxidation reactor and to carry out the partial oxidation of said material in the presence of a mixture of oxygen gas and gaseous water. It has proven particularly preferred if gaseous water is additionally supplied to the reactor in a weight ratio of gaseous water to oxygen gas of the oxygen-containing gas stream of at least 0.2.

[0029] The gaseous water and the oxygen-containing gas stream can be introduced into the reactor separately, or the gaseous water can be mixed with the oxygen-containing gas stream before being introduced into the reactor and introduced into the reactor together with the oxygen-containing gas stream as a component thereof.

[0030] According to the invention, the material introduced into the reactor contains at least one polymeric, organic compound. The partial oxidation should take place as uniformly and selectively as possible in the reactor. These parameters can be improved if, in a preferred embodiment, the weight ratio of the oxygen gas contained in the oxygen-containing gas stream to the polymeric, organic compound is introduced into the reactor within a weight ratio range of 0.4 to 1.0 to 1.2 to 1.0, preferably 0.6 to 1.0 to 0.9 to 1.0, based on the time before introduction.

[0031] It has proven advantageous if the material in question is introduced into the reactor in particulate form, in the form of solid particles (particularly in the form of a granular mixture). A granular mixture of the material in question is formed from a multitude of loose, solid particles of the material in question, which in turn comprise so-called grains. A grain is a term for the particulate components of powders (grains are the loose, solid particles), dusts (grains are the loose, solid particles), granules (loose, solid particles are agglomerates of several grains), and other granular mixtures.

[0032] Preferably, the solid particles, in particular the loose, solid particles of the granular mixture, of said material introduced into the reactor have an average diameter X50,3 (volume average) of 0.01 mm to 5 cm, preferably of 0.1 mm to 5 cm. The average particle size diameter X50,3 is determined by sieving or using a Camsizer particle size analyzer from Retsch. Further preferred average particle diameters are described below, depending on the reactor type selected.

[0033] It has proven preferable to preselect the material in question based on its composition before introduction into the reactor. This results in an improved and more consistent quality of the resulting product gas over the operating time of the partial oxidation. In this context, a minimum amount of polymeric organic compound and a minimum proportion of carbon have proven advantageous.

[0034] In a preferred embodiment, it is therefore advantageous if the total amount of all polymeric, organic compounds contained in the material is at least 50% by weight, preferably at least 60% by weight, particularly preferably at least 75% by weight.

[0035] A further preferred embodiment of the process is characterized in that the total amount of all polymeric, organic compounds contained in the material has a carbon content of at least 40.0 wt.%, preferably of at least 50 wt.%.

[0036] In a particularly preferred embodiment of the process, the total amount of all polymeric, organic compounds contained in the material is at least 50 wt.% (preferably at least 60 wt.%, particularly preferably at least 75 wt.%), wherein the total amount of all polymeric, organic compounds contained in the material has a carbon content of at least 40.0 wt.%, preferably at least 50 wt.%.

[0037] A particularly preferred and therefore particularly suitable material contains as polymeric, organic compound those which are selected from at least one homopolymeric or copolymeric compound from the group cellulose, polyester, polyamide, polyurethane (PUR), polyurea, polyisocyanurate (PIR), polycarbonate, preferably from at least one homopolymeric or copolymeric compound from the group polyurethane (PUR), polyisocyanurate (PIR). Polymeric, organic compounds which have at least one repeating unit which is derived from monomers having a carbonyl group which form at least one linkage selected from urethane linkage, carbonate linkage, ester linkage, amide linkage or isocyanurate linkage in the polymeric, organic compound are very particularly preferably suitable as polymeric, organic compounds in said material for partial oxidation according to a further preferred embodiment of the process according to the invention.A particularly preferred embodiment of the process is a process in which the structure of the polymeric, organic compound of the material fed to the partial oxidation contains at least one repeating structural unit of the formula (I). wherein

[0038] X 1 and X 2 independently of one another represent a direct bond, O or NH, preferably O or NH,

[0039] Y 1 and Y 2 independently represent O or NH,

[0040] R 1 and R 2 independently of one another each represent any bivalent, carbon-containing structural element, and a covalent bond marked with * means a bond to the remaining molecule of the polymeric, organic compound.

[0041] Within the scope of this most preferred embodiment, it has proven suitable if the total amount of polymeric, organic compounds containing at least one repeating structural unit of the formula (I) present in the material is at least 50 wt.%, preferably at least 60 wt.%, particularly preferably at least 75 wt.%. If, according to formula (I), X1 and X2 represent an NH group and Y1 and Y2 represent O, then the polymeric, organic compound contains the urethane linkage very particularly preferred according to the invention. Such polymeric, organic compounds very particularly preferably contained in said material can be prepared by reacting at least 11) at least one organic isocyanate compound containing at least two to four, in particular two isocyanate groups bonded to a hydrocarbon unit having 2 to 8 carbon atoms, preferably having 3 to 8 carbon atoms; with

[0042] 12) at least one organic compound having at least two hydroxyl groups.

[0043] The at least one organic isocyanate compound may contain, as said hydrocarbon unit, a unit which has the number of carbon atoms mentioned in il) and is derived from aliphatic hydrocarbon units, cycloaliphatic hydrocarbon units, araliphatic hydrocarbon units, aromatic hydrocarbon units or heterocyclic hydrocarbon units.

[0044] As said organic isocyanate compound, at least one compound according to formula (II) is particularly preferably selected

[0045] Q(NCO) n(II) wherein n is a number from 2 to 10, preferably from 2 to 6, and Q is a radical selected from an aliphatic hydrocarbon radical having 2 to 70 carbon atoms (preferably having 3 to 30 carbon atoms), a cycloaliphatic hydrocarbon radical having 3 to 30 carbon atoms, an aromatic hydrocarbon radical having 6 to 70 carbon atoms (preferably having 6 to 30 carbon atoms) or an araliphatic hydrocarbon radical having 6 to 70 carbon atoms (preferably having 6 to 30 carbon atoms).

[0046] It is preferred if in step il) at least one diisocyanate of the formula (IIIa) or (IIIb) is selected as at least one organic polyisocyanate compound, wherein n is a number from 0 to 8, in particular from 0 to 4, more preferably from 0 to 2.

[0047] Preferably, in step i2) for the preparation of the polymeric, organic compound, at least one organic compound having at least two hydroxyl groups is selected from polyester polyol, polyether polyol, polycarbonate polyol, polyether ester polyol, polyacrylate polyol, polyester polyacrylate polyol or mixtures thereof, particularly preferably selected from the group of polyether polyols and / or polyester polyols.

[0048] The OH number of the organic compound used with at least two hydroxyl groups or of the organic compounds used with at least two hydroxyl groups, each according to DIN 53240-1 (June 2013), is preferably from 15 to 4000 mg KOH / g. If more than one organic compound with at least two hydroxyl groups is used, the mixture of said compounds can preferably have a hydroxyl number between 20 and 200 mg KOH / g, in particular 25 to 100 mg KOH / g. The OH number (also: hydroxyl number) indicates the OH number of a single added organic compound with at least two hydroxyl groups. Information on the OH number for mixtures refers to the number-average OH number of the mixture, calculated from the OH numbers of the individual components in their respective molar proportions. The OH number indicates the amount of potassium hydroxide in milligrams which is equivalent to the amount of acetic acid bound during acetylation of one gram of substance.In the context of this discussion, it is determined according to the standard DIN 53240-1 (June 2013).

[0049] Preferably, the organic compounds having at least two hydroxyl groups have a number-average molecular weight of > 100 g / mol to < 15000 g / mol, in particular > 2000 g / mol to < 12000 g / mol, more preferably ≥ 3500 g / mol to ≤ 6500 g / mol.

[0050] The number average molar mass Mn (also: molecular weight) is determined in this context by gel permeation chromatography according to DIN 55672-1 of August 2007, unless explicitly specified otherwise elsewhere.

[0051] The organic compounds having at least two hydroxyl groups have a functionality of 1 to 8, whereby “functionality” in the context of the present invention refers to the theoretical average functionality (number of functions in the molecule that are reactive towards isocyanates or polyols) calculated from the known starting materials and their quantitative ratios.

[0052] Usable polyetherester polyols are compounds that contain ether groups, ester groups, and OH groups. Preferably, organic dicarboxylic acids with up to 12 carbon atoms are used to produce the polyetherester polyols, preferably aliphatic dicarboxylic acids with 4 to 6 carbon atoms or aromatic dicarboxylic acids, which are used individually or in a mixture. Examples include suberic acid, azelaic acid, decanedicarboxylic acid, malonic acid, phthalic acid, pimelic acid, and sebacic acid, and in particular glutaric acid, fumaric acid, succinic acid, adipic acid, phthalic acid, terephthalic acid, and isophthalic acid. In addition to organic dicarboxylic acids, derivatives of these acids, for example their anhydrides and their esters and half-esters with low-molecular-weight, monofunctional alcohols with 1 to 4 carbon atoms, can also be used. The proportional use of the above-mentioned bio-based starting materials, in particular fatty acids orFatty acid derivatives (oleic acid, soybean oil, etc.) are also possible and can offer advantages, e.g. with regard to storage stability of the polyol formulation, dimensional stability, fire behavior and compressive strength of the foams.

[0053] Polyether polyols, which are obtained by alkoxylating starter molecules such as polyhydric alcohols, are used as a further component in the production of polyetherester polyols. The starter molecules are at least difunctional, but may optionally also contain portions of higher-functionality, particularly trifunctional, starter molecules.

[0054] Starter molecules are, for example, ethylene glycol, propylene glycol, 1,3-butanediol, 1,4-butanediol, 1,5-pentenediol, 1,5-pentanediol, 1,6-hexanediol, 1,7-heptanediol, 1,8-octanediol, 1,10-decanediol, 2-methylpropane-1,3-diol, neopentyl glycol, 2,2-dimethyl-1,3-propanediol, 3-methyl-1,5-pentanediol, 2-butyl-2-ethyl-1,3-propanediol, 2-butene-1,4-diol and 2-butyne-1,4-diol, diethylene glycol, dipropylene glycol, glycerin, trimethylolpropane, di- and trifunctional polyether polyols. The polyether polyols preferably have an OH functionality of 2 to 4 and a molecular weight Mn in the range of 62 to 4500 g / mol, and in particular a molecular weight Mn in the range of 62 to 3000 g / mol. Starter molecules with functionalities other than OH can also be used alone or in mixtures.Polyetherester polyols can also be prepared by alkoxylation, particularly by ethoxylation and / or propoxylation, of reaction products obtained by reacting organic dicarboxylic acids and their derivatives, as well as components containing Zerewitinoff-active hydrogens, particularly diols and polyols. Derivatives of these acids can include, for example, their anhydrides.

[0055] The polyester polyols can be, for example, polycondensates of polyhydric alcohols, preferably diols, having 2 to 12 carbon atoms, preferably 2 to 6 carbon atoms, and polycarboxylic acids, such as di-, tri-, or even tetracarboxylic acids or hydroxycarboxylic acids or lactones. Aromatic dicarboxylic acids or mixtures of aromatic and aliphatic dicarboxylic acids are preferred. Instead of the free polycarboxylic acids, the corresponding polycarboxylic acid anhydrides or corresponding polycarboxylic acid esters of lower alcohols can also be used to produce the polyesters.

[0056] Particularly suitable carboxylic acids are: succinic acid, glutaric acid, adipic acid, suberic acid, azelaic acid, sebacic acid, decanedicarboxylic acid, tetrahydrophthalic acid, hexahydrophthalic acid, cyclohexanedicarboxylic acid, tetrachlorophthalic acid, itaconic acid, malonic acid, 2-methylsuccinic acid, 3,3-diethylglutaric acid, 2,2-dimethylsuccinic acid, dodecanedioic acid, endomethylenetetrahydrophthalic acid, dimer fatty acid, trimer fatty acid, citric acid, trimellitic acid, benzoic acid, maleic acid, fumaric acid, phthalic acid, isophthalic acid, and terephthalic acid. Derivatives of these carboxylic acids, such as dimethyl terephthalate, can also be used. The carboxylic acids can be used individually or in mixtures. Preferred carboxylic acids are adipic acid, sebacic acid, and / or succinic acid, particularly preferably adipic acid and / or succinic acid.

[0057] Hydroxycarboxylic acids that can be used as reactants in the production of a polyester polyol with terminal hydroxyl groups include, for example, lactic acid, malic acid, hydroxycaproic acid, hydroxybutyric acid, hydroxydecanoic acid, hydroxystearic acid, and the like. Suitable lactones include caprolactone, butyrolactone, and homologues. Bio-based starting materials and / or their derivatives are also particularly suitable for the production of polyester polyols, such as:Castor oil, polyhydroxy fatty acids, ricinoleic acid, hydroxyl-modified oils, grape seed oil, black caraway oil, pumpkin seed oil, borage seed oil, soybean oil, wheat seed oil, rapeseed oil, sunflower seed oil, peanut oil, apricot kernel oil, pistachio oil, almond oil, olive oil, macadamia nut oil, avocado oil, sea buckthorn oil, sesame oil, hemp oil, hazelnut oil, primrose oil, rosehip oil, safflower oil, walnut oil, fatty acids, hydroxyl-modified and epoxidized fatty acids and fatty acid esters, for example based on myristoleic acid, palmitoleic acid, oleic acid, vaccenic acid, petroselinic acid, gadoleic acid, erucic acid, nervonic acid, linoleic acid, alpha- and gamma-linolenic acid, stearidonic acid, arachidonic acid, timnodonic acid, clupanodonic acid and cervonic acid. Particularly preferred are esters of ricinoleic acid with polyfunctional alcohols, e.g., glycerin. The use of mixtures of such bio-based acids with other carboxylic acids, e.g., phthalic acids, is also preferred.

[0058] Examples of suitable diols are ethylene glycol, butylene glycol, diethylene glycol, triethylene glycol, polyalkylene glycols such as polyethylene glycol, and also 1,2-propanediol, 1,3-propanediol, 1,3-butanediol, 1,4-butanediol, 1,6-hexanediol and isomers, neopentyl glycol, or neopentyl glycol hydroxypivalate. Preference is given to using ethylene glycol, diethylene glycol, 1,4-butanediol, 1,5-pentanediol, 1,6-hexanediol, or mixtures of at least two of the diols mentioned, in particular mixtures of 1,4-butanediol, 1,5-pentanediol, and 1,6-hexanediol.

[0059] In addition, polyols such as trimethylolpropane, glycerol, erythritol, pentaerythritol, trimethylolbenzene or trishydroxyethyl isocyanurate can also be used, with glycerol and trimethylolpropane being preferred.

[0060] The polyether polyols which can be used as organic compounds having at least two hydroxyl groups are obtained by preparation methods known to the person skilled in the art, such as, for example, by anionic polymerization of one or more alkylene oxides having 2 to 4 carbon atoms with alkali hydroxides, such as sodium or potassium hydroxide, alkali alkoxides, such as sodium methylate, sodium or potassium ethylate or potassium isopropylate, or aminic alkoxylation catalysts, such as dimethylethanolamine (DMEA), imidazole and / or imidazole derivatives, or DMC catalysts using at least one starter molecule which contains 2 to 8, preferably 2 to 6, reactive hydrogen atoms bonded.

[0061] Suitable alkylene oxides include, for example, tetrahydrofuran, 1,3-propylene oxide, 1,2- or 2,3-butylene oxide, styrene oxide, and preferably ethylene oxide and 1,2-propylene oxide. The alkylene oxides can be used individually, alternately, or as mixtures. Preferred alkylene oxides are propylene oxide and ethylene oxide; copolymers of propylene oxide with ethylene oxide are particularly preferred. The alkylene oxides can be reacted in combination with CO2.

[0062] Examples of suitable starter molecules are: water, organic dicarboxylic acids such as succinic acid, adipic acid, phthalic acid and terephthalic acid, aliphatic and aromatic, optionally N-mono-, N,N- and N,N'-dialkyl-substituted diamines having 1 to 4 carbon atoms in the alkyl radical, such as optionally mono- and dialkyl-substituted ethylenediamine, diethylenetriamine, triethylenetetramine, 1,3-propylenediamine, 1,3- or 1,4-butylenediamine, 1,2-, 1,3-, 1,4-, 1,5- and 1,6-hexamethylenediamine, phenylenediamines, 2,3-, 2,4- and 2,6-tolylenediamine and 2,2'-, 2,4'- and 4,4'-diaminodiphenylmethane.

[0063] Preferably used are two or more polyhydric alcohols, such as ethanediol, 1,2- and 1,3-propanediol, diethylene glycol, dipropylene glycol, 1,4-butanediol, 1,6-hexanediol, paraformaldehyde, triethanolamine, bisphenols, glycerol, trimethylolpropane, pentaerythritol, sorbitol and sucrose.

[0064] Suitable polycarbonate polyols are polycarbonates containing hydroxyl groups, such as polycarbonatediols. These are formed by the reaction of carbonic acid derivatives, such as diphenyl carbonate, dimethyl carbonate, or phosgene, with polyols, preferably diols.

[0065] Examples of such diols are ethylene glycol, 1,2- and 1,3-propanediol, 1,3- and 1,4-butanediol, 1,6-hexanediol, 1,8-octanediol, neopentyl glycol, 1,4-bishydroxymethylcyclohexane, 2-methyl-1,3-propanediol, 2,2,4-trimethylpentanediol-1,3, dipropylene glycol, polypropylene glycols, dibutylene glycol, polybutylene glycols, bisphenols and lactone-modified diols of the type mentioned above. Instead of or in addition to pure polycarbonate diols, polyether polycarbonate diols can also be used, which are obtainable, for example, by copolymerization of alkylene oxides, such as propylene oxide, with CO2.

[0066] Polymer polyols, PHD polyols, and PIPA polyols can also be used as organic compounds with at least two hydroxyl groups as compounds containing hydrogen atoms reactive towards isocyanates. Polymer polyols are polyols that contain portions of solid polymers produced by radical polymerization of suitable monomers such as styrene or acrylonitrile in a base polyol. PHD (polyhydrazodicarbonamide) polyols are produced, for example, by in situ polymerization of an isocyanate or an isocyanate mixture with a diamine and / or hydrazine (or hydrazine hydrate) in a polyol, preferably a polyether polyol. The PHD dispersion is preferably produced by reacting an isocyanate mixture of 75 to 85% by weight of 2,4-tolylene diisocyanate (2,4-TDI) and 15 to 25% by weight of-% 2,6-toluene diisocyanate (2,6-TDI) with a diamine and / or hydrazine hydrate in a polyether polyol prepared by alkoxylation of a trifunctional starter (such as glycerol and / or trimethylolpropane). PIPA polyols are polyether polyols modified by polyisocyanate polyaddition with alkanolamines, with the polyether polyol preferably having a functionality of 2.5 to 4.0 and a hydroxyl number of 3 mg KOH / g to 112 mg KOH / g (molecular weight 500 g / mol to 18,000 g / mol).

[0067] Isocyanate-reactive substances with cell-opening effects can also be used, such as copolymers of ethylene oxide and propylene oxide with an excess of ethylene oxide or aromatic diamines such as diethyltoluenediamine.

[0068] For the production of polyurethane foams by the cold foam process, in a further embodiment, polyethers containing at least two hydroxyl groups and having an OH number of 20 to 50 mg KOH / g are used as an organic compound with at least two hydroxyl groups, wherein the OH groups consist of at least 80 mol% primary OH groups (determined by 1H NMR (e.g. Bruker DPX 400, deuterochloroform)). The OH number is particularly preferably 25 to 40 mg KOH / g, very particularly preferably 25 to 35 mg KOH / g. In addition to the previously defined structural unit of the formula (I), the polymeric, organic compound of the material can contain isocyanurate structural units of the formula where R represents a divalent hydrocarbon radical, especially a divalent aromatic hydrocarbon radical. Corresponding isocyanurate structural units are found, for example, to a large extent in rigid polyurethane foams.

[0069] The material containing the said polymeric organic compound is preferably a foam, more preferably a polyurethane foam. If the material is in the form of a polyurethane foam, it is preferably a flexible polyurethane foam or a rigid polyurethane foam.

[0070] If, according to formula (I), Xi and X2 represent a group O and Y1 and Y2 represent O, then the polymeric organic compound contains the carbonate linkage which is particularly preferred according to the invention.

[0071] Polymeric organic compounds of this embodiment suitable for the process according to the invention are, for example, aromatic polycarbonates and / or aromatic polyestercarbonates. These are known from the literature or can be prepared by processes known from the literature (for the preparation of aromatic polycarbonates, see, for example, Schnell, "Chemistry and Physics of Polycarbonates", Interscience Publishers, 1964, as well as DE-AS 1 495 626, DE-A 2 232 877, DE-A 2 703 376, DE-A 2 714 544, DE-A 3 000 610, DE-A 3 832 396; for the preparation of aromatic polyestercarbonates, see, for example, DE-A 3 007 934).

[0072] The aromatic polycarbonates usable as a corresponding polymeric organic compound are prepared, for example, by reacting compounds having at least two hydroxyl groups, in particular diphenols, with carbonic acid halides, preferably phosgene, and / or with aromatic dicarboxylic acid dihalides, preferably benzenedicarboxylic acid dihalides, by the interfacial process, optionally using chain terminators, for example monophenols, and optionally using trifunctional or more than trifunctional branching agents, for example triphenols or tetraphenols. Likewise, production via a melt polymerization process is possible by reacting compounds having at least two hydroxyl groups, in particular diphenols, with, for example, diphenyl carbonate.

[0073] According to the invention, such said materials can be used advantageously in which the polymeric, organic compound is at least one compound obtained by reacting at least the compounds (i) at least one aromatic compound having at least two hydroxyl groups, particularly preferably bisphenol A, and (ii) phosgene or diphenyl carbonate.

[0074] To prepare the polycarbonate-containing compound, it is preferred to use at least one aromatic compound having at least two hydroxyl groups, which is selected from the general formula (IV), wherein

[0075] A is a single bond, C1 to C5 alkylene, C2 to C5 alkylidene, C5 to C6 cycloalkylidene, - O-, -SO-, -CO-, -S-, -SO2-, C6 to C 12 -arylene, to which further aromatic rings, optionally containing heteroatoms, may be condensed, or a radical of the formula (V) or (VI)

[0076]

[0077] B each C1 to C 12 -Alkyl, preferably methyl, halogen, preferably chlorine and / or bromine x is each independently 0, 1 or 2, p is 1 or 0, and

[0078] R 5 and R 6 for each X 1 individually selectable, independently of one another, hydrogen or C1 to C6 alkyl, preferably hydrogen, methyl or ethyl,

[0079] X 1 Carbon and m is an integer from 4 to 7, preferably 4 or 5, with the proviso that at least one atom X 1 , R 5 and R 6 are simultaneously alkyl.

[0080] Preferred aromatic compounds having at least two hydroxyl groups are hydroquinone, resorcinol, dihydroxydiphenols, bis-(hydroxyphenyl)-C1-C5-alkanes, bis-(hydroxyphenyl)-C5-C6-cycloalkanes, bis-(hydroxyphenyl) ethers, bis-(hydroxyphenyl) sulfoxides, bis-(hydroxyphenyl) ketones, bis-(hydroxyphenyl) sulfones and oc,oc-bis-(hydroxyphenyl)-diisopropylbenzenes and their nuclear-brominated and / or nuclear-chlorinated derivatives.

[0081] Particularly preferred aromatic compounds having at least two hydroxyl groups are 4,4'-dihydroxydiphenyl, bisphenol-A, 2,4-bis(4-hydroxyphenyl)-2-methylbutane, 1,1-bis-(4-hydroxyphenyl)-cyclohexane, 1,1-bis-(4-hydroxyphenyl)-3,3,5-trimethylcyclohexane, 4,4'-

[0082] Dihydroxydiphenyl sulfide, 4,4'-dihydroxydiphenyl sulfone, and their di- and tetrabrominated or chlorinated derivatives, such as 2,2-bis(3-chloro-4-hydroxyphenyl)propane, 2,2-bis(3,5-dichloro-4-hydroxyphenyl)propane, or 2,2-bis(3,5-dibromo-4-hydroxyphenyl)propane. 2,2-bis(4-hydroxyphenyl)propane (bisphenol A) is particularly preferred. The aromatic compounds having at least two hydroxyl groups can be used individually or as any desired mixtures. The aromatic compounds having at least two hydroxyl groups are known from the literature or are obtainable by processes known from the literature.

[0083] In a further embodiment of the invention, usable thermoplastic, aromatic polycarbonates have average molecular weights (weight average M w, measured by GPC (gel permeation chromatography) with polycarbonate standard based on bisphenol A) of preferably 20,000 to 40,000 g / mol, more preferably 24,000 to 32,000 g / mol, particularly preferably 26,000 to 30,000 g / mol.

[0084] The thermoplastic, aromatic polycarbonates can be branched in a known manner, preferably by incorporating 0.05 to 2.0 mol%, based on the sum of the aromatic compound used having at least two hydroxyl groups, of trifunctional or more than trifunctional compounds, for example those having three or more phenolic groups.

[0085] Linear polycarbonates, more preferably based on bisphenol A, are preferably used.

[0086] Both homopolycarbonates and copolycarbonates are suitable as polymeric organic compounds. For the production of copolycarbonates preferably used according to the invention, 1 to 25 wt. %, preferably 2.5 to 25 wt. %, based on the total amount of aromatic compound containing at least two hydroxyl groups, of polydiorganosiloxanes with hydroxyaryloxy end groups can also be used. These are known (US Pat. No. 3,419,634) and can be prepared by processes known from the literature. Polydiorganosiloxane-containing copolycarbonates are also suitable; the production of polydiorganosiloxane-containing copolycarbonates is described, for example, in DE-A 3,334,782.

[0087] Aromatic dicarboxylic acid dihalides for the preparation of aromatic polyester carbonates are preferably the diacid dichlorides of isophthalic acid, terephthalic acid, diphenyl ether-4,4'-dicarboxylic acid and naphthalene-2,6-dicarboxylic acid.

[0088] The aromatic polyester carbonates can be either linear or branched in a known manner (see DE-A 2940024 and DE-A 3 007 934), with linear polyester carbonates being preferred. The partial oxidation of the material used is carried out in the reactor at a temperature of at least 400°C. Preferably, the partial oxidation of the material in the reactor is carried out at a temperature in a temperature range from 600°C to 1500°C, in particular from 850°C to 1400°C, more preferably from 1100°C to 1300°C.

[0089] In a preferred embodiment, the partial oxidation of the material used is carried out at an absolute pressure of more than 1 bar, preferably at an absolute pressure in a range from 2 to 80 bar, particularly preferably at an absolute pressure in a range from 2 to 50 bar.

[0090] The partial oxidation of the material can be carried out in at least one of the following three reactors: entrained flow gasification reactor, fluidized bed gasification reactor and fixed bed gasification reactor.

[0091] For use in an entrained flow gasification reactor, the polymeric organic compounds or the material containing them must be reduced to a grain size with an average particle diameter X 50.3of < 0.1 mm (dust). The feed into the reactor occurs either pneumatically or as a slurry. The major limitation of this type of partial oxidation for the chemical recycling of waste is the grindability and pumpability of feedstocks from heterogeneous waste. Thermal treatment of biomass (torrefaction) at 200–300 °C under the exclusion of oxygen is used to produce a "biochar" with grindability similar to that of hard coal. In another variant, upstream pyrolysis can be used to produce a pumpable pyrolysis oil. The oil obtained by waste pyrolysis can be partially oxidized either directly or in the form of a slurry mixed with the solid pyrolysis residue (pyrolysis coke). This process configuration was designed by Noel (Noell conversion process for the recycling and disposal of waste, Jürgen Carl EF-Verl. für Energie- und Umwelttechnik, 1994. ISBN: 3924511829).

[0092] Another option is the use of a fluidized bed gasification reactor. Waste gasification in fluidized bed reactors is widely known, using technologies such as EBARA (Showa Denko, Japan), ENERKEM (Enerkem, Edmonton, Canada), and the large-scale demonstration of high-temperature Winkler gas production (HTW) by Rheinbraun AG (now RWE) from 1993 to 1997 in Berrenrath, Germany. Pretreatment for feeding the polymeric, organic compounds, or the material containing them, into the reactor requires comminution to an average particle diameter X50.3 of 30-80 mm. Feeding into the reactor vessel is via screw conveyors, limiting the gasification pressure to a maximum of 10 bar. The ENERKEM and EBARA technologies enable the gasification of high-calorie waste (plastic waste or plastic-rich refuse-derived fuels).Fluidized bed gasifiers operate at mild temperatures of 700–950 °C, significantly below the ash melting point of the feedstock, to avoid caking and agglomeration in the reactor. Another advantage of this mild reactor temperature is the incomplete carbon conversion in the fluidized bed. Furthermore, the raw gas from fluidized bed gasifier reactors typically contains significant amounts of methane and other hydrocarbons. To compensate for this and ensure a high syngas yield of H2 and CO, the ENERKEM and EBARA processes utilize a second high-temperature partial oxidation stage (approx. 1400 °C), located directly downstream of the fluidized bed, to melt fly ash and convert hydrocarbons in the first-stage product gas into the final carbon monoxide-containing product gas stream. ENERKEM calls this second stage a "thermoreformer," while EBARA refers to it as a "high-temperature gasification furnace."The high temperature of this second partial oxidation stage increases CO2 production.

[0093] In a further embodiment of the process according to the invention, the partial oxidation of the material is preferably carried out in at least two steps, wherein in a first step a partial oxidation of the material is carried out in a first reactor at a temperature in a temperature range from 400 °C to 800 °C, the product gas from the first reactor is transferred to a second reactor and there, in a further step, with the addition of an oxygen-containing gas stream, is subjected to a partial oxidation at a temperature of more than 800 °C, preferably at a temperature in a range from 1300 °C to 1500 °C, to obtain the carbon monoxide-containing product gas stream.

[0094] Fixed-bed gasification is differentiated between dry ash and liquid slag discharging processes. The British Gas-Lurgi (BGL) process (British Gas / Lurgi slagging gasifier, published on: 1993-08-30) has been successfully applied for the co-gasification of up to 80% waste (derived solids, modernized municipal solid waste and industrial waste, shredder light fraction, mixed plastics waste, waste, and sewage sludge) with lignite and hard coal.

[0095] Pretreatment of waste intended for partial oxidation in fixed-bed gasifiers with slag requires granulation, compaction, or pressing. The waste feedstock is then introduced into the reactor via a lock system at the top of the reactor (gasifier). This allows the reactor to operate at pressures of up to 40 bar, reducing the compressor load for subsequent gas treatment and chemical synthesis. The tubes near the reactor floor heat the feedstock well above the ash melting point, forming a slag bath. Vitrified, nearly carbon-free slag (< 1 wt%) is discharged discontinuously into a water-filled chamber.The product gas moves upwards through the reactor (gasifier) ​​and passes through a post-gasification zone as a second step of partial oxidation, in which additional oxygen and preferably additional gaseous water (steam) is introduced to increase the temperature to 1000 - 1150 °C and convert methane and hydrocarbons before it leaves the reactor as a carbon monoxide-containing product gas stream.

[0096] The carbon monoxide-containing product gas from partial oxidation obtainable from the process according to the invention usually contains, in addition to carbon monoxide, portions of CO2, as well as water, hydrogen gas, and methane. Furthermore, particulate solids are dispersed in the carbon monoxide-containing product gas from partial oxidation obtainable from the process according to the invention.

[0097] The carbon monoxide-containing product gas stream is therefore subsequently fed to a purification step, in which the carbon monoxide-containing product gas stream is first fed to a washing step to separate solids, in which

[0098] (i) water is brought into contact with the carbon monoxide-containing product gas stream, whereby the particulate solid dispersed in the carbon monoxide-containing product gas stream forms a slag and this slag is removed and discharged,

[0099] (ii) the carbon monoxide-containing product gas stream, purified of particulate solids, is discharged. In the scrubbing step, the carbon monoxide-containing product gas extracted from the partial oxidation can initially be introduced into the scrubbing step at a temperature of more than 400°C. In this case, the product gas is cooled after contact with water, and the evaporating water, for example as condensate, is separated and optionally returned to the process.

[0100] The carbon monoxide-containing product gas stream discharged from the washing step, which has been purified from particulate solids, preferably has a temperature of at most 100°C, particularly preferably at most 80°C.

[0101] It has been found to be particularly preferred if the water is sprayed into the carbon monoxide-containing product gas stream during the washing step for contacting.

[0102] Carbon monoxide-containing product gas purified from particulate solids is, optionally after carrying out further optional purification steps different from step c1) to c5), next fed to at least one water separation in a drying step according to priority c2), water is separated off and the resulting carbon monoxide-containing product gas stream is discharged.

[0103] In a water separation unit, the carbon monoxide-containing product gas taken from the partial oxidation is cooled to separate the water and the water is separated, for example as condensate.

[0104] The separated water can be fed to the washing step cl).

[0105] A carbon monoxide-containing product gas stream purified by water separation is, optionally after performing further optional purification steps different from steps c1) to c5), next fed to at least one carbon dioxide separation step according to priority c3), carbon dioxide is separated, and the resulting carbon monoxide-containing product gas stream and carbon dioxide are discharged. The discharged carbon dioxide can be released into the environment or, as described later, introduced into the partial oxidation process in addition to the oxygen-containing gas and utilized there.The separation of CO2 can be carried out as an “amine scrubbing”, whereby the carbon monoxide-containing product gas passes through the basically known scrubbing of the gas mixture according to the principle of chemisorption with amines, such as monoethanolamine (MEA), diethanolamine (DEA), methyldiethanolamine (MDEA) or diglycolamine (DGA), which achieves a high purity of the purified gas mixture in an absorption column.

[0106] In order to reduce the CCE footprint, it is particularly preferred in a further embodiment of the present invention if the separated carbon dioxide discharged in step c3) is recycled to a partial oxidation reactor and introduced into this reactor.

[0107] Preferably, in one embodiment of the aforementioned CO2 recycling, the carbon dioxide is added to the partial oxidation in an amount of at most 1 kg per kg of polymeric, organic compound, preferably of at most 0.9 kg per kg of polymeric, organic compound, particularly preferably of 0.8 kg per kg of polymeric, organic compound.

[0108] If the partial oxidation of the material is carried out in at least two reactors, the separated carbon dioxide discharged in step c3) is recycled at least to the first reactor of the partial oxidation and introduced into this reactor.

[0109] Although CO2 recycling is particularly preferred, CO2 for partial oxidation can also be supplied from another CO2 source, for example, the CO2 emitted from the combustion chamber of a heating element during the provision of thermal energy, or CO2 from an external CO2 source. This can also be done in addition to the aforementioned CO2 recycling.

[0110] As a further CO2 source, preferably at least one external CO2 source serves which contributes CO2 which is not emitted by the process according to the invention. An external CO2 source would be, for example, the CO2 which arises during cement production, during H2 production for ammonia synthesis, during the combustion of fuels (e.g. waste incineration), or CO2 which is obtained from the air. In a preferred embodiment of the process according to the invention, this CO2 from an external CO2 source is obtained by absorbing a CO2 portion from (i) process gases or exhaust gases which are selected from at least one process selected from cement production, H2 production, or combustion and / or (ii) from air by introducing it into alkali lye, for example potassium lye. This forms potassium bicarbonate, which can then be thermally decomposed back into CO2 and potassium lye.The CO2 released in this process is then subjected to partial oxidation to synthesize carbon monoxide. The heat energy generated from the partial oxidation can be used, for example, to provide the heat energy required for CO2 release.

[0111] Optionally, further purification steps of the CO2 can be carried out to produce sufficient purity of the CO2 for the aforementioned partial oxidation.

[0112] A carbon monoxide-containing product gas stream purified by separation of carbon dioxide is, optionally after carrying out further optional purification steps different from step c1) to c5), next fed according to priority to at least one separation unit for the separation of carbon monoxide c4), a separation of carbon monoxide is carried out and the resulting carbon monoxide and a hydrogen gas-containing residual gas are discharged.

[0113] This preferably produces at least one gas stream which, at 25°C and 1013 mbar, contains at least 95 vol.% carbon monoxide, more preferably at least 99 vol.% carbon monoxide, and which is discharged as carbon monoxide. The said product gas stream, which has been purified of carbon dioxide and contains carbon monoxide, is preferably first separated into two gas streams in the separation unit for separating carbon monoxide (hereinafter also referred to as the H2-CO separation unit). This produces a gas in the form of a gas stream which contains at least 95 vol.% (preferably at least 99 wt.%) carbon monoxide, and a further gas in the form of a gas stream whose largest constituent is hydrogen and which contains, among other things, carbon monoxide and methane. The further gas is also referred to as the residual gas from the H2-CO separation or, if no residual gas treatment takes place, as the tail gas. An H2-CO separation unit which operates according to this separation principle is the so-called cold box.

[0114] The hydrogen-containing residual gas from the H2-CO separation can be subjected to subsequent residual gas treatment to concentrate the hydrogen. A hydrogen-containing residual gas separated by the carbon monoxide separation unit is fed to a residual gas treatment unit, hydrogen gas is separated, and hydrogen gas and a tail gas are discharged. After processing by the residual gas treatment, a hydrogen-enriched gas is obtained in the form of a gas stream, and another gas—the so-called residual gas from the residual gas treatment or tail gas—is obtained in the form of a gas stream. This gas contains a mixture of CO, methane, and a smaller amount of hydrogen than the hydrogen-enriched gas.

[0115] The hydrogen gas separated from the carbon monoxide separation in the process according to the invention can be used for the hydrogenation of nitro compounds to produce amines as a raw material for isocyanate synthesis. In a preferred embodiment of the process, after the separation of hydrogen in the H2-CO separation, in particular using a cold box, the separated gaseous hydrogen from the residual gas of the H2-CO separation is fed, after further residual gas treatment, as the resulting hydrogen into a hydrogenation of an organic nitro compound to produce organic amine as a raw material for organic isocyanate.

[0116] As mentioned, in a preferred embodiment of the process, phosgene synthesis is additionally carried out in step d) by reacting at least chlorine gas and carbon monoxide, with at least the carbon monoxide from purification step c) being reacted as carbon monoxide and phosgene being extracted. In particular, said purification is preferably carried out according to an embodiment suitable for a high degree of purity, and the remaining carbon monoxide from the purification is fed into the phosgene synthesis.

[0117] For the provision of chlorine for the phosgene synthesis carried out in this embodiment, the production of chlorine gas from electrochemical oxidation after hydrochloric acid electrolysis with a gas diffusion electrode (also referred to as the HCl ODC electrolysis process (ODC stands for oxygen depleting electrode, the so-called ODC (oxygen depleting cathode) is used as an ODC, for example); suitable electrolysis cells cf. US, 6022, 634 A, WO 03 / 31690 A1), the production of chlorine gas from hydrochloric acid diaphragm electrolysis (cf. EP 1 103 636 A1), the production of chlorine gas from thermocatalytic gas phase oxidation (cf. WO 2012 / 025483 A2), and the production of chlorine from chlor-alkali electrolysis (cf. WO 2009 / 007366 A2) are sufficiently known to the person skilled in the art. The contents of the aforementioned documents cited in connection with the production of chlorine gas are expressly and fully referred to.In a preferred variant of this embodiment of the process, the chlorine required for the synthesis of phosgene is produced electrolytically, in particular by electrochemical oxidation after hydrochloric acid electrolysis with a gas diffusion electrode, by electrochemical oxidation after hydrochloric acid diaphragm electrolysis, or by electrochemical oxidation after chlor-alkali electrolysis. It is particularly preferred if said electrochemical oxidation is carried out using electricity generated from renewable energy, in particular from renewable energy in the form of wind power, solar energy, or hydropower.

[0118] In a particularly preferred embodiment of the process, the phosgene formed by the phosgene synthesis is used in a further step e) to produce organic isocyanate (9), in which the phosgene (8a) from the phosgene synthesis (8) is reacted with at least one organic amino compound (20a), and at least organic isocyanate (9a) is extracted. Preferably, at least organic isocyanate and hydrogen chloride are extracted.

[0119] In general, those processes according to the invention of this embodiment are preferred in which the organic isocyanate obtained contains at least two isocyanate groups. For this purpose, an organic amine having at least two amino groups is again preferably used as the reactant in the synthesis.

[0120] Particularly preferably, the organic isocyanate obtained contains at least two isocyanate groups and has a molecular weight of at most 1000 g / mol, in particular of at most 800 g / mol.

[0121] Organic amines which are particularly preferably used are selected from tolylenediamine (TDA), methylenedi(phenylamine) (MDA) (in turn preferably selected from diphenylmethane-2,2'-diamine, diphenylmethane-2,4'-diamine, diphenylmethane-4,4'-diamine or mixtures thereof), hexamethylenediamine, isophoronediamine, 1,3-bis(aminomethyl)benzene, cyclohexyldiamine or mixtures thereof, with TDA, MDA or mixtures thereof being very particularly preferred organic isocyanates.

[0122] Very particularly preferably obtained organic isocyanates are selected from tolylene diisocyanate (TDI), methylene di(phenyl isocyanate) (MDI) (in turn preferably selected from diphenylmethane 2,2'-diisocyanate, diphenylmethane 2,4'-diisocyanate, diphenylmethane 4,4'-diisocyanate or mixtures thereof), hexamethylene diisocyanate (HDI), isophorone diisocyanate (IPDI), 1,3-bis(isocyanatomethyl)benzene (XDI), cyclohexyl diisocyanate (CHDI) or mixtures thereof, where TDI, MDI or mixtures thereof are very particularly preferred organic isocyanates.

[0123] Furthermore, in the embodiment involving the synthesis of organic isocyanate, hydrogen chloride is preferably also produced in addition to said organic isocyanate. It is again preferable to feed this hydrogen chloride as a reactant for the production of chlorine for the said phosgene synthesis. The necessary separation and purification of the hydrogen chloride formed in the isocyanate production can subsequently be carried out by an oxidative conversion in a thermocatalytic gas-phase oxidation with oxygen to form chlorine and water, optionally using O2 from water electrolysis.

[0124] Another alternative approach to utilizing hydrogen chloride as a starting material for chlorine production is the reaction of hydrogen chloride with water to form hydrochloric acid, followed by electrochemical oxidation of the hydrochloric acid to chlorine and, if necessary, hydrogen. This aqueous hydrochloric acid is used, in particular, for the previously described electrochemical oxidation after hydrochloric acid electrolysis with a gas diffusion electrode, the electrochemical oxidation after hydrochloric acid diaphragm electrolysis, or the electrochemical oxidation after chlor-alkali electrolysis. In the case of hydrochloric acid electrolysis with a gas diffusion electrode, the O2 required can be obtained from water electrolysis.

[0125] The hydrogen chloride produced during isocyanate production can also be converted into hydrochloric acid after purification and absorption in water, and the resulting hydrochloric acid can be sold on the market for various applications.

[0126] Within the scope of a particularly preferred embodiment of the process, a phosgene synthesis is additionally carried out by reacting at least chlorine gas and the carbon monoxide previously obtained after purifying the said carbon monoxide-containing product gas from step c); an isocyanate production by reacting the resulting phosgene with at least one organic amine to form at least one organic isocyanate compound and hydrogen chloride; a separation and purification of the hydrogen chloride formed in the isocyanate production and a subsequent oxidative conversion of the hydrogen chloride, selected from - a conversion of hydrogen chloride in a thermocatalytic gas phase oxidation with oxygen to chlorine and water, optionally using oxygen from water electrolysis, - a conversion of hydrogen chloride with water to hydrochloric acid and subsequent electrochemical oxidation of the hydrochloric acid to chlorine and optionally hydrogen;a subsequent addition of the chlorine formed to the said synthesis of phosgene following the oxidative conversion of the hydrogen chloride, optionally with the addition of an additional quantity of chlorine to the said synthesis of phosgene originating from a chlor-alkali electrolysis;

[0127] For all embodiments of the process which include a phosgene synthesis as a step, it is further preferred to carry out an electrochemical oxidation (electrolysis) for the chlorine production using electric power generated from renewable energy, in particular electric power optionally obtained by using wind power, solar energy or hydropower.

[0128] The organic amines used in the embodiment of the process for isocyanate production are in turn preferably provided by an additional step of hydrogenating organic nitro compounds with gaseous hydrogen. The hydrogen used here preferably originates from water electrolysis and / or from the purification of the carbon monoxide-containing product gas as separated hydrogen after the carbon monoxide separation step c4) and the residual gas treatment c5).

[0129] In a particularly preferred embodiment of the process according to the invention, hydrogen from water electrolysis is fed into the hydrogenation of an organic nitro compound for the production of an organic amine. Particularly preferably, the hydrogen is formed by water electrolysis using electric current from renewable energy (in particular from renewable energy in the form of wind power, solar energy, or hydropower) and fed to a step for the hydrogenation of at least one organic nitro compound, wherein the at least one organic amine obtained in the hydrogenation of said nitro compound is reacted with phosgene to obtain at least one organic isocyanate.

[0130] According to the invention, it is particularly preferred to feed at least the hydrogen separated from the carbon monoxide-containing product gas during the purification step to a hydrogenation step of at least one organic nitro compound. This also makes at least one organic amine available for the production of organic isocyanate.

[0131] The resulting organic isocyanates can be reacted in an additional step of the process with at least one organic compound having at least two hydroxyl groups, in particular at least one polyester polyol or polyether polyol, to form polyurethane materials. Preferred for the preparation of polyurethane material are those embodiments described above to characterize the preferred polymeric organic compound of the material used in the partial oxidation.

[0132] Polyurethane materials produced in this way are components of commercial products, for example, in the form of foams, paints, and insulating compounds. At the end of their life cycle, they can serve as material for the partial oxidation of the process according to the invention.

[0133] The present invention further relates to a device with which, in particular, the process according to the invention can be carried out. This is a device for providing carbon monoxide for the production of phosgene, preferably for the production of phosgene for the synthesis of organic isocyanate compounds, comprising at least one metering device for feeding material, at least one device for partial oxidation, and at least one purification device for carbon monoxide-containing product gas, characterized in that i) said device for partial oxidation contains at least one outlet for a carbon monoxide-containing product gas stream and at least one reactor for the partial oxidation of the material with at least one control device suitable for setting the temperature of the reactor to a temperature of at least 400°C,wherein the reactor contains at least one inlet for an oxygen-containing gas stream and at least one inlet for material and at least one different outlet for product gas, wherein the inlet for an oxygen-containing gas stream is in fluid communication with a source of an oxygen-containing gas stream containing at least 50 wt.% oxygen gas, and the outlet for product gas of the reactor is in fluid communication with the outlet for the carbon monoxide-containing product gas stream, optionally at least via at least one intermediate reactor for partial oxidation of the product gas; and, ii) the metering device and said device for partial oxidation are arranged and configured in such a way that the metering device is in fluid communication with the inlet for material of the reactor for the partial oxidation of the material via at least one feed line; and iii) a purification device for carbon monoxide-containing product gas,which contains at least one outlet for carbon monoxide and at least one inlet for the carbon monoxide-containing product gas stream, wherein this inlet is in fluid communication with the outlet for the carbon monoxide-containing product gas stream of the partial oxidation device, wherein the purification device is designed such that the carbon monoxide-containing product gas stream can be passed through the following modules for purification in the specified order: iii-1) at least one gas scrubbing device, containing at least one inlet for the carbon monoxide-containing product gas stream, at least one inlet for water, at least one scrubbing vessel in which water and carbon monoxide-containing product gas stream are combined, as well as at least one outlet for the carbon monoxide-containing product gas stream and at least one outlet for slag,wherein the washing vessel and the outlet for slag are in fluid communication, and the washing vessel and the outlet for the carbon monoxide-containing product gas stream are in fluid communication; iii-2) at least one drying device, comprising at least one inlet for the carbon monoxide-containing product gas stream, at least one cooling device suitable for cooling the carbon monoxide-containing product gas stream, at least one outlet for the carbon monoxide-containing product gas stream, and at least one outlet for liquid condensate, iii-3) at least one device for separating carbon dioxide, comprising at least one inlet for the carbon monoxide-containing product gas stream, at least one outlet for the carbon monoxide-containing product gas stream, and additionally at least one outlet for carbon dioxide, iii-4) at least one separation unit for separating carbon monoxide, comprising at least one inlet for the carbon monoxide-containing product gas stream,at least one outlet for carbon monoxide and additionally at least one outlet for residual gas containing hydrogen gas.,

[0134] According to the invention, a "fluid connection" is understood to mean a device part that connects plant parts to one another and through which a substance, which can be present in any aggregate state, can be transported from one plant part to another through a material flow, for example a feed line in the form of a pipe, which can be interrupted by other plant parts, or a feed line in the form of a conveying device, such as a chute, a screw conveyor, or a conveyor belt for solids. The reactors of the device for partial oxidation are preferably selected from at least one reactor from the group consisting of reactors for entrained flow gasification, reactors for fluidized bed gasification, and reactors for fixed bed gasification.

[0135] The source of an oxygen-containing gas stream containing at least 50% by weight of oxygen gas is preferably a water electrolysis device, the oxygen gas outlet of which is in fluid communication with the oxygen-containing gas stream inlet located on the reactor. Analogously to the method described above, within the scope of a preferred embodiment of the device, it is also preferred if the device according to the invention additionally contains a water electrolysis device which, in addition to at least one anode and at least one cathode, additionally has at least one water inlet, at least one hydrogen gas outlet, and at least one oxygen gas outlet, and is connected to a source of electrical power from renewable energy, and the hydrogen gas outlet of which is in fluid communication with a hydrogen gas inlet of a device for hydrogenating organic nitro compounds.

[0136] The preferred embodiments of the gas washing device, the drying device, the device for separating carbon dioxide and the separation unit for separating carbon monoxide are designed as described under the subject matter of the process according to the invention (vide supra).

[0137] It has proven to be preferred if, within the scope of a preferred embodiment, the device is characterized in that the purification device additionally contains at least one device for residual gas treatment, containing at least one inlet for hydrogen-containing residual gas, at least one outlet for hydrogen gas and at least one outlet for tail gas, wherein the inlet for hydrogen-containing residual gas is in fluid connection with the outlet for hydrogen-containing residual gas of the separation unit for separating carbon monoxide.

[0138] A particularly preferred embodiment of the device is suitable for recirculating CO2 separated in the carbon dioxide separation device into a partial oxidation reactor. Therefore, a particularly preferred embodiment of the device is characterized in that at least one reactor of the partial oxidation device has a carbon dioxide inlet that is fluidly connected to the carbon dioxide outlet of the carbon dioxide separation device, thereby enabling recirculation of the carbon dioxide into this reactor of the partial oxidation device against the flow direction of the carbon monoxide-containing product gas stream.

[0139] Conducting the process with at least two stages of partial oxidation has proven to be preferred. A suitable embodiment of the device is one in which said device for partial oxidation has at least one outlet for a carbon monoxide-containing product gas stream and a first reactor for the partial oxidation of the material with at least one heating element suitable for controlling the temperature of the reactor to a temperature of at least 400°C, wherein the first reactor has at least one inlet for an oxygen-containing gas stream and at least one inlet for material and at least one different outlet for product gas, wherein the inlet for an oxygen-containing gas stream is in fluid communication with a source of an oxygen-containing gas stream having at least 50% by weight.-% oxygen gas; and a second reactor for the partial oxidation of the product gas with at least one heating element which is suitable for tempering the reactor to a temperature of more than 800°C, wherein the second reactor contains at least one inlet for an oxygen-containing gas stream and at least one inlet for optionally intermediately treated product gas of the first reactor and at least one different outlet for product gas, wherein the outlet for product gas of the first reactor is in fluid communication with the inlet of the second reactor for optionally intermediately treated product gas of the first reactor, and the inlet for an oxygen-containing gas stream is in fluid communication with a source of an oxygen-containing gas stream with at least 50 wt.% oxygen gas, and the outlet for product gas of the second reactor is in fluid communication with the outlet for the carbon monoxide-containing product gas stream.

[0140] Preferably, a reactor is designed such that, in addition to the oxygen-containing gas stream, gaseous water can also be introduced into the reactor. Such reactors are characterized in that at least one reactor is in fluid communication with at least one source of gaseous water.

[0141] Furthermore, an embodiment of the device is preferred in which the carbon monoxide outlet of the carbon monoxide separation unit is in fluid communication with the inlet of a reactor of a phosgene synthesis device. The phosgene synthesis device contains at least one inlet for chlorine gas, at least one inlet for carbon monoxide, and at least one outlet for phosgene.

[0142] For the synthesis of organic isocyanate, it is advantageous in a preferred embodiment of the device if the phosgene outlet of the device for phosgene synthesis is in fluid communication with a device for producing organic isocyanate, wherein the device for producing organic isocyanate, in addition to at least one inlet for phosgene, additionally has at least one inlet for organic amine and at least one outlet for organic isocyanate. It is particularly preferred if the device for producing organic isocyanate is in fluid communication with a device for hydrogenating organic nitro compounds via at least one inlet for organic amine, wherein the device for hydrogenating organic nitro compounds has at least one inlet for hydrogen gas, at least one inlet for organic nitro compounds, and at least one outlet for organic amine.The hydrogen gas from the residual gas treatment of the residual gas from the H2-CO separation device can advantageously serve as the source of the hydrogen gas for hydrogenation. For this purpose, the hydrogen gas outlet of the residual gas treatment device and the hydrogen gas inlet of the device for hydrogenating organic nitro compounds are preferably fluidly connected. In addition or in addition to this, the hydrogen gas from the device for producing chlorine particularly preferably serves as the source of the hydrogen gas for hydrogenation. For this purpose, the hydrogen gas outlet of the device for producing chlorine and the hydrogen gas inlet of the device for hydrogenating organic nitro compounds are particularly preferably fluidly connected.

[0143] To utilize the hydrogen gas from the residual gas of the H2-CO separation device for synthesis purposes, it is preferred if the outlet for the residual gas of the H2-CO separation device is fluidly connected to the inlet of a residual gas treatment device, wherein said residual gas treatment device has at least one outlet for hydrogen gas and at least one outlet for residual gas from the residual gas treatment. In this case, it is preferred if the outlet for the residual gas of the residual gas treatment device is fluidly connected to the heating element of the reformer, in particular to the combustion chamber of the heating element.

[0144] The invention further relates to the use of a partial oxidation of material containing at least one polymeric organic compound to provide carbon monoxide for the synthesis of phosgene. It is preferred if the partial oxidation of the material is carried out according to a process of the first subject matter of the invention.

[0145] The invention further relates to the use of material containing at least one polymeric organic compound in a partial oxidation of the material to provide carbon monoxide for the synthesis of phosgene. It is preferred if the partial oxidation of the material is carried out according to a process of the first subject matter of the invention.

[0146] The invention is explained in more detail below with reference to Figures 1 and 2. In the figures, the following reference numerals have the meanings shown on the right:

[0147] 1 Material pretreatment la processed material containing polyurethane as a polymeric, organic compound

[0148] 1b processed material containing polycarbonate as a polymeric, organic

[0149] Connection

[0150] 2 partial oxidation (gasification)

[0151] 2a Reactor for partial oxidation

[0152] 2b Reactor for partial oxidation of the product gas from 2a

[0153] 2c Product gas

[0154] 2d Product gas stream containing CO and H2 and particulate solid

[0155] 3 washing steps

[0156] 3a Product gas stream containing CO and H2 and scrubbed

[0157] 3 b slag

[0158] 4 Drying by H2O removal

[0159] 4a Product gas stream containing CO and H2 and dried

[0160] 4b Water

[0161] 5 Separation of carbon dioxide

[0162] 5a Product gas stream from CO2 removal containing CO and H2

[0163] 5b CO2

[0164] 6 Separation of carbon monoxide (H2-CO separation)

[0165] 6a Residual gas

[0166] 6b CO

[0167] 7 H2 cleaning

[0168] 7a H2

[0169] 7b Tail gas

[0170] 8 Phosgene synthesis

[0171] 8a Phosgen

[0172] 9 Isocyanate production

[0173] 9a organic isocyanate

[0174] 10 Polyurethane production 10a organic compound with at least 2 hydroxy groups, e.g. polyether polyol or polyester polyol

[0175] 11 Polyurethane end of life - collection / separation

[0176] 11a Material containing polyurethane

[0177] 20 Hydrogenation of organic nitro compounds

[0178] 20a organic diamino compound

[0179] 20b organic compound

[0180] 21 organic nitro compound

[0181] 22 Water electrolysis

[0182] 22a Hydrogen

[0183] 22b Oxygen

[0184] 30 H2O for partial oxidation (gasification) 2

[0185] 100 Polycarbonate production

[0186] 101 Polycarbonate

[0187] 110 Polycarbonate-containing material end of life - Collection / Separation

[0188] 110a polycarbonate containing material

[0189] 200 Chlor-alkali electrolysis

[0190] 200a sodium hydroxide solution

[0191] 200b Sodium chloride-containing wastewater from 100

[0192] 200c sodium chloride (NaCl)

[0193] 200d chlorine gas

[0194] Arrows in the figures symbolize the flow of materials, energy, or heat between process steps or device components in which the corresponding process steps take place. Dashed arrows symbolize additional features of preferred embodiments of the process, which can preferably be used individually or in combination.

[0195] Fig.1 shows an embodiment of the process for the production of carbon monoxide by gasification of a polyurethane waste fraction using oxygen from a water electrolysis for the preparation of phosgene for the synthesis of organic isocyanate, comprising at least the steps a) providing an oxygen-containing gas stream 22b containing at least 50 wt.- % oxygen gas, b) partial oxidation 2 of material 1a containing at least one polymeric, organic compound, wherein said material 1a is introduced into a reactor 2a of a device and treated there at least by supplying said oxygen-containing gas stream 22b and heat at at least 400°C to form a product gas 2c, and the resulting product gas 2c, optionally after at least one further partial oxidation step 2b of the product gas 2c, is discharged from the device as a carbon monoxide-containing product gas stream 2d together with particulate solid dispersed therein; c) the carbon monoxide-containing product gas stream 2d is fed to a purification step in which at least c1) the carbon monoxide-containing product gas stream 2d is fed to a washing step 3 for the separation of solid, wherein.

[0196] (i) water is brought into contact with the carbon monoxide-containing product gas stream 2d, whereby the particulate solid dispersed in the carbon monoxide-containing product gas stream 2d forms a slag 3b and this slag 3b is removed and discharged,

[0197] (ii) the carbon monoxide-containing product gas stream 3a purified from particulate solids is discharged; c2) a carbon monoxide-containing product gas stream 3a purified from particulate solids by means of washing step 3 is fed to at least one water separation stage 4 in a drying step, water 4b is separated off, and the resulting carbon monoxide-containing product gas stream 4a is discharged; c3) a carbon monoxide-containing product gas stream 4a purified from water 4 is fed to at least one carbon dioxide separation stage 5, carbon dioxide is separated off, and the resulting carbon monoxide-containing product gas stream 5a and carbon dioxide 5b are discharged, wherein the carbon dioxide 5b is at least partially introduced into a partial oxidation reactor 2;c4) a carbon monoxide-containing product gas stream 5a purified by means of carbon dioxide removal is fed to at least one separation unit 6 for the separation of carbon monoxide, a separation of carbon monoxide is carried out, and the resulting carbon monoxide 6b and a hydrogen gas-containing residual gas 6a are discharged; c5) optionally, a hydrogen gas-containing residual gas 6a separated by means of said separation unit 6 is fed to a residual gas treatment 7, hydrogen gas 7a is separated, and hydrogen gas 7a and tail gas 7b are discharged; d) phosgene synthesis 8 by reacting at least chlorine gas and carbon monoxide, wherein at least the carbon monoxide 6b from the purification of step c) is reacted as carbon monoxide and phosgene 8a is discharged.

[0198] The integration of this process into an isocyanate production process is described as an example in the examples section.

[0199] Fig. 2 shows an embodiment of the process for producing carbon monoxide by gasifying a polycarbonate waste fraction using oxygen from water electrolysis to produce phosgene for the synthesis of polycarbonate. This process includes at least the steps described in Fig. 1 except for step d).

[0200] The integration of this process into polycarbonate production is described as an example in the examples section.

[0201] The following aspects 1 to 25 represent a further embodiment of the invention, wherein the reference numerals in brackets are merely clarifying and do not limit the embodiment to the subject matter of Figure 1:

[0202] 1. A process for providing carbon monoxide for the production of phosgene, preferably for the production of phosgene for the synthesis of organic isocyanate compounds, comprising at least the following steps a) providing an oxygen-containing gas stream (22b) containing at least 50 wt.-% oxygen gas, b) partial oxidation (2) of material (1a) containing at least one polymeric, organic compound, wherein said material (1a) is introduced into a reactor (2a) of a device and treated there at least by supplying said oxygen-containing gas stream (2b) and heat at at least 400°C to form a product gas (2c), and the resulting product gas (2c), optionally after at least one further partial oxidation step (2b) of the product gas (2c), is discharged from the device as a carbon monoxide-containing product gas stream (2d) together with particulate solid dispersed therein; c) the carbon monoxide-containing product gas stream (2d) is fed to a purification step in which at least c1) the carbon monoxide-containing product gas stream (2d) is fed to a washing step (3) to separate off solid, wherein.

[0203] (i) water is brought into contact with the carbon monoxide-containing product gas stream (2d), whereby the particulate solid dispersed in the carbon monoxide-containing product gas stream (2d) forms a slag (3b) and this slag (3b) is removed and discharged,

[0204] (ii) the carbon monoxide-containing product gas stream (3a) purified from particulate solids is discharged; c2) a carbon monoxide-containing product gas stream (3a) purified from particulate solids by means of a washing step (3) is fed to at least one water separation unit (4) in a drying step, water (4b) is separated off, and the resulting carbon monoxide-containing product gas stream (4a) is discharged; c3) a carbon monoxide-containing product gas stream (4a) purified by means of separation of water (4) is fed to at least one carbon dioxide separation unit (5), carbon dioxide is separated off, and the resulting carbon monoxide-containing product gas stream (5a) and carbon dioxide (5b) are discharged; c4) a carbon monoxide-containing product gas stream (5a) purified by means of separation of carbon dioxide is fed to at least one separation unit (6) for separating carbon monoxide,a separation of carbon monoxide is carried out, and the resulting carbon monoxide (6b) and a hydrogen gas-containing residual gas (6a) are discharged; c5) optionally, a hydrogen gas-containing residual gas (6a) separated by means of said separation unit (6) is fed to a residual gas treatment (7), hydrogen gas (7a) is separated, and hydrogen gas (7a) and end gas (7b) are discharged; d) optionally, phosgene synthesis (8) by reacting at least chlorine gas and carbon monoxide, wherein at least the carbon monoxide (6b) from the purification of step c) is reacted as carbon monoxide, and phosgene (8a) is discharged. Process according to aspect 1, characterized in thatthat, to provide the oxygen-containing gas stream (22b), an electrolysis of water (22) is carried out to obtain oxygen gas (22a) and hydrogen gas, and the oxygen gas (22a) from this electrolysis (22) is used to provide the oxygen-containing gas stream (22b). Method according to one of aspects 1 or 2, characterized in that gaseous water is additionally supplied to the reactor (2a) in a weight ratio of gaseous water to oxygen gas of the oxygen-containing gas stream of at least 0.2. Method according to one of the preceding aspects, characterized in that the partial oxidation (2) is carried out at an absolute pressure of more than 1 bar, preferably at an absolute pressure in a range from 2 to 80 bar, particularly preferably at an absolute pressure in a range from 2 to 50 bar. Method according to one of the preceding aspects, characterized inthat the total amount of all polymeric, organic compounds contained in the material (Ia) is at least 50 wt. %, preferably at least 60 wt. %, particularly preferably at least 75 wt. %. . Process according to one of the preceding aspects, characterized in that the total amount of all polymeric, organic compounds contained in the material (Ia) has a carbon content of at least 40.0 wt. %, preferably at least 50 wt. %. Process according to one of the preceding aspects, characterized in that the weight ratio of the oxygen gas contained in the oxygen-containing gas stream (22b) to the polymeric, organic compound is introduced into the reactor (2a) within a weight ratio range of 0.4 to 1.0 to 1.2 to 1.0, preferably from 0.6 to 1.0 to 0.9 to 1.0. Process according to one of the preceding aspects, characterized in that the polymeric,The organic compound of the material (Ia) is selected from at least one homopolymeric or copolymeric compound from the group consisting of cellulose, polyester, polyamide, polyurethane (PUR), polyurea, polyisocyanurate (PIR), and polycarbonate, preferably from at least one homopolymeric or copolymeric compound from the group consisting of polyurethane (PUR), polyisocyanurate (PIR). The process according to one of the preceding aspects, characterized in that the structure of the polymeric, organic compound of the material (Ia) contains at least one repeating structural unit of the formula (I), where X 1 and X 2 independently of one another represent a direct bond, O or NH, preferably O or NH,

[0205] Y 1 and Y 2 independently represent O or NH,

[0206] R 1 and R 2independently of one another, each represent any bivalent, carbon-containing structural element, and a covalent bond marked with * represents a bond to the remaining molecule of the polymeric, organic compound. Process according to aspect 7, characterized in that the total amount of the polymeric, organic compounds containing at least one repeating structural unit of the formula (I) in the material (Ia) is at least 50 wt. %, preferably at least 60 wt. %, particularly preferably at least 75 wt. %. Process according to one of the preceding aspects, characterized in that the partial oxidation of the material (Ia) in the reactor (2a) is carried out at a temperature in a temperature range from 600°C to 1500°C, in particular from 850°C to 1400°C, more preferably from 1100°C to 1300°C. Process according to one of the preceding aspects, characterized inthat the water is sprayed into the carbon monoxide-containing product gas stream (2c) during the washing step (3). A process according to one of the preceding aspects, characterized in that the carbon monoxide-containing product gas stream (3a) discharged from the washing step (3) and purified from particulate solids has a temperature of at most 100°C, preferably at most 80°C. A process according to one of the preceding aspects, characterized in that the partial oxidation (2) of the material (1a) is carried out in at least two steps, wherein, in a first step, a partial oxidation of the material (1a) is carried out in a first reactor (2a) with the addition of an oxygen-containing gas stream (22b) at a temperature in a temperature range from 400°C to 800°C.the product gas (2c) of the first reactor is transferred to a second reactor (2b) and there, in a further step, is subjected to partial oxidation at a temperature of more than 800°C, preferably at a temperature in a range from 1300°C to 1500°C, with the addition of an oxygen-containing gas stream (22b), to obtain the carbon monoxide-containing product gas stream (2d). Process according to one of aspects 1 to 12, characterized in that the separated carbon dioxide (5b) discharged in step c3) is recycled to a partial oxidation reactor (2) and introduced into this reactor. Process according to aspect 13, characterized in that the partial oxidation (2) of the material (1a) is carried out according to claim 12 and that the carbon monoxide discharged in step c3)separated carbon dioxide (5b) is returned at least to the first reactor (2a) of the partial oxidation and introduced into this reactor. Process according to one of the preceding aspects, characterized in that the carbon dioxide (5b) is added to the partial oxidation (2) in an amount of at most 1 kg per kg of polymeric, organic compound, preferably of at most 0.9 kg per kg of polymeric, organic compound, particularly preferably of 0.8 kg per kg of polymeric, organic compound. Process according to one of the preceding aspects, characterized in that the phosgene synthesis (8) is carried out in step d) and additionally the following step: e) production of organic isocyanate (9), wherein the phosgene (8a) from the phosgene synthesis (8) is reacted with at least one organic amino compound (20a) and at least organic isocyanate (9a) is discharged. Device for providing carbon monoxide for the production of phosgene,preferably for the production of phosgene for the synthesis of organic isocyanate compounds, comprising at least one metering device for feeding in material, at least one device for partial oxidation and at least one purification device for carbon monoxide-containing product gas, characterized in that i) said device for partial oxidation contains at least one outlet for a carbon monoxide-containing product gas stream and at least one reactor for the partial oxidation of the material with at least one heating element which is suitable for tempering the reactor to a temperature of at least 400°C, wherein the reactor contains at least one inlet for an oxygen-containing gas stream and at least one inlet for material and at least one different outlet for product gas,wherein the inlet for an oxygen-containing gas stream is in fluid communication with a source of an oxygen-containing gas stream containing at least 50 wt.% oxygen gas, and the outlet for product gas of the reactor, optionally at least via at least one intermediate reactor for partial oxidation of the product gas, is in fluid communication with the outlet for the carbon monoxide-containing product gas stream; and, ii) the metering device and said device for partial oxidation are arranged and configured in such a way that the metering device is in fluid communication with the inlet for material of the reactor for the partial oxidation of the material via at least one feed line; and iii) a purification device for carbon monoxide-containing product gas, which contains at least one outlet for carbon monoxide and at least one inlet for the carbon monoxide-containing product gas stream,wherein this inlet is in fluid communication with the outlet for the carbon monoxide-containing product gas stream of the partial oxidation device, wherein the purification device is designed such that the carbon monoxide-containing product gas stream can be passed through the following modules for purification in the specified order iii-1) at least one gas scrubbing device, comprising at least one inlet for the carbon monoxide-containing product gas stream, at least one inlet for water, at least one scrubbing vessel in which water and carbon monoxide-containing product gas stream are combined, as well as at least one outlet for the carbon monoxide-containing product gas stream and at least one outlet for slag,wherein the washing vessel and the outlet for slag are in fluid communication, and the washing vessel and the outlet for the carbon monoxide-containing product gas stream are in fluid communication; iii-2) at least one drying device, comprising at least one inlet for the carbon monoxide-containing product gas stream, at least one cooling device suitable for cooling the carbon monoxide-containing product gas stream, at least one outlet for the carbon monoxide-containing product gas stream, and at least one outlet for liquid condensate, iii-3) at least one device for separating carbon dioxide, comprising at least one inlet for the carbon monoxide-containing product gas stream, at least one outlet for the carbon monoxide-containing product gas stream, and additionally at least one outlet for carbon dioxide, iii-4) at least one separation unit for separating carbon monoxide, comprising at least one inlet for the carbon monoxide-containing product gas stream,at least one outlet for carbon monoxide and additionally at least one outlet for hydrogen gas-containing residual gas. Device according to aspect 17, characterized in that the purification device additionally contains at least one device for residual gas treatment, containing at least one inlet for hydrogen-containing residual gas, at least one outlet for hydrogen gas, and at least one outlet for tail gas, wherein the inlet for hydrogen-containing residual gas is in fluid communication with the outlet for hydrogen-containing residual gas of the separation unit for separating carbon monoxide. 19. Device according to one of aspects 17 or 18, characterized in that at least one reactor of the device for partial oxidation has an inlet for carbon dioxide, which is in fluid communication with the outlet for carbon dioxide of the device for separating carbon dioxide.whereby a recirculation of the carbon dioxide into this reactor of the partial oxidation device is enabled, counter to the flow direction of the carbon monoxide-containing product gas stream. 20. Device according to one of aspects 17 to 19, characterized in that said partial oxidation device contains at least one outlet for a carbon monoxide-containing product gas stream and a first reactor for the partial oxidation of the material with at least one control system suitable for setting the temperature of the reactor to a temperature of at least 400°C, wherein the first reactor contains at least one inlet for an oxygen-containing gas stream and at least one inlet for material and at least one different outlet for product gas.wherein the inlet for an oxygen-containing gas stream is in fluid communication with a source of an oxygen-containing gas stream containing at least 50 wt.% oxygen gas; and a second reactor for the partial oxidation of the product gas with at least one heating element suitable for controlling the temperature of the reactor to a temperature of more than 800°C, wherein the second reactor contains at least one inlet for an oxygen-containing gas stream and at least one inlet for optionally intermediately treated product gas from the first reactor and at least one different product gas outlet, wherein the product gas outlet of the first reactor is in fluid communication with the second reactor inlet for optionally intermediately treated product gas from the first reactor, and the inlet for an oxygen-containing gas stream is in fluid communication with a source of an oxygen-containing gas stream containing at least 50 wt.% oxygen gas,and the product gas outlet of the second reactor is in fluid communication with the outlet for the carbon monoxide-containing product gas stream. Apparatus according to any one of aspects 17 to 20, characterized in that at least one reactor is in fluid communication with at least one source of gaseous water. 22. Apparatus according to any one of aspects 17 to 21, characterized in that the carbon monoxide outlet of the carbon monoxide separation unit is in fluid communication with the inlet of a reactor of a phosgene synthesis apparatus. 23. Use of a partial oxidation of material (2) containing at least one polymeric, organic compound to provide carbon monoxide for the synthesis of phosgene. 24. Use of material (2) containing at least one polymeric, organic compound,in a partial oxidation of the material to provide carbon monoxide for the synthesis of phosgene. 25. Use according to one of aspects 23 or 24, characterized in that the partial oxidation of the material is carried out according to a process according to one of aspects 1 to 16.

[0207] Examples

[0208] Example 1 - Process according to the invention - partial oxidation 2 of polyurethane-containing material (two reaction zones 2a and 2b) - without CO2 recirculation according to Fig.l

[0209] In a device for partial oxidation 2, 10.94 t / h of polyurethane-containing material 1a with a composition of 54.2 wt.% carbon, 8.78 wt.% hydrogen, 35.7 wt.% oxygen, 1.1 wt.% N2, and 0.5 wt.% non-combustible inorganic solids are introduced into a reactor 2a. The conversion of the polyurethane-containing material 1a takes place in reactor 2a at 950°C, resulting in a CO- and H2-containing product gas 2c, which is fed into a reactor 2b. In reactor 2b, the conversion of the gas mixture 2c introduced from 2a takes place at 1450°C.

[0210] Furthermore, 5.46 t / h of oxygen 22b from a water electrolysis 22 are fed to the partial oxidation 2.

[0211] The CO and H2-containing gas mixture 2d from zone 2b is contacted with water in a scrubbing step 3 and cooled to 60°C. This separates 0.049 t / h of slag 3b, 0.1 t / h of water, and 0.54 t / h of ash. A portion of the condensed water is purged and replaced with fresh water.

[0212] The washed product gas mixture 3a from the partial oxidation 2 is fed to a dryer 4.

[0213] The dried product gas mixture 4a is fed to an amine scrubber for CO2 separation 5, where 7.9 t / h of CO2 5b are separated. The product gas mixture 5a, largely free of CO2, is fed to a cold box for H2-CO separation 6, where the remaining CO2 is also separated. From the cold box, 6.28 t / h of CO 6b and 0.95 t / h of FE-containing residual gas 6a, along with small amounts of by-products including methane and nitrogen, are removed.

[0214] The CO 6b is fed to a phosgene synthesis 8, where it is converted with 15.92 t / h of CE to produce 22.2 t / h of phosgene 8a. The phosgene 8a is converted with 13.68 t / h of toluenediamine from an isocyanate synthesis 9 to produce 19.5 t / h of toluene diisocyanate 9a. This can be further processed with poly / polyesterols 10a to produce polyurethane materials.

[0215] After the polyurethane materials have been used in various applications, these end-of-life materials 110 are collected, separated, and processed to produce a material lb that can be fed into gasification 2. Thus, the CO group of the functional isocyanate group (-NCO) in the isocyanate can be sustainably produced and the carbon recycled, thus closing the value chain for this carbon.

[0216] The hydrogen-containing residual gas stream 6a separated from the cold box 6 is fed to a pressure swing adsorption unit 7 for hydrogen purification, from which 0.9 t / h of H2 is separated and fed to the hydrogenation of dinitrotoluene 20. Here, 20.4 t / h of dinitrotoluene 21 are reacted with the 0.9 t / h of H27a from the residual gas treatment 7 and a further 0.445 t / h of H2 from a water electrolysis 22 to produce 13.68 t / h of toluene diamine 20a.

[0217] The co-product hydrogen, which is used for the hydrogenation of the nitro compounds, can provide a large part of the required hydrogen, which then no longer needs to be produced via water electrolysis and thus also makes a sustainable contribution.

[0218] The oxygen 22b taken as a co-product from the water electrolysis 22 at 3.6 t / h is fed to the gasification 2 with additional oxygen of 1.86 t / h.

[0219] Example 2 Fig.1 - Process according to the invention - partial oxidation of polyurethane-containing material (two reaction zones 2a and 2b) with CO2 recirculation

[0220] 10.94 t / h of polyurethane-containing material 1a with an average composition of 54.2 wt.% carbon, 8.73 wt.% hydrogen, 35.5 wt.% oxygen, 1.1 wt.% N2, and 0.45 wt.% non-combustible inorganic solids are introduced into a device for partial oxidation 2. The conversion of the polyurethane-containing material 1a takes place in the device in a zone 2a with the addition of oxygen-containing gas 22b at 950°C, from which a CO- and H2-containing gas mixture is fed into a zone 22b. In zone 22b, the conversion of the product gas mixture 2c introduced from 2a takes place at 1450°C. Furthermore, 5.46 t / h of oxygen 22b from a water electrolysis unit 22 and 7.91 t / h of CO25b from the CO2 separation unit 5 are fed to the gasification device (2). The CO and H2-containing gas mixture 2d is cooled to 60°C in a washing step 3 by washing with water. In this step, 0.049 t / h of slag 3b, 0.1 t / h of water, and 0.54 t / h of ash are separated.A portion of the condensed water (3.23 t / h) is purged and 0.1 t / h of fresh water is added.

[0221] The product gas mixture 3a from the washing step 3 is fed to a dryer 4 after cooling.

[0222] The dried gas mixture 4a is fed to an amine scrubber for CO2 separation 5, where 7.91 t / h of CO2 5b are separated. The gas mixture, largely freed of CO2, is fed to a cold box for H2-CO separation 6, where the remaining CO2 is also separated. From the cold box, 11.31 t / h of CO 6b and 0.6 t / h of H2-containing residual gas 6a, along with small amounts of byproducts including methane and nitrogen, are removed. The CO 6b is fed to a phosgene synthesis 8, where it is reacted with 28.67 t / h of Cl2 to produce 39.98 t / h of phosgene 8a. Phosgene 8a is reacted with 24.63 t / h of toluenediamine 20a from an isocyanate synthesis 9 to yield 35.13 t / h of toluene diisocyanate 9a. This can be further processed with poly- / polyesterols 10a to produce polyurethane materials.After use of the polyurethane materials in various applications, they are collected as end-of-life material 11a, separated, and processed 1, resulting in a material 1a that can be subjected to partial oxidation 2. Thus, the CO group of the functional isocyanate group (-NCO) in the isocyanate can be sustainably produced and the carbon recycled, thus closing the value chain for this carbon.

[0223] The hydrogen-containing residual gas stream 6a separated from the cold box 6 is fed to a pressure swing adsorption unit 7 for residual gas purification, from which 0.55 t / h of H27a is separated, which is then fed to the hydrogenation of dinitrotoluene 20. In this process, 34.74 t / h of dinitrotoluene 21 are reacted with the 0.55 t / h of H27a from the hydrogen purification unit and a further 1.87 t / h of H2 from a water electrolysis 22 to produce 24.63 t / h of toluene-diamine 20a. The hydrogen by-product, which is used for the hydrogenation of the nitro compounds, can provide a large portion of the required hydrogen, which then no longer needs to be produced via water electrolysis, thus also representing a sustainable contribution.

[0224] Of the 14.97 t / h of oxygen 22b produced as a co-product during water electrolysis 22, 5.46 t / h are fed to partial oxidation 2

[0225] Example 3, Fig.2 - Inventive process - Gasification in polycarbonate composite - without CO2 recycling

[0226] In a gasification device 2, 10.935 t / h of polycarbonate-containing material 1b with an average composition of 75.65 wt.% carbon, 5.51 wt.% hydrogen, 18.9 wt.% oxygen, and 0.45 wt.% non-combustible inorganic solids are introduced. The conversion of the polycarbonate-containing material 1b takes place in the gasification device 2 in a zone 2a at 950°C, from which a CO and H2-containing product gas mixture 2c is fed into a zone 2b, and 0.54 t / h of ash is discharged (not shown). In 2b, the conversion of the gas mixture 2c introduced from 2a takes place at 1450°C. Furthermore, 9.89 t / h of oxygen 22b from a water electrolysis 22 are fed to the gasification device. The CO and H2-containing product gas mixture 2d from 2b is cooled to 60°C by washing with water in a washing step 3. 0.049 t / h of slag 3b and 0.1 t / h of water are separated.A portion of 1.6 t / h of the condensed water is purged and replaced by 1.7 t / h of fresh water.

[0227] The cooled product gas mixture 3a from washing step 3 is fed to a dryer 4.

[0228] The dried product gas mixture 4a is fed to an amine scrubber for CO2 separation 5, where 6.52 t / h of CO25b are separated. The gas mixture 5a, largely freed of CO2, is fed to a cold box for H2-CO separation 6, where the remaining CO2 is also separated. From the cold box, 12.61 t / h of CO 6b and 0.6 t / h of H2-containing residual gas 6a, along with small amounts of by-products including methane, are removed. The hydrogen-containing residual gas stream 6a separated from the cold box is fed to a pressure swing adsorption unit 7 for hydrogen purification, from which 0.55 t / h of H27a is separated and sent for further utilization.

[0229] The CO from the cold box is fed to a phosgene synthesis 8 and converted there with 31.97 t / h of CH to 44.58 t / h of phosgene 8a.

[0230] From the phosgene synthesis 8, 44.58 t / h of phosgene 8a are taken and reacted in a polycarbonate production 100 as a solution in chlorinated solvent (e.g. 482 t / h of a 1:1 mixture of methylene chloride and chlorobenzene) (2) with 599.4 t / h of 15 wt% bisphenol A solution 102 (89.9 t / h BPA corresponding to 393.8 kmol) in alkaline water (with 2.13 mol NaOH per mol bisphenol A, corresponding to 838.8 kmol NaOH = 33.5 t / h NaOH and 71.21 H2O as 32% sodium hydroxide solution) to give 102.9 t / h polycarbonate 101 by using at least one chain terminator (e.g. 2.55 t / h tert-butylphenol), 32.19 t / h of an additional 22 wt.% NaOH solution (7.08 t / h NaOH and 19.8 t / h H2O as 32% sodium hydroxide solution) and at least one catalyst (e.g., 0.5 t / h N-ethylpiperidine). 36.0 t / h NaOH with 76.5 t / h water are supplied as 32 wt.% sodium hydroxide solution 200a from the chlor-alkali electrolysis 200. An additional quantity of 4.58 t / h NaOH with 19.8 t / h H2O is added separately.

[0231] In polycarbonate production, 627.2 t / h of washing and process water are used, which, among other things, forms the NaCl-containing wastewater 200b.

[0232] The resulting NaCl-containing wastewater is obtained as NaCl-containing wastewater at a rate of 59.38 t / h NaCl and 1128.3 t / h water. A partial stream consisting of 0.85 t / h NaCl and 16.2 t / h H2O 200b is purified via a stripping system with carrier gas and an activated carbon purification system and fed into a CH production plant using chlor-alkali electrolysis 200. This covers the water requirement of the electrolysis, eliminating the need to add water to the chlor-alkali electrolysis. This conserves water resources. The resulting polycarbonate 101 is used to produce polycarbonate material for commercial applications.

[0233] After use of the polycarbonate material in various applications on the market, it can be collected and recycled as end-of-life material 110a in order to feed the resulting polycarbonate material waste after processing 1 as material for partial oxidation 1b into a gasification device.

[0234] The process according to the invention allows 6.25% of the carbon present in PC to be replaced with a non-fossil carbon source. By using renewable energy in chlor-alkali electrolysis, the CO2 footprint of the phosgene produced from CO and C12 is further reduced, thus enabling sustainably produced PC.

[0235] Example 4 Fig. 2 - Inventive process - Gasification in polycarbonate composite - with CO2 recirculation

[0236] In a gasification device 2, 10.935 t / h of polycarbonate-containing material 1b with an average composition of 75.65 wt.% carbon, 5.51 wt.% hydrogen, 18.9 wt.% oxygen, and 0.45 wt.% non-combustible inorganic solids are introduced. The conversion of the polyurethane-containing material 1b takes place in the gasification device 2 in a zone 2a at 950°C, from which a CO and H2-containing gas mixture 2c is fed into a zone 2b, and 0.54 t / h of ash is discharged. In 2b, the conversion of the gas mixture 2c introduced from 2a takes place at 1450°C. Furthermore, 9.89 t / h of oxygen from a water electrolysis and 6.52 t / h of CO2 from the CO2 separation unit are fed to the gasification device 2. The CO and H2-containing gas mixture from Zone 2 is cooled to 60°C by quenching with water. This separates 0.049 t / h of slag and 0.1 t / h of water.A portion of 2.67 t / h of the condensed water is purged and 0.1 t / h of fresh water is added.

[0237] The gas mixture from the gasification device 2 is fed to a dryer after cooling.

[0238] The dried gas mixture is fed to an amine scrubber for CO2 separation, where 6.52 t / h of CO2 are separated. The CO2 is fed back to the gasification unit. The gas mixture, largely free of CO2, is fed to a cold box for H2-CO separation, where the remaining CO2 is also separated. 16.77 t / h of CO and 0.31 t / h of H2, along with small amounts of by-products including methane, are removed from the cold box. The hydrogen-containing gas stream separated from cold box 6 is fed to a pressure swing adsorption unit 7 for hydrogen purification, from which 0.28 t / h of H2 is separated and sent for further utilization.

[0239] The CO 6b from the cold box 6 is fed to a phosgene synthesis 8 and converted there with 42.52 t / h of CH to 59.29 t / h of phosgene 8a.

[0240] From the phosgene synthesis 8, 44.58 t / h of phosgene 8a are taken and reacted in a polycarbonate production 100 as a solution in chlorinated solvent (e.g. 641 t / h of a 1:1 mixture of methylene chloride and chlorobenzene) (2) with 797.2 t / h of 15 wt.% bisphenol A solution 102 (119.56 t / h BPA corresponding to 523.74 kmol) in alkaline water (with 2.13 mol NaOH per mol bisphenol A, corresponding to 1115.6 kmol NaOH = 44.55 t / h NaOH and 94.69 t / h H2O as 32% sodium hydroxide solution)) as a diol to 136.85 t / h polycarbonate 101 by using at least one chain terminator (e.g. 3.39 t / h tert-butylphenol), 42.8 t / h of an additional 22% by weight NaOH solution (9.4 t / h NaOH and 26.3 t / h H2O as 32% sodium hydroxide solution), and at least one catalyst (e.g., 0.66 t / h N-ethylpiperidine). 47.88 t / h of NaOH are supplied with 101.75 t / h of water as 32% by weight sodium hydroxide solution from the chlor-alkali electrolysis 200.An additional quantity of 6.09 t / h NaOH with 26.33 t / h H2O is purchased externally and supplied.

[0241] In polycarbonate production, 834.17 t / h of washing and process water are used, which, among other things, forms the NaCl-containing wastewater.

[0242] The resulting NaCl-containing wastewater 200b, containing 78.97 t / h of NaCl and 1500.6 t / h of water, is collected as NaCl-containing wastewater. A partial stream consisting of 1.13 t / h of NaCl and 21.55 t / h of H2O is purified via a stripping system with carrier gas and an activated carbon purification system and fed into a C12 production plant using chloralkali electrolysis 200. This covers the water requirement of the electrolysis, eliminating the need to add water to the chloralkali electrolysis 200. This conserves water resources. The resulting polycarbonate 101 is used to produce polycarbonate material for commercial applications.

[0243] After use of the polycarbonate material in various applications in the market 110, it can be collected and recycled in order to feed the resulting polycarbonate material waste after processing 1 as material for partial oxidation 1b into a gasification device.

[0244] The process according to the invention allows 6.25% of the carbon present in the polycarbonate to be replaced with a non-fossil carbon source. By using renewable energy in chlor-alkali electrolysis, the CO2 footprint of the phosgene produced from CO and CE is further reduced, thus enabling a sustainably produced polycarbonate.

Claims

P a t e n t a n s p r ü c h e 1. Process for providing carbon monoxide for the production of phosgene, preferably for the production of phosgene for the synthesis of organic isocyanate compounds, comprising at least the following steps: b) Provision of an oxygen-containing gas stream (22b), containing at least 50 wt.-% oxygen gas, b) partial oxidation (2) of material (1a) containing at least one polymeric organic compound, wherein said material (1a) is introduced into a reactor (2a) of an apparatus and is treated there at least by supplying said oxygen-containing gas stream (22b) and heat at at least 400°C to form a product gas (2c), and the resulting product gas (2c), optionally after at least one further partial oxidation step (2b) of the product gas (2c), is discharged from the apparatus as a carbon monoxide-containing product gas stream (2d) together with particulate solid dispersed therein; c) the carbon monoxide-containing product gas stream (2d) is subjected to a purification process in which at least cl) the carbon monoxide-containing product gas stream (2d) is subjected to a washing step (3) for the separation of solid, wherein. (i) Water is brought into contact with the carbon monoxide-containing product gas stream (2d), causing the particulate solid dispersed in the carbon monoxide-containing product gas stream (2d) to form a slag (3b) and for this slag (3b) to be removed and carried away, (ii) the product gas stream (3a) containing carbon monoxide, purified of particulate solids, is discharged; c2) a product gas stream (3a) containing carbon monoxide, purified of particulate solids by washing step (3), is fed in a drying step to at least one separation of water (4), water (4b) is separated and the resulting carbon monoxide-containing product gas stream (4a) is discharged; c3) a carbon monoxide-containing product gas stream (4a) purified by separation of water (4) is fed to at least a carbon dioxide separation unit (5), carbon dioxide is separated, and the resulting carbon monoxide-containing product gas stream (5a) and carbon dioxide (5b) are discharged; c4) a carbon monoxide-containing product gas stream (5a) purified by separation of carbon dioxide is fed to at least a separation unit (6) for the separation of carbon monoxide, a separation of carbon monoxide is carried out, and the resulting carbon monoxide (6b) and a hydrogen gas-containing residual gas (6a) are discharged; c5) optionally, a hydrogen gas-containing residual gas (6a) separated by said separation unit (6) is fed to a residual gas treatment unit (7), hydrogen gas (7a) is separated, and hydrogen gas (7a) and final gas (7b) are discharged;d) optionally phosgene synthesis (8) by reacting at least chlorine gas and carbon monoxide, wherein at least the carbon monoxide (6b) from the purification of step c) is reacted as the carbon monoxide and phosgene (8a) is produced.

2. The process according to claim 1, characterized in that, to provide the oxygen-containing gas stream (22b), an electrolysis of water (22) is carried out to obtain oxygen gas (22a) and hydrogen gas, and the oxygen gas (22a) from this electrolysis (22) is used to provide the oxygen-containing gas stream (22b).

3. The process according to one of claims 1 or 2, characterized in that gaseous water is additionally supplied to the reactor (2a) in a weight ratio of gaseous water to oxygen gas of the oxygen-containing gas stream of at least 0.2; 4. Method according to one of the preceding claims, characterized in that the total amount of all polymeric organic compounds contained in the material (1a) is at least 50 wt.%, preferably at least 60 wt.%, particularly preferably at least 75 wt.%.

5. Method according to one of the preceding claims, characterized in that the weight ratio of the oxygen gas contained in the oxygen-containing gas stream (22b) to the polymeric, organic compound is introduced into the reactor (2a) within a weight ratio range of 0.4 to 1.0 to 1.2 to 1.0, preferably from 0.6 to 1.0 to 0.9 to 1.

0.

6. Method according to one of the preceding claims, characterized in that the polymeric, organic compound of the material (1a) is selected from at least one homopolymeric or copolymer compound from the group consisting of cellulose, polyester, polyamide, polyurethane (PUR), polyurea, polyisocyanurate (PIR), polycarbonate, preferably from at least one homopolymeric or copolymer compound from the group consisting of polyurethane (PUR), polyisocyanurate (PIR).

7. Method according to one of the preceding claims, characterized in that the structure of the polymeric organic compound of material (1a) contains at least one repeating structural unit of formula (1), wherein X 1 and X 2 independently of each other, a direct bond, O or NH, preferably O or NH, mean, Y 1 and Y 2 independently of each other they stand for O or NH, R 1 and R28. The process according to claim 7, characterized in that the total amount of the polymeric organic compounds containing at least one repeating structural unit of formula (1) in the material (1a) is at least 50 wt.%, preferably at least 60 wt.%, and particularly preferably at least 75 wt.%.

9. The process according to any one of the preceding claims, characterized in that the partial oxidation of the material (1a) in the reactor (2a) is carried out at a temperature in a temperature range of 600 °C to 1500 °C, in particular from 850 °C to 1400 °C, and more preferably from 1100 °C to 1300 °C. 10.A method according to any one of the preceding claims, characterized in that the carbon monoxide-containing product gas stream (3a) obtained from the washing step (3), purified of particulate solids, has a temperature of at most 100 °C, preferably at most 80 °C. A method according to any one of the preceding claims, characterized in that the partial oxidation (2) of the material (1a) is carried out in at least two steps, wherein in a first step a partial oxidation of the material (1a) is carried out in a first reactor (2a) by supplying an oxygen-containing gas stream (22b) at a temperature in a temperature range of 400 °C to 800 °C. The product gas (2c) of the first reactor is transferred to a second reactor (2b) and is subjected there in a further step to partial oxidation at a temperature of more than 800 °C, preferably at a temperature in the range of 1300°C to 1500°C, by supplying an oxygen-containing gas stream (22b), while obtaining the carbon monoxide-containing product gas stream (2d).

12. Method according to any one of claims 1 to 12, characterized in that the separated carbon dioxide (5b) released in step c3) is returned to a partial oxidation reactor (2) and introduced into this reactor.

13. Method according to claim 12, characterized in that the partial oxidation (2) of the material (1a) is carried out according to claim 11 and that the separated carbon dioxide (5b) released in step c3) is recycled at least to the first reactor (2a) of the partial oxidation and introduced into this reactor.

14. Method according to one of the preceding claims, characterized in that the carbon dioxide (5b) is added to the partial oxidation (2) in an amount of at most 1 kg per kg of polymeric organic compound, preferably at most 0.9 kg per kg of polymeric organic compound, particularly preferably at most 0.8 kg per kg of polymeric organic compound.

15. Method according to one of the preceding claims, characterized in that the Phosgene synthesis (8) in step d) and additionally the following step is carried out: e) Production of organic isocyanate (9) wherein the phosgene (8a) from the phosgene synthesis (8) is reacted with at least one organic amino compound (20a) and at least organic isocyanate (9a) is obtained.

16. Device for providing carbon monoxide for the production of phosgene, preferably for the production of phosgene for the synthesis of organic isocyanate compounds, comprising at least one metering device for feeding material, at least a device for partial oxidation and at least one purification device for carbon monoxide-containing product gas, characterized in that 1) said device for partial oxidation comprising at least one outlet for a carbon monoxide-containing product gas stream and at least one reactor for the partial oxidation of the material with at least one heating element suitable for temperature-controlling the reactor to a temperature of at least 400°C, wherein the reactor comprises at least one inlet for an oxygen-containing gas stream and at least one inlet for material and at least one outlet for product gas different from the above, wherein the inlet for an oxygen-containing gas stream is in fluid connection with a source of an oxygen-containing gas stream with a density of at least 50 wt.-% oxygen gas and the outlet for product gas of the reactor, optionally via at least one intermediate reactor for the partial oxidation of the product gas, is in fluid communication with the outlet for the carbon monoxide-containing product gas stream; and, ii) the metering device and said device for partial oxidation are arranged and designed such that the metering device is in fluid communication with the inlet for material of the reactor for the partial oxidation of the material via at least one supply line; and i ii) a purification device for carbon monoxide-containing product gas, which has at least one outlet for carbon monoxide and at least one inlet for the. containing a carbon monoxide-containing product gas stream, wherein this inlet is in fluid communication with the outlet for the carbon monoxide-containing product gas stream of the device for partial oxidation, wherein the purification device is designed such that the carbon monoxide-containing product gas stream can be passed through the following modules in the specified order of precedence for purification iii-1) at least one gas scrubbing device comprising at least one inlet for the carbon monoxide-containing product gas stream, at least one inlet for water, at least one scrubbing vessel in which water and carbon monoxide-containing product gas stream are combined, and at least one outlet for carbon monoxide-containing product gas stream and at least one outlet for slag, wherein the scrubbing vessel and the outlet for slag are in fluid communication and the scrubbing vessel and the outlet for carbon monoxide-containing product gas stream are in fluid communication;iii-2) at least one drying device, comprising at least one inlet for a carbon monoxide-containing product gas stream, at least one cooling device suitable for cooling the carbon monoxide-containing product gas stream, at least one outlet for a carbon monoxide-containing product gas stream, and at least one outlet for liquid condensate; iii-3) at least one device for separating carbon dioxide, comprising at least one inlet for a carbon monoxide-containing product gas stream, at least one outlet for a carbon monoxide-containing product gas stream, and additionally at least one outlet for carbon dioxide; iii-4) at least one separation unit for separating carbon monoxide, comprising at least one inlet for a carbon monoxide-containing product gas stream, at least one outlet for carbon monoxide, and additionally at least one outlet for; Residual gas containing hydrogen gas.

17. Device Claim 16, characterized in that at least one reactor of the device for partial oxidation has an inlet for carbon dioxide which is in a fluid connection with the outlet for carbon dioxide of the device for separating carbon dioxide, thereby enabling the return of carbon dioxide to this reactor of the device for partial oxidation against the flow direction of the carbon monoxide-containing product gas stream.

18. Device according to one of claims 16 or 17, characterized in that said device for partial oxidation comprises at least one outlet for a carbon monoxide-containing product gas stream and a first reactor for the partial oxidation of the material with at least one control system suitable for adjusting the temperature of the reactor to a temperature of at least 400°C, wherein the first reactor comprises at least one inlet for an oxygen-containing gas stream and at least one inlet for material and at least one outlet for product gas different therefrom, wherein the inlet for an oxygen-containing gas stream is in fluid connection with a source of an oxygen-containing gas stream with at least 50 wt.-% oxygen gas; and a second reactor for the partial oxidation of the product gas with at least one heating element suitable for temperature control of the reactor to a temperature of more than 800°C, wherein the second reactor has at least one inlet for an oxygen-containing gas stream and at least one inlet for optionally intermediate-treated product gas of the first reactor and at least one different outlet for product gas, wherein the outlet for product gas of the first reactor is in fluid communication with the inlet of the second reactor for optionally intermediate-treated product gas of the first reactor, and the inlet for an oxygen-containing gas stream is in fluid communication with a source of an oxygen-containing gas stream with at least 50 wt% oxygen gas, and the outlet for product gas of the second reactor is in fluid communication with the outlet for the carbon monoxide-containing product gas stream.

19. Device according to one of claims 16 to 18, characterized in that the outlet for carbon monoxide of the carbon monoxide separation unit is in fluid connection with the inlet of a reactor of a device for phosgene synthesis.

20. Use of material (2) containing at least one polymeric organic compound, in a partial oxidation of the material to provide carbon monoxide for the synthesis of phosgene.

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