Sustainable preparation of bisphenol A for the manufacture of polycarbonates

Abstract

The present invention relates to a method for preparing bisphenol A for synthesizing a polycarbonate as described in claim 1, a method for preparing a polycarbonate from bisphenol A obtained by the above-described preparation method as described in claim 14, and a multicomponent system for preparing bisphenol A by the above-described preparation method. In this method, bisphenol A is prepared from a provided acetone and a provided phenol, where these raw materials must be method products of a specific preparation method based on CO2, methane of biological origin, carbohydrates and / or organic solid compounds as starting materials.

Description

[Technical Field]

[0001] The present invention relates to a process for producing bisphenol A for the synthesis of polycarbonate, a process for producing polycarbonate from bisphenol A obtained by the aforementioned process, and a multi-component system for producing bisphenol A by the aforementioned process. [Background technology]

[0002] Industrial production of bisphenol A has historically relied primarily on fossil fuels, such as synthesis gas derived from natural gas and petroleum-based aromatic compounds. Systematically utilizing renewable raw materials and / or by-products from waste in the production of materials like bisphenol A is a goal for providing sustainable plastics such as polycarbonate and its derivatives.

[0003] It is also desirable to utilize energy from renewable energy sources for the industrial production of chemical raw materials, such as bisphenol A.

[0004] Patent Document 1 describes that bisphenol A can be produced from renewable phenol and renewable acetone, that is, from phenol and acetone derived from renewable raw materials. Therefore, acetone is produced from bioethanol, which is a renewable raw material source, or by fermentation. However, according to the teachings of the above document, the route for producing renewable acetone outlined therein is considered unsuitable for industrial-scale production. [Prior art documents] [Patent Documents]

[0005] [Patent Document 1] U.S. Patent Application Publication No. 2010 / 0152406 [Overview of the project]

[0006] Therefore, an object of the present invention was to provide a more sustainable manufacturing process for bisphenol A on an industrial scale that enables the use of renewable raw materials. Furthermore, a further object of the present invention was to provide a method for producing bisphenol A that enables the achievement of low-emission bisphenol A for the production of polycarbonates, even if fluctuations in the availability of renewable energy may occur. "Renewable energy" will be understood by those skilled in the art to mean energy from inexhaustible energy sources, such as wind, hydro, bioenergy (e.g., the conversion of biogas or biomass into electricity), or solar power.

[0007] The “sustainability” of a process is understood by those skilled in the art in accordance with the definition of sustainability (sustainable development) proposed in the Brundtland Report of the United Nations World Commission on Environment and Development, which means that the current implementation of a process contributes as little as possible, or no contribution at all, to the ability of future generations to meet their own needs, particularly their needs regarding the use of resources such as fossil fuels, and especially their needs regarding the preservation of living spaces, such as the protection of the Earth’s atmosphere. Accordingly, the object of the present invention is to make the production of bisphenol A and polycarbonates produced therefrom more sustainable than known production methods from the prior art. The contribution of the production of bisphenol A and polycarbonates to the satisfaction of future generations’ needs should be reduced, if not avoided.

[0008] First, the present invention provides a process for producing bisphenol A for the production of polycarbonate, comprising at least the following steps: a) A step of providing acetone which is a process product of a process including at least the following steps: i) At least the following steps: i-1) A step of obtaining methanol by conversion of CO, wherein CO is a process product of at least partial reduction from CO2 to CO and / or a process product of at least partial oxidation from an organic material to CO, wherein at least one organic material is selected from at least one organic solid compound, methane of biological origin, or a mixture thereof. A step of providing methanol, which is a process product of a process including, ii) From the methanol provided in advance, at least the following steps: A process that provides propene as a product of a process including at least the following steps, ii-1) A step of converting a pre-provided methanol to obtain a product mixture containing dimethyl ether, water, and methanol, ii-2) A step of converting a starting material containing dimethyl ether, water, and methanol from the aforementioned product mixture into propene by contacting it with a catalyst and preferably at least one zeolite compound at a temperature exceeding 200°C, ii-3) A step of converting propene by oxidation of at least propene to acetone, The process of synthesizing acetone by, Processes including, b) A step of providing phenol which is a process product of at least one manufacturing process comprising at least the following steps: i) At least one organoaromatic compound according to formula (I) [ka] (In the formula, R 1 is a hydrogen atom, a hydroxyl group, methyl, carboxyl, carboxylate, or -CHR 3 R 4 This represents, where R 3 and R 4 These independently represent (C1~C3)-alkyl groups or form an aliphatic hydrocarbon ring with residual molecules. R 2represents a hydrogen atom, methyl, carboxyl, or carboxylate, provided that R 1 is -CHR 3 R 4 When represents, R 2 represents a hydrogen atom, and when R 1 represents a hydroxyl group, R 2 represents a hydrogen atom, carboxyl or carboxylate, Here, the above organic aromatic compound is a process product of the conversion of at least one starting material selected from at least one compound selected from the group consisting of a polymer organic compound, a carbohydrate, and methane from a biological origin), and a step of providing In the above organic aromatic compound from step i) according to formula (I), when R 1 does not represent a hydroxyl group and R 2 does not represent a hydrogen atom, ii) Step ii-1) and / or step ii-2) and / or step iii-3) ii-1) A step of reacting the organic aromatic compound from step i) with propene to obtain a propane-2-yl-substituted aromatic organic compound as a product; ii-2) A step of oxidizing the organic aromatic compound from step i) and / or the product from step ii-1) to obtain at least one oxidized aromatic organic compound; ii-3) A step of removing at least one carbon-containing substituent from the organic aromatic compound from step i) and / or the oxidized organic aromatic compound from the oxidation in step ii-2); at least one of the steps of, including the steps of, c) Reacting the provided acetone with the provided phenol to result in bisphenol A, including the process of providing.

[0009] According to the present invention, the "catalytic reaction" or "catalytic reaction" is carried out using a catalyst that catalyzes the formation of a product from at least one reactant (e.g., carbon dioxide or methanol), thereby reducing the energy required and / or increasing selectivity to improve the product yield compared to the case where no catalyst is present under the same reaction conditions. For example, the conversion in step a)ii-2) is a catalytic reaction to yield propene from the above starting materials.

[0010] Step a) of the process according to the present invention includes providing acetone. According to the present invention, providing acetone is sufficient if the acetone provided is the actual process product of steps i) and ii) described in at least a). This means that carrying out the step of providing acetone is sufficient if the acetone is taken from a storage container or from a supply conduit as a raw material as part of the delivery and thereby supplied to at least step c) of the process according to the present invention. In this case, the bisphenol A producer, who is carrying out the process according to the present invention, does not carry out steps i) and ii) for producing the acetone described in a) of the process according to the present invention himself, but merely ensures that the acetone provided is produced by applying at least steps i) and ii) described in a) and is therefore the process product.

[0011] According to the present invention, for the purpose of providing acetone, steps i) and ii) for producing acetone as described in at least a) may be carried out by a bisphenol A producer as an essential step in the bisphenol A production process according to the present invention, and the acetone thereby obtained may be supplied to at least step c) of the process according to the present invention after intermediate storage in a storage container as necessary.

[0012] The possibility of a bisphenol A manufacturer providing, i.e., supplying or producing specific acetone in-house also applies in each case to the following embodiments of steps i) and ii) described in a).

[0013] Step i) described in a) of the process according to the present invention comprises at least the following steps: i-1) A step of obtaining methanol by conversion of CO, wherein CO is a process product of at least partial reduction from CO2 to CO and / or a process product of at least partial oxidation from an organic material to CO, wherein at least one organic material is selected from at least one organic solid compound, methane of biological origin, or a mixture thereof. The provision of methanol, which is a process product of a process including the process, is required.

[0014] According to the present invention, a material or compound is an organic substance if it contains at least one carbon-hydrogen covalent bond.

[0015] A substance is defined as a solid if it is in a solid state at 25°C and 10¹³ mbar.

[0016] According to the present invention, providing methanol is sufficient if the methanol is an actual process product of at least the reaction described in i-1), which utilizes carbon monoxide (also known as CO), which is also a process product of a particular process. This means that carrying out the step of providing methanol is sufficient if the methanol is taken out as a raw material as part of the delivery from a storage container or a supply conduit. In this case, the bisphenol A producer who is carrying out the process according to the present invention, or the provider of acetone provided for the process according to the present invention, does not carry out the aforementioned reaction for producing methanol himself, but merely ensures that the methanol provided for providing acetone is produced by applying at least step i-1) above and is therefore a process product.

[0017] According to the present invention, for the purpose of providing methanol, at least the aforementioned reaction for producing methanol may be carried out by a bisphenol A producer or a provider of acetone as an essential step in the bisphenol A production process according to the present invention, and the methanol thereby obtained may be supplied to the synthesis of acetone by step ii) provided in step a) of the process, after intermediate storage in a storage container as needed, while carrying out at least steps ii-1), ii-2), and ii-3).

[0018] The possibility of providing, i.e., supplying or producing in-house, specific methanol by a bisphenol A manufacturer also applies, in each case, to the following embodiments of the methanol provision.

[0019] The production of methanol typically involves the reaction of carbon oxides and hydrogen (this mixture is also called synthesis gas). This process is exothermic and can be represented by the following equation: CO + 2H2 ⇔ CH3OH CO2 + 3H2 ⇔ CH3OH + H2O

[0020] Both reactions are linked by a water-gas shift reaction, which is also an exothermic reaction, and can be expressed as follows: CO + H2O ⇔ CO2 + H2

[0021] Traditionally, methanol synthesis has used synthesis gas, which is mainly composed of CO and H2. This synthesis gas is produced from natural gas (fossil methane) and water vapor through a reforming process (steam reforming). The composition of the synthesis gas significantly affects the optimal utilization rate. This composition can be expressed by the stoichiometric number (SN): SN=(n H2 -n CO2 ) / (n CO +n CO2 )

[0022] When SN=2, the reactants exist in stoichiometric ratios according to the above reaction equation. However, in practice, slightly higher values ​​of SN (2.01~2.1) are used, which is achieved by increasing the hydrogen content in the synthesis gas (Dittmeyer et al. "Chemische Technik" [Chemical Technology], volume 4, 5th edition).

[0023] In the process according to the present invention, the carbon monoxide required for methanol conversion is provided not by conventional steam reforming using a fossil carbon source (natural gas), but by partial reduction of carbon dioxide and / or partial oxidation of the organic material to CO (and gasification if necessary).

[0024] According to the process of the present invention, the partial oxidation of an organic solid material (preferably an organic polymer material) includes converting the organic solid material into a CO-containing gas by partial oxidation (hereinafter also referred to as gasification), thereby providing CO from the organic solid material (preferably a spent polymer waste fraction) and an oxygen-containing gas.

[0025] For example, using a polymer-containing waste fraction (hereinafter referred to as the polymer waste fraction), which may preferably consist mostly of waste fractions containing PET, PE, PP, polyurethane, or polycarbonate, to provide CO means that these polymer-containing waste fractions are supplied for recycling, and in this way, bisphenol A is produced, and further, polycarbonate is produced from this bisphenol A with improved sustainability.

[0026] A "polymer compound" is a molecule having a relative molecular weight (Mw) of at least 2000 g / mol, and its chemical structure mainly consists of multiple repeating structural units derived from one or more different molecules with lower relative molecular weights. In the scope of this application, the average molar mass defined for a polymer or polymer compound is always the weight-average molar mass Mw unless explicitly specified otherwise, and this can, in principle, be measured by gel permeation chromatography using an RI detector, and the measurement should be performed against an external standard. A "polymer material" is a material containing at least one polymer compound.

[0027] Partial oxidation involves subjecting an organic material (preferably an organic solid material, particularly preferably a polymeric organic material, and most preferably a polymer waste fraction) to a partial oxidation reaction with oxygen, yielding a product gas mixture containing hydrogen and CO, and optionally by-products. The by-products are particularly hydrocarbons having 1 to 8 carbon atoms. CO2 and water vapor are also present in the product gas mixture.

[0028] Further by-products obtained in the gasification process are residual fractions that cannot be reacted any further.

[0029] The temperature required for gasification is at least partially achieved by partially burning (partially oxidizing) the organic solid material (preferably a polymeric organic material, particularly preferably a polymer waste fraction) with an oxygen-containing gas. The partial oxidation of the introduced organic solid material 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 in a temperature range of 600°C to 1500°C, particularly 850°C to 1400°C, and more preferably 1100°C to 1300°C.

[0030] Carbon monoxide provided as a process product of partial oxidation is obtained, for example, through at least the following steps: 1) A step of providing an oxygen-containing gas stream containing at least 50% by weight of oxygen gas, 2) A step of partially oxidizing an organic material (preferably an organic material containing at least one polymeric organic compound), wherein the organic material is introduced into a reactor of the apparatus, where at least the oxygen-containing gas stream is provided and it is treated by heating at at least 400°C to form a product gas, and the resulting product gas is discharged from the apparatus as a carbon monoxide-containing product gas stream together with particulate solids dispersed therein, after at least one further partial oxidation step of the product gas as necessary. 3) A step of supplying a carbon monoxide-containing product gas stream to the purification process, wherein at least, 3-1) The carbon monoxide-containing product gas stream is supplied to the washing process for solid separation, where, (i) Water is brought into contact with a carbon monoxide-containing product gas stream, and as a result, particulate solids dispersed in the carbon monoxide-containing product gas stream form slag, which is then removed and discharged. (ii) A gas stream containing carbon monoxide, from which particulate solids have been purified, is discharged. 3-2) The carbon monoxide-containing product gas stream, from which particulate solids have been purified by the washing process, is supplied to at least one water separator in the drying process, the water is separated, and the resulting carbon monoxide-containing product gas stream is discharged. 3-3) The carbon monoxide-containing product gas stream purified by the separation of water is fed to at least one carbon dioxide separator to separate the carbon dioxide, and the resulting carbon monoxide-containing product gas stream and carbon dioxide are discharged. 3-4) The carbon monoxide-containing product gas stream purified by the separation of carbon dioxide is supplied to at least one separation unit for carbon monoxide separation, carbon monoxide separation is carried out, and the resulting carbon monoxide and hydrogen gas-containing residual gas is discharged. 3-5) If necessary, the hydrogen gas-containing residual gas separated using the above separation unit is supplied to the residual gas treatment to separate the hydrogen gas, and the hydrogen gas and final gas are discharged, in a process, It may be produced by a process for producing carbon monoxide for the provision of methanol containing methanol.

[0031] It is known that a solid is "particulate" when it takes the form of a granular mixture of numerous free solid particles of the substance mentioned above, and this itself includes so-called granules. The term "granular material" refers to the particulate components of powder (granular material is free solid particles), fine powder (granular material is free solid particles), granules (free solid particles are aggregates of multiple granular materials), and other granular mixtures.

[0032] A "reactor" is a spatial region where chemical transformations, such as the partial oxidation of a polymeric organic compound, occur. In the case of partial oxidation, this can refer to, for example, the spatial region of a heating vessel containing the material.

[0033] The oxygen gas required for partial oxidation can be obtained, for example, from a water electrolysis device or an air separation device. In a preferred embodiment of partial oxidation, the oxygen-containing gas stream is provided by performing electrolysis of water to obtain oxygen gas and hydrogen gas, and the oxygen gas from this electrolysis is used to provide the oxygen-containing gas stream.

[0034] Water electrolysis can be carried out using conventional equipment. Industrial systems for alkaline water electrolysis and polymer electrolyte-based electrolysis, so-called PEM electrolysis, are known and commercially available. The principle of water electrolysis is described as an example in Chapter 6.3.4 of "Elektrochemische Verfahrenstechnik" [Electrochemical process technology] by Volkmar M. Schmidt (2003 Wiley-VCH-Verlag; ISBN 3-527-29958-0).

[0035] According to the present invention, the organic solid material introduced into the reactor for partial oxidation preferably comprises at least one polymeric organic compound. It is desirable that the partial oxidation be carried out as uniformly and selectively as possible within the reactor. In preferred embodiments, in each case, an increase in these parameters can be achieved when the weight ratio of oxygen gas to polymeric organic compound present in the oxygen-containing gas stream, based on the time before introduction, is in the range of 0.4:1.0 to 1.2:1.0, preferably 0.6:1.0 to 0.9:1.0.

[0036] In a preferred embodiment, the partial oxidation of the introduced organic solid material is carried out at an absolute pressure greater than 1 bar, preferably in the range of 2 bar to 80 bar, and particularly preferably in the range of 2 bar to 50 bar.

[0037] Partial oxidation of organic solid materials can be carried out in at least one of the following three reactors: a jet bed gasification reactor, a fluidized bed gasification reactor, and a fixed bed gasification reactor.

[0038] When used in a jet-bed gasification reactor, the organic solid material has an average particle size of less than 0.1 mm (fine powder). 50.3The material must be pulverized to a particle size having [specific properties]. Supply to the reactor is either by air pressure or as a slurry. The greatest constraint of this type of partial oxidation in the chemical recycling of waste is the pulverizability and transportability of the starting material from heterogeneous waste. Using the O2-free heat treatment (roasting) of biomass at 200°C-300°C, "biochar" with pulverizability similar to coal can be produced. In another modification, upstream pyrolysis can be used to produce pyrolysis oil that can be pumped. The oil obtained by the pyrolysis of waste can be partially oxidized either directly or in the form of a slurry mixed with solid pyrolysis residue (pyrolysis coke). This process configuration was developed by Noell (Noell-Konversionsverfahren zur Verwertung und Entsorgung von Abfaellen [Noell conversion process for the recovery and disposal of waste], Juergen Carl EF-Verl. fuer Energie- und Umwelttechnik, 1994, ISBN: 3924511829).

[0039] Another variation is the use of a fluidized bed gasification reactor. The gasification of organic solid materials, particularly waste, in fluidized bed reactors is well known through the technologies of EBARA (Showa Denko K.K., Japan) and ENERKEM (Enerkem GmbH, Edmonton, Canada), as well as through the large-scale demonstration of high-temperature winkler gas production (HTW) by Rheinbraun AG (now RWE) in Berlenrath, Germany, from 1993 to 1997. Pretreatment for introducing organic materials or materials containing polymeric organic compounds into the reactor involves X-rays with an average particle size of 30 mm to 80 mm. 50.3Fine grinding is required. Introduction to the reaction vessel is via a screw conveyor, and the gasification pressure is limited to 10 bar or less. ENERKEM and EBARA technologies enable the gasification of high-calorie waste (plastic waste or alternative fuels containing a large amount of plastic). Fluidized bed gasifiers are operated at a gentle temperature of 700°C to 950°C, much lower than the melting point of the ash of the inserted material, to avoid solidification and agglomeration within the reactor. A further advantage of this gentle reactor temperature is incomplete carbon turnover in the fluidized bed. Furthermore, the crude gas discharged from the fluidized bed gasifier reactor typically contains a considerable amount of methane and other hydrocarbons. To compensate for this and ensure a high synthesis gas yield of H2 and CO, the ENERKEM and EBARA processes utilize a second high-temperature stage (approximately 1400°C) for partial oxidation just downstream of the fluidized bed, thereby melting the fly ash and converting the hydrocarbons in the product gas from the first stage into a final product gas stream containing carbon monoxide. ENERKEM calls this second stage the "thermoreformer," while EBARA calls it the "high-temperature gasification furnace." The high temperature in this second partial oxidation stage increases the amount of CO2 produced.

[0040] The CO for providing methanol may also preferably be a process product derived from the conversion of methane from biological sources by partial oxidation in a classical reforming process. In a preferred embodiment of such provision, the CO is a process product obtained by reacting methane and steam from at least biological sources (particularly preferably with the addition of CO2) at a temperature of at least 500°C while supplying thermal energy to produce carbon monoxide. A further suitable sustainable reforming process with the addition of CO2 is described in the PCT patent application no. PCT / EP2022 / 052267, the contents of which are fully and expressly part of this specification by reference. This process is for the production of carbon monoxide from methane, steam, and CO2 from biological sources, and comprises at least the following steps: A step of synthesizing carbon monoxide in a reforming process that reacts methane and water vapor of biological origin with at least CO2 added and supplied with thermal energy at a temperature of at least 500°C to produce a carbon monoxide-containing product gas, The carbon monoxide-containing product gas obtained from the aforementioned synthesis is purified by separating at least CO2, and then, if necessary, by separating water, separating hydrogen, or at least one separation selected from a combination thereof, to obtain carbon monoxide. The process includes at least the step of providing CO2 from the separation of CO2 in the aforementioned purification process to the addition of CO2 to the aforementioned reforming process, Including, relating to manufacturing.

[0041] Furthermore, it is preferable that the thermal energy supplied to the reforming process for carbon monoxide synthesis is provided by at least one method selected from (i) combustion of a hydrogen-containing fuel produced by renewable energy, (ii) combustion of a methane-containing fuel of biological origin, and (iii) conversion of electrical energy from renewable energy into heat.

[0042] "Methane of biological origin" (also called "biomethane") is understood by those skilled in the art to mean methane industrially obtained from biomass through methane fermentation, in contrast to fossil methane. Methane fermentation is known to mean the anaerobic decomposition of organic matter by microorganisms. Methane of biological origin is produced, for example, in biogas plants that ferment both organic waste and renewable raw materials in proportion to each other.

[0043] To those skilled in the art, “renewable energy” is understood to mean energy from inexhaustible energy sources, such as wind energy, hydroelectric energy, bioenergy (e.g., the conversion of biogas or biomass into electricity), or solar energy. Therefore, suitable renewable energy is most preferably wind, solar, hydroelectric, or a mixture thereof.

[0044] According to the present invention, methanol provided according to step i) of process step a) according to the present invention is the process product of the reaction of CO, where the CO used in the reaction is the process product of at least partial reduction from CO2 to CO, and is particularly preferred when selected from a reverse water-gas shift reaction using H2 produced by electrolysis (preferably water electrolysis, i.e., electrolysis of water), from an electrochemical reduction from CO2 to CO, or a combination thereof.

[0045] In a particularly preferred embodiment of the process according to the present invention, the methanol provided is provided as a process product of the conversion of CO, where the CO used in the conversion is at least CO x The process product is produced by at least partial reduction of a gas stream containing (wherein x=1 or 2) and, optionally, hydrogen gas.

[0046] Furthermore, in one embodiment of this process, it was found to be extremely preferable when methanol was obtained by the conversion of CO2, with or without hydrogen, and used to provide methanol. It is also particularly preferable when the reaction is an electrochemical reaction, a homogeneous catalytic reaction, or a heterogeneous catalytic reaction. In a further embodiment, the CO2 used here is derived from a further CO2 source, for example, CO2 emitted in the provision of thermal energy, or from an external CO2 source, for example, CO2 from industrial off-gas.

[0047] According to the present invention, the "electrochemical reaction" is carried out by passing an electric current through a reaction medium in the presence of at least one reactant (e.g., carbon dioxide) (for example, through at least one electrode immersed in the reaction medium).

[0048] A "catalytic reaction" or "catalytic reaction" is defined as described above (see above). According to the present invention, a "homogeneous catalytic reaction" is carried out using a homogeneous catalyst, and a "heterogeneous catalytic reaction" is carried out using a heterogeneous catalyst.

[0049] A preferred CO2 source is at least one "external CO2 source" that provides CO2 that is not emitted by the process according to the present invention. Examples of external CO2 sources include CO2 produced in off-gases from fuel combustion (e.g., waste incineration) in cement production, H2 production for ammonia synthesis, fermentation, or CO2 obtained from air.

[0050] In a particularly preferred embodiment of the process according to the present invention, carbon monoxide for methanol synthesis is produced from CO2 by a reaction of at least hydrogen with CO2 in a reverse water-gas shift (RWGS) reaction zone. Such embodiments of carbon monoxide production are described, for example, in International Publication No. 2021 / 089737, the contents of which are fully and expressly incorporated herein by reference.

[0051] A "reaction zone" is a portion of the reaction space in which a chemical reaction, such as a reverse water-gas shift reaction, takes place. A "reaction space" is a spatial region in which co-reactants involved in a chemical reaction are attracted to each other and the chemical reaction occurs. In the case of a chemical reaction, this may be, for example, the spatial region of a container in which the reactants, such as carbon dioxide in the case of the RWGS reaction, and their co-reactants, such as hydrogen in the case of the RWGS reaction, coexist and react in the reaction zone. This spatial region may be, for example, the inside of a reactor.

[0052] The hydrogen gas used in the RWGS reaction is preferably supplied by electrolysis, particularly by chlor-alkali electrolysis or water electrolysis, and most preferably by water electrolysis. This also preferably uses electrical energy generated from renewable energy sources (in particular hydroelectric, solar, or wind power) in each case.

[0053] In a particularly preferred process, carbon monoxide provided for the provision of methanol is obtained by at least the following steps: A process for supplying a CO2 gas flow, A process to obtain purified carbon dioxide by purifying secondary components, particularly nitrogen oxides, sulfur compounds, fine particles, water, oxygen, and HCl, from a CO2 gas stream, as needed, by adsorption, gas washing, or catalytic treatment. The process involves introducing hydrogen gas, provided along with a purified CO2 gas stream, into the RWGS reaction zone, reacting the reactants according to the principle of the RWGS reaction, and obtaining a product gas mixture consisting of water vapor, CO, and optionally by-products, particularly lower hydrocarbons, especially preferably methane. From the gas mixture obtained from the RWGS reaction, unreacted carbon dioxide is separated, particularly by amine washing, and the unreacted carbon dioxide is recycled back into the RWGS reaction. The process involves separating hydrogen that was not converted in the RWGS reaction from the gas mixture of carbon monoxide and hydrogen obtained after separation, particularly using a cold box, and recycling the hydrogen back into the RWGS reaction as needed. A process to discharge residual carbon monoxide after separation, It is a product of a process that includes [the specified element].

[0054] The CO2 source for providing the CO2 gas flow is, for example, CO2 released when providing thermal energy for the process according to the present invention (e.g., for the RWGS reaction), CO2 obtained from air separation, or CO2 from a further external CO2 source.

[0055] An external CO2 source provides CO2 that is not emitted by the process or its embodiments according to the present invention. Examples of external CO2 sources include CO2 formed in off-gas during cement production or during the combustion of fuel (e.g., waste incineration), or CO2 obtained from air. In a preferred embodiment of the process of the present invention, this CO2 from the external CO2 source is obtained by (i) a process gas or off-gas selected from at least one process selected from cement production, H2 production, and incineration, and / or (ii) absorption of a CO2 fraction from air by introduction into an alkali metal hydroxide solution, such as a potassium hydroxide solution. As a result, potassium bicarbonate is formed, which is then thermally decomposed back into CO2 and potassium hydroxide. The released CO2 is fed into the process of the present invention for the synthesis of carbon monoxide.

[0056] The RWGS reaction is preferably carried out in the reaction zone at a temperature of 650°C or higher, particularly preferably 700°C or higher, and most preferably 750°C or higher.

[0057] The RWGS reaction is preferably carried out in the presence of at least one catalyst. The latter is more preferably selected from at least one compound from the following group: (I) Equation A (1-w-x) A' w A'' x B (1-y-z) B' y B'' z O 3-δ mixed metal oxides (In the formula, A, A', and A'' are independently selected from the group Mg, Ca, Sr, Ba, Li, Na, K, Rb, Cs, Sn, Sc, Y, La, Ce, Pr, Nd, Pm, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Yb, Tl, Lu, Ni, Co, Pb, Bi, and / or Cd. B, B', and B'' are independently selected from the group consisting of Cr, Mn, Fe, Bi, Cd, Co, Cu, Ni, Sn, Al, Ga, Sc, Ti, V, Nb, Ta, Mo, Pb, Hf, Zr, Tb, W, Gd, Yb, Mg, Li, Na, K, Ce, and / or Zn. 0≦w≦0.5;0≦x<0.5;0≦y≦0.5;0≦z≦0.5 and -1≦δ≦1); (II) Equation A (1-w-x) A' w A'' x B (1-y-z) B' y B'' z O 3-δ mixed metal oxides (In the formula, A, A', and A'' are independently selected from the group Mg, Ca, Sr, Ba, Li, Na, K, Rb, Cs, Sn, Sc, Y, La, Ce, Pr, Nd, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Yb, Tl, Lu, Ni, Co, Pb, and / or Cd. B is selected from the group consisting of Cr, Mn, Fe, Bi, Cd, Co, Cu, Ni, Sn, Al, Ga, Sc, Ti, V, Nb, Ta, Mo, Pb, Hf, Zr, Tb, W, Gd, Yb, Mg, Cd, Zn, Re, Ru, Rh, Pd, Os, Ir, and / or Pt. B' is selected from the group Re, Ru, Rh, Pd, Os, Ir, and / or Pt, and B'' is selected from the group Cr, Mn, Fe, Bi, Cd, Co, Cu, Ni, Sn, Al, Ga, Sc, Ti, V, Nb, Ta, Mo, Pb, Hf, Zr, Tb, W, Gd, Yb, Mg, Cd, and / or Zn. 0≦w≦0.5;0≦x≦0.5;0≦y≦0.5;0≦z≦0.5 and -1≦δ≦1); (III) A mixture of at least two different metals M1 and M2 supported on a carrier containing an oxide of Al, Ce, and / or Zr, which is doped with metal M3: Here, M1 and M2 are independently selected from the group Re, Ru, Rh, Ir, Os, Pd, and / or Pt. M3 is selected from the group consisting of Sc, Y, La, Ce, Pr, Nd, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Yb, and / or Lu; (IV) formula LO x (M (y / z) Al (2-y / z) O3) z mixed metal oxide (wherein, L is selected from the group consisting of Na, K, Rb, Cs, Mg, Ca, Sr, Ba, Sc, Y, Sn, Pb, Pd, Mn, In, Tl, La, Ce, Pr, Nd, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Yb, and / or Lu, M is selected from the group consisting of Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Re, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd, Pt, Zn, Cu, Ag, and / or Au, 1 < x ≦ 2; 0 < y ≦ 12; and 4 ≦ z ≦ 9); (V) formula LO(Al2O3) z mixed metal oxide (wherein, L is selected from the group consisting of Na, K, Rb, Cs, Mg, Ca, Sr, Ba, Sc, Y, Sn, Pb, Mn, In, Tl, La, Ce, Pr, Nd, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Yb, and / or Lu, 4 ≦ z ≦ 9); (VI) an oxide catalyst containing Ni and Ru; (VII) a metal M1 and / or at least two different metals M1 and M2 supported on and / or in a carrier, where the carrier is, a carbide, oxycarbide, carbonitride, nitride, boride, silicide, germanide, and / or selenide of metal A and / or metal B, M1 and M2 are independently selected from the group consisting of Cr, Mn, Fe, Co, Ni, Re, Ru, Rh, Ir, Os, Pd, Pt, Zn, Cu, La, Ce, Pr, Nd, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Yb, and / or Lu, A and B are independently selected from the group Be, Mg, Ca, Sc, Ii, V, Cr, Mn, Fe, Co, Ni, Y, Zr, Nb, Mo, Hf, Ta, W, La, Ce, Pr, Nd, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Yb, and / or Lu; and / or, Reaction products of (I), (II), (III), (IV), (V), (VI), and / or (VII) at a temperature of 700°C or higher in the presence of carbon dioxide, hydrogen, carbon monoxide, and / or water.

[0058] In an equally preferred embodiment of this process, the methanol provided to provide acetone in the process according to the present invention is produced from carbon monoxide, where carbon monoxide is a product of the electrochemical partial reduction of carbon dioxide to yield carbon monoxide. In this embodiment, CO provision is carried out by introducing a stream of CO2 gas into an electrolytic device and reducing the stream to carbon monoxide at an electrode, preferably a gas diffusion electrode (particularly preferably using electrical energy generated from renewable energy). This electrochemical partial reduction is hereafter referred to as CO2 electrolysis.

[0059] CO2 electrolysis is a high-temperature electrolysis process, for example, operated at temperatures exceeding 600°C, and water may be added to produce synthesis gas. High-temperature electrolysis is generally known, and products such as Haldor Topsoe's eCOs (trademark) are commercially available. High-temperature electrolysis forms oxygen at the anode.

[0060] When CO2 electrolysis is operated as low-temperature electrolysis, the electrolysis is carried out at a temperature of less than 150°C.

[0061] In all CO2 electrolysis processes, CO2 gas is supplied to the cathode space.

[0062] In low-temperature electrolysis, CO2 is converted to carbon monoxide, and optionally hydrogen, in particular, at a gas diffusion electrode. Those skilled in the art will recognize electrodes and methods for carrying out the electrochemical reduction of CO2, for example, from International Publication No. 2021 / 069470. The electrochemical reduction of CO2 is preferably carried out by the process of International Publication No. 2021 / 069470, which expressly and entirely constitutes a part of this specification by reference. In this preferred electrolytic process for the production of carbon monoxide, carbon monoxide, and optionally hydrogen and chlorine, are obtained by the electrochemical conversion of carbon dioxide with an alkali metal chloride solution. This preferred electrolytic process is characterized in that carbon dioxide is electrochemically reduced at a gas diffusion electrode as a cathode in an aqueous alkali metal chloride-containing solution as the cathode solution, and at the same time, chlorine is anodically produced from the aqueous alkali metal chloride-containing solution as the anode solution, where the alkali metal salt of carbonic acid formed in the cathode solution (selected from alkali metal carbonate, alkali metal bicarbonate, or a mixture thereof) is then reacted with hydrogen chloride to produce carbon dioxide and alkali metal chloride, the released carbon dioxide is returned to the cathode space of the gas diffusion electrode, and the produced alkali metal chloride is returned to either the anode space and / or the cathode space.

[0063] According to known principles, the MEA (membrane-electrode assembly) concept can also be used for low-temperature electrolysis. In this case, a catalyst is applied to the membrane. An upstream gas diffusion layer controls the transport of gases and liquids. This can be done on both the anode and cathode sides. It is also possible to have the gas diffusion electrode in direct contact with the membrane.

[0064] The gas diffusion electrodes used can be installed in a zero-gap or finite-gap configuration within the electrolytic cell. A preferred configuration for low-temperature electrolysis of CO2 is described in International Publication No. 2020 / 057998, which, by reference, constitutes an entire and express part of this specification.

[0065] An excess amount of CO2 can be supplied to the cathode space, or to the gas diffusion electrode installed therein. "Excess" means introducing more CO2 than is required for the stoichiometric conversion based on the flowing current. In this way, a mixed gas consisting of unreacted CO2, CO, and H2 passes through the cathode space.

[0066] In a further embodiment of CO2 electrolysis, it is preferable that the electrical energy used is generated from renewable energy sources, particularly from wind, solar, or hydroelectric power.

[0067] If the carbon monoxide used to provide methanol is a process product of at least one of the aforementioned processes, the reaction of CO to impart methanol can be at least one of the processes known to those skilled in the art, starting from CO-containing synthesis gas.

[0068] However, in step ii-1), if CO mixed with sufficient hydrogen as synthesis gas is not directly provided, or if there is a shortage of sufficient hydrogen gas, the CO is mixed with hydrogen gas to produce synthesis gas before conversion to methanol. This hydrogen gas, which is added to the CO as part of the methanol supply, is preferably provided by electrolysis, in particular by chlorine-alkaline electrolysis or water electrolysis. Water electrolysis can be carried out using prior art equipment. Industrial systems for alkaline water electrolysis and polymer electrolyte-based electrolysis, so-called PEM electrolysis, are known and commercially available. The principle of water electrolysis is described as an example in Chapter 6.3.4 of "Elektrochemische Verfahrenstechnik" [Electrochemical process technology] by Volkmar M. Schmidt (2003 Wiley-VCH-Verlag; ISBN 3-527-29958-0). In further embodiments, the electrical energy used for electrolysis for hydrogen production is preferably electrical energy generated from renewable energy sources, in particular from wind power, solar power, or hydropower.

[0069] Particularly preferred is an embodiment in which methanol supplied to the process according to the present invention is produced in proportion to the process product using renewable energy, preferably in a geographical location where renewable energy is readily available, and thereby supplied to the process of the present invention either by container transport or by methanol flow in a continuous process. To supply to a continuous process, methanol production is preferably fluidly connected to acetone production, for example, via a pipeline.

[0070] Methanol production equipment is licensed on the market from companies such as Air Liquide and Johnson Matthey. An overview of the classic production of methanol from synthesis gas is provided, for example, in Ott et al., Methanol in: Ullmann's Encyclopedia of Industrial Chemistry, 2012, Wiley-VCH Verlag, Weinheim (doi 10.1002 / 14356007.a16_465.pub3), which, by reference, constitutes an entire and express part of this specification.

[0071] The methanol provided in accordance with step a)i) as described above is used in step a)ii) of the process according to the present invention for providing acetone, in at least the following steps: A process that provides propene as a product of a process including at least the following steps, ii-1) A step of converting a pre-provided methanol to obtain a product mixture containing dimethyl ether, water, and methanol, ii-2) A step of converting a starting material containing dimethyl ether, water, and methanol from the aforementioned product mixture into propene by contacting it with a catalyst and preferably at least one zeolite compound at a temperature exceeding 200°C, ii-3) A step of converting propene by oxidation of at least propene to acetone, It is converted to acetone by a process that includes [a specific component].

[0072] Steps ii-1) and ii-2) are part of the methanol-to-propylene process (also known as the MTP process). The MTP process was first developed by Lurgi.

[0073] In the MTP process, for example, gaseous methanol is reacted on a catalyst in a reactor to produce a product mixture containing dimethyl ether, water, and methanol according to step ii-1) of the process according to the present invention. Suitable reactors include, for example, fixed-bed reactors or fluidized-bed reactors.

[0074] In a preferred embodiment of the process according to the present invention, the reaction of methanol provided according to step a)ii-1) is carried out by contacting methanol, preferably methanol in the gas phase, with a catalyst.

[0075] Examples of particularly preferred catalysts suitable for the conversion of methanol in step ii-1) are Al2O3 pellets, such as those described in European Patent No. 0448000 or German Patent Application Publication No. 19723363.

[0076] Prior to the conversion of methanol in step a)ii-1), the provided methanol is preferably heated to a temperature in the range of 200°C to 350°C, and the conversion is carried out using this appropriately temperature-controlled methanol. After the conversion, the product mixture containing dimethyl ether, methanol, and water also preferably has a temperature of 350°C to 450°C.

[0077] The product mixture from step ii-1), particularly in the form of a gaseous flow, is introduced into a further reactor, for example, as the starting material for step ii-2), after undergoing an optional purification step as needed, where it is converted to propene on a catalyst. Examples of suitable catalysts include the catalyst sold by Clariant under the trade name MTPROP®, or zeolite compound catalysts such as those described in, for example, column 1, lines 43-52 of U.S. Patent No. 7,015,369, and in Examples 1 and 2. In further embodiments of the process according to the present invention, the starting material is converted to propene, preferably by contact with a zeolite compound as a catalyst.

[0078] In step ii-2), it is preferable to react the starting materials at a temperature of 350°C to 600°C, particularly 380°C to 550°C.

[0079] The propene provided in step ii-2) of the process according to the present invention is oxidized to yield acetone, after separation of secondary components as necessary, according to step ii-3). In addition, as described below, in one embodiment of step b) of the process according to the present invention, it may be preferable to use the propene provided in step ii-2) in the provision of phenol according to step b) via a cumene intermediate step in cumene oxidation to obtain phenol and acetone (see below).

[0080] The oxidation step of propene according to the present invention (ii-3) is, for example, the following method: 1) A method for producing acetone by the reaction of propene with water using a catalyst system composed of palladium(II) chloride and copper(II) chloride, according to the Wacker-Hoechst process; 2) A method of hydroxylating propene with water to obtain 2-propanol, followed by catalytic dehydrogenation of 2-propanol to obtain acetone; 3) A method of obtaining acetone by converting propene to cumene and carrying out the cumene hydroperoxide method (Hock method), or by converting propene to diisopropylbenzene and carrying out the cumene hydroperoxide method using diisopropylbenzene hydroperoxide instead of cumene hydroperoxide; It can be carried out in accordance with at least one of the following.

[0081] Those skilled in the art are familiar with these methods and their implementation, for example, as described in the publication Weber et al., Acetone in: Ullmann's Encyclopedia of industrial chemistry, 2013, Wiley-VCH Verlag, Weinheim (doi 10.1002 / 14356007.a01_079.pub4), which is fully and expressly part of this by reference.

[0082] In addition, the process according to the present invention includes not only the provision of acetone as described above, but also the provision of phenol in step b), wherein the phenol provided is provided in at least the following steps: i) At least one organoaromatic compound according to formula (I) [ka] (In the formula, R 1 is a hydrogen atom, a hydroxyl group, methyl, carboxyl, carboxylate, or -CHR 3 R 4 This represents, where R 3 and R 4 These independently represent (C1~C3)-alkyl groups or form an aliphatic hydrocarbon ring with residual molecules. R 2 R represents a hydrogen atom, methyl, carboxyl, or carboxylate, however, R 1 ga-CHR 3 R 4 When representing R, 2 represents a hydrogen atom, and R 1 When R represents a hydroxyl group, 2 This represents a hydrogen atom, carboxyl, or carboxylate. Here, the above-mentioned organic aromatic compound is a process product of the transformation of at least one starting material selected from the group consisting of high-molecular-weight organic compounds, carbohydrates, and methane of biological origin. In the above organic aromatic compound from step i) according to formula (I), R1 does not represent a hydroxyl group, R 2 If does not represent a hydrogen atom, ii) Steps ii-1) and / or ii-2) and / or iii-3) ii-1) A step of reacting the organic aromatic compound from step i) with propene to obtain a propan-2-yl substituted aromatic organic compound as a product; ii-2) A step of oxidizing the organic aromatic compound from step i) and / or the product from step ii-1) to obtain at least one oxidized aromatic organic compound; ii-3) A step of removing at least one carbon-containing substituent from the organic aromatic compound from step i) and / or the oxidized organic aromatic compound from oxidation by step ii-2); At least one of the following steps, It is a process product of at least one manufacturing process that includes [the specified element].

[0083] According to the present invention, "phenol" is understood to mean the compound monohydroxybenzene.

[0084] In step b) of the process according to the present invention, phenol is provided. According to the present invention, for the provision of phenol, it is sufficient that the phenol provided is the actual process product of steps i) and ii) described in at least b). This means that for the implementation of the step of providing phenol, it is sufficient to simply take the phenol from the storage container or from the supply conduit as a raw material as part of the delivery and thereby supply it to at least step c) of the process according to the present invention. In this case, the bisphenol A producer, who is implementing the process according to the present invention, does not perform steps i) and ii) for producing the phenol described in b) of the process according to the present invention himself, but merely ensures that the phenol provided is produced by applying steps i) and ii) described in at least b) and is therefore the process product.

[0085] According to the present invention, for the purpose of providing phenol, steps i) and ii) for producing phenol as described in at least b) may be carried out by a bisphenol A producer as an essential step in the bisphenol A production process according to the present invention, and the phenol obtained thereby may be supplied to at least step c) of the process according to the present invention after intermediate storage in a storage container, if necessary.

[0086] The possibility of a bisphenol A manufacturer providing, i.e., supplying or producing in-house, a specific phenol also applies in each case to the following embodiments of steps i) and ii) described in b).

[0087] The above organic aromatic compound process product of formula (I) according to step b)i) is provided by the transformation of at least one starting material selected from at least one compound from the group consisting of high molecular weight organic compounds, carbohydrates, and methane of biological origin. Suitable starting materials are preferably at least one high molecular weight organic compound selected from at least one homopolymer or copolymer compound from the group consisting of lignin, polyester, polyamide, polyurethane (PUR), polyurea, polyisocyanurate (PIR), and polycarbonate, and preferably at least one homopolymer or copolymer compound from the group consisting of polyurethane (PUR) and polyisocyanurate (PIR). Suitable starting materials are preferably at least one carbohydrate selected from polysaccharides (particularly preferably starch or cellulose, etc.), trisaccharides (e.g., kestose), C-6 monosaccharides (particularly preferably glucose, setose, or mannose, etc.), and C-5 monosaccharides (particularly preferably xylose or arabinose, etc.).

[0088] In one embodiment of step b), step b)i) is R 1 and R 2The invention involves providing at least one compound of formula (I), wherein each of the elements independently represents a hydrogen atom or a methyl group, preferably toluene and / or benzene. In a preferred embodiment, this at least one compound (particularly benzene and / or toluene) is obtained by thermal decomposition of the starting material at a temperature of 400°C to 1000°C. Thermal decomposition is understood by those skilled in the art to mean decomposition by heat under low oxygen conditions, where the absence of oxygen is required to avoid combustion of the organic material as much as possible. It is preferable that the gas phase contains less than 2% by volume of oxygen, particularly less than 1% by volume, during the thermal decomposition. Suitable thermal decomposition methods for obtaining xylene, toluene, and benzene are known to those skilled in the art, for example, from International Publication No. 2020 / 204707 and U.S. Patent No. 9,328,297.

[0089] In a particularly preferred embodiment of the thermal decomposition, this at least one compound is subjected to at least the following steps: A process of thermally decomposing an organic material at a temperature of 600°C to 1000°C to obtain a gaseous pyrolysis product and a pyrolysis residue, A step of contacting a gaseous pyrolysis product with a heterogeneous catalyst to obtain a conversion product containing at least one aromatic organic compound having a molecular weight of less than 300 g / mol, A step of post-processing the conversion product to obtain the above compound of formula (I), particularly toluene or benzene, It is provided as a process product of a process that includes the process.

[0090] The corresponding pyrolysis method for providing this information is described, for example, in International Publication No. 2020 / 204707, the contents of which, by reference, constitute a full and express part of this specification. This document also describes heterogeneous catalysts for producing conversion products suitable for this process. Examples of organic materials suitable for pyrolysis include polysaccharides, lignin, wood, plastic waste, or at least one homopolymer or copolymer compound from the group consisting of polyester, polyamide, polyurethane (PUR), polyurea, polyisocyanurate (PIR), and polycarbonate.

[0091] In a further embodiment of step b), step b)i) is R 1 and R 2 The present invention includes providing at least one compound of formula (I) above, where independently a hydrogen atom or a methyl group, particularly preferably toluene and / or benzene, where methane of biological origin is used as a starting material. The conversion of methane to aromatic hydrocarbons such as benzene is well known to those skilled in the art. Aromatic hydrocarbons, in particular benzene, are provided, for example, by contact and heat supply of methane and a catalyst in a fluidized bed reactor or a fixed bed reactor, where the catalyst is obtained by impregnating ZSM-5 (open-pore zeolite) as a support with 4 wt% molybdenum compound (B. Cook et al., Applied Catalysis A: General 365 (2009), 34-41). International Publication No. 2006 / 068814 also describes an optimized process in which the temperature required for the reaction is supplied to the process flow in an intervening heating section. In this embodiment, methane of biological origin can be used in the prior art process, as can the provision of aromatic hydrocarbons, in particular benzene.

[0092] In the embodiment of step b), formula R 1 and formula R 2 The compound of formula (I) above, in which each of the elements independently represents a hydrogen atom or a methyl group, can be used, for example, as a starting material to provide an oxidized aromatic organic compound as a process product of step b)ii-2).

[0093] R 1 Base or R 2If at least one of the groups represents a methyl group, the existing methyl group of the compound of formula (I) is oxidized in step b)ii-2) to yield a carboxyl group. This occurs, for example, at 100°C to 150°C in the presence of cobalt naphthalate and atmospheric oxygen. The resulting oxidized aromatic organic compound is decarboxylated by the removal of carbon dioxide according to step b)ii-3) to obtain phenol as a process product. The oxidation-decarboxylation reaction is carried out, for example, in a molten reactant (for example, at 230°C to 240°C in the presence of atmospheric oxygen, water vapor and copper(II) benzoate as a catalyst). The carbon dioxide obtained in the decarboxylation reaction in step b)ii-3) can be used, for example, preferably in step a) of the process according to the present invention, as a carbon dioxide source for providing methanol.

[0094] R according to the above formula (I) 1 and R 2 If both groups represent hydrogen atoms, phenol can be obtained by oxidation by introducing a ring-bonded hydroxyl group according to step b)ii-2). This can be done, for example, using oxygen, hydrogen peroxide, or N2O. This oxidation is preferably carried out by heating (for example, at 600°C to 800°C) using a catalyst such as zeolite (e.g., of type ZSM-5) or titanium silicate (TS-1). This direct oxidation of benzene represents a possible but unpreferred embodiment of step b)ii-2).

[0095] In a further, particularly preferred embodiment of step b), step b)i) is R 1 and R 2The present invention includes providing at least one compound (benzene) of formula (I) as described above, wherein represents hydrogen, where the benzene provided in this preferred embodiment is used as the organic aromatic compound in step b)ii-1), where steps a) and b) converge in this case, and as a result steps b)ii-1) and b)ii-3) become part of the oxidation step ii-3) from step a) of the present invention, where the propene provided in step a)ii-2) is reacted with the benzene from step b)i) to yield cumene, and then the cumene hydroperoxide method (Hock method) is carried out as oxidation to obtain acetone and phenol as the process products to be provided. Therefore, the preferred process is that in order to carry out step b)ii-1), the benzene provided in step b)i) is introduced into the oxidation of propene in step a)ii-3), where it is reacted with the propene provided from step a)ii-2) to yield cumene, and then the formed cumene is oxidized to provide phenol and acetone.

[0096] The cumene hydroperoxide method is well known and familiar to those skilled in the art, as described in various instruction manuals.

[0097] Therefore, the entire process according to this embodiment, which has convergence steps b)ii-1) and b)ii-3) and oxidation step ii-3) from step a), consists of at least the following steps: a) A step of providing propene which is a process product of a process including at least the following steps: i) At least the following steps: i-1) A step of obtaining methanol by conversion of CO, wherein CO is a process product of at least partial reduction from CO2 to CO and / or a process product of at least partial oxidation from an organic material to CO, wherein at least one organic material is selected from at least one organic solid compound, methane of biological origin, or a mixture thereof. A step of providing methanol, which is a process product of a process including, ii) From the methanol provided in advance, at least the following steps: ii-1) A step of converting a pre-provided methanol to obtain a product mixture containing dimethyl ether, water, and methanol, ii-2) A step of converting a starting material containing dimethyl ether, water, and methanol from the aforementioned product mixture into propene by contacting it with a catalyst and preferably at least one zeolite compound as a catalyst at a temperature exceeding 200°C, This involves the process of synthesizing propene, b) A step of providing acetone and phenol, which are process products of at least one manufacturing process comprising at least the following steps: i) At least one organoaromatic compound according to formula (I) [ka] (In the formula, R 1 and R 2 The process of providing benzene as (where represents a hydrogen atom), Here, benzene is a process product of the conversion of at least one starting material selected from the group consisting of high molecular weight organic compounds, carbohydrates, and methane of biological origin, and the process is as follows: ii) Processes ii-1), ii-2), and iii-3) ii-1) A step of reacting the benzene provided in step i) with the propene provided in step a)ii) to obtain a propan-2-yl substituted aromatic organic compound, particularly cumene, as a product, ii-2) A step of oxidizing the propan-2-yl substituted aromatic organic compound, particularly cumene, from step ii-1) to obtain at least one aromatic organic hydroperoxide compound, particularly cumene hydroperoxide, ii-3) A step of separating acetone as at least one carbon-containing substituent of the aromatic organic hydroperoxide compound from oxidation in step ii-2) to provide acetone and phenol, The process of carrying out the following: c) A step of reacting a mixture containing the provided acetone and the provided phenol to yield bisphenol A, This can be devised as a manufacturing process for bisphenol A for producing polycarbonate, including [the specified element].

[0098] Similarly, in carrying out step b)ii-3), without converging steps a) and b), it is also possible to convert such organic aromatic compounds of formula (I) provided in step b)i) into phenol via oxidation similar to the cumene hydroperoxide method, where R 1 is CHR 3 R 4 Represents the base of R 3 and R 4 R independently represents an (C1~C3)-alkyl group, or together with the residual molecule, forms an aliphatic hydrocarbon ring. 2 R independently represents hydrogen. In such embodiments, step b)i) of the process is R 1 The residue R 3 and residue R 4 The present invention provides a corresponding organic aromatic compound according to formula (I), which is independently selected from methyl, ethyl, and propyl, or which, together with the residual molecule, forms a six-membered aliphatic hydrocarbon ring, particularly cyclohexyl. In formula (I), the residue -CHR 3 R 4 R as 1 The process according to any of the preceding claims, characterized in that the substance is selected from propan-2-yl, sec-butyl, or cyclohexyl.

[0099] In a further embodiment of step b), step b)i) is R 1 The hydroxyl group is R 2 The present invention includes providing at least one compound of formula (I) (phenol) in which is hydrogen. This includes, in particular, providing phenol as a process product of a preferred microbiological process according to the present invention. The phenol provided is also particularly preferably a product of the following steps: A step of providing a recombinant host strain produced by a process in accordance with International Publication No. 2014 / 076113 (the contents of which, by reference, constitute the entirety and express part of this specification), The process involves incubating a recombinant host strain under fermentation conditions in the presence of at least one sugar as a starting material, It can be obtained as a product of a phenol production process in a recombinant host, including [the specified element].

[0100] Suitable sugars for this purpose are preferably polysaccharides such as disaccharides (e.g., sucrose) or trisaccharides (e.g., kestose), as well as C-6 monosaccharides (particularly glucose, cetose, or mannose) and C-5 monosaccharides (xylose, arabinose, etc.).

[0101] Suitable host strains are selected from representative examples of the group consisting of, for example, bacteria, yeasts, or fungi. Preferably, bacterial strains of Escherichia coli are suitable, with E. coli BW25113, E. coli DH10b, and E. coli LJ110 being particularly suitable. Similarly, bacterial strains of Pseudomonas putida, especially Pseudomonas putida S12, are also preferably suitable.

[0102] The recombinant host strain contains the necessary nucleic acid sequence as specified in International Publication No. 2014 / 076113.

[0103] Glucose can be converted to phenol, for example, by incubating sugars with a recombinant host.

[0104] In addition to the microbiological transformation of the starting materials, in a further embodiment of step b)i), phenol can be obtained from the transformation of lignin, a high-molecular-weight organic compound. This can be achieved, for example, by depolymerizing lignin at 400°C and a pressure of up to 300 bar in the presence of nitrogen or CO2 (see Zurbel et al., Chem. Ing. Tech., 2019, 4, 484-493), and then subsequently transforming the resulting alkylmethoxyphenol in the manner described, for example, by Huang et al. in ACS Catal. 2018, 8, 11184-11190.

[0105] In a further embodiment of step b), step b)i) is R 1 is a carboxyl group or carboxylate, and R 2 The present invention provides at least one compound of formula (I) in which is represented by a hydroxyl group (salicylic acid / salicylate) or hydrogen (benzoic acid / benzoate). In this embodiment, phenol is provided therefrom as a process product of the decarboxylation reaction according to steps b)ii-3). This decarboxylation reaction can be carried out, for example, as described above (see above).

[0106] The acetone provided in step a) and the phenol provided in step b) are mixed. The mixture containing the provided acetone and the provided phenol is reacted in step c) of the process according to the present invention to yield bisphenol A.

[0107] The reaction yielding bisphenol A is carried out according to a process known to those skilled in the art, for example, the process described in International Publication No. 00 / 35847, European Patent Application Publication No. 1728777, or U.S. Patent No. 2,775,620.

[0108] The reaction is preferably carried out at a temperature of 45°C to 110°C, particularly 50°C to 80°C, using at least one catalyst (particularly selected from hydrogen chloride, polystyrene sulfonates, and cross-linked polystyrene sulfonates).

[0109] In the reaction of mixtures, it is also preferable that the mixture used contains phenol and acetone in a molar ratio of phenol to acetone in the range of 2.1:1 to 15:1, particularly 5:1 to 12:1.

[0110] Particularly preferred is that the catalyst (in particular at least one polystyrene sulfonate compound) is localized on a fixed bed in the reaction zone of the reactor, where the fixed bed is brought into contact with the mixture to carry out the reaction.

[0111] It is highly preferable that the reaction of phenol with acetone in step c) is carried out in the presence of at least one sulfonated ion exchanger and at least one sulfur-containing co-catalyst to yield a bisphenol A-containing product mixture, which is then post-treated as necessary to obtain purified bisphenol A. Examples of acidic catalysts used include gel-like (microporous) or macroporous sulfonated crosslinked polystyrene resins (acidic ion exchangers), which may be in monodisperse or polydisperse (heterodisperse) form. The crosslinking agent used is usually divinylbenzene, but other crosslinking agents such as divinylbiphenyl may also be used. In addition to the catalyst, a co-catalyst is used. This is typically a thiol having at least one SH functional group and having a positive effect on both the selectivity and reactivity of the reaction. The co-catalyst may be uniformly dissolved in the reaction solution or immobilized on the catalyst itself. Examples of homogeneous co-catalysts include mercaptopropionic acid, hydrogen sulfide, alkyl sulfides, or alkylsilylthiols, such as ethyl sulfide or silylmethanethiol, and similar compounds. The immobilized co-catalysts are aminoalkylthiols and pyridylalkylthiols ionically bonded to the catalyst, where the SH functional group may be protected and exposed only during or after immobilization to the catalyst, for example, in the case of dimethylthiazolidine and alkylcarbamoylalkylthioesters. Similarly, the co-catalyst may be covalently bonded to the catalyst as an alkylthiol or arylthiol, or it may be a component of the catalyst. Two or more of the described co-catalysts may also be used together.

[0112] The bisphenol A obtained after the reaction is purified as described, for example, in European Patent Application Publication No. 1728777.

[0113] The process according to the present invention is illustrated as an example in Figure 1. The reference numerals in the figure have the following definitions: A = Organic materials (organic solid compounds and / or methane of biological origin) or CO2 B = Oxidizing agent (e.g., oxygen gas) or reducing agent (e.g., hydrogen gas or electric current) A product gas mixture containing C=CO D = Synthesis gas E=propene F = Bisphenol A G = Starting material consisting of at least high molecular weight organic compounds, carbohydrates, or biomethane. H = precursor according to equation (I), R 1 =hydroxyl group and R 2 = Not a hydrogen atom I = phenol CO provision through partial reduction of 1=CO2 or partial oxidation of organic materials Conversion of 2=CO to methanol Providing methanol from 3=2 4 = Conversion of methanol to propene E via the MTP process 5 = Oxidation of propene E to acetone 6 = Provision of acetone 7 = Synthesis of bisphenol A using provided acetone and provided phenol 8 = Provision of phenol 9 = Conversion of starting material G to phenol or its precursor by formula (I) Conversion of precursor H to phenol from 10=9

[0114] The arrows in Figures 1, 2, and 3 represent the flow of matter, energy, or heat between process steps / equipment components where the corresponding process steps are performed. The dashed lines represent process steps in a process that uses the materials provided in steps 6 and 8 as process products. The thick dots represent process gas treatment, including optional mixing equipment.

[0115] Figure 1 shows the manufacturing process for bisphenol AF for producing polycarbonate, comprising at least the following steps: a) A step of providing acetone which is a process product of a process including at least the following steps: i) At least the following steps: i-1) For example, a process for producing methanol by the conversion 2 of CO mixed with hydrogen as synthesis gas D, wherein the CO 3 provided therefor is a process product of at least partial reduction 1 of CO2A to CO by reducing agent B and / or a process product of at least partial oxidation 1 of an organic material to CO by oxidizing agent B, wherein at least one organic material A is selected from at least one organic solid compound, methane from biological origin, or a mixture thereof, A step 3 of providing methanol which is a process product of a process including ii) From the methanol 3 provided in advance, at least the following steps: A step 4 of providing propene as a product of a process including at least the following steps, ii-1) A step of converting the pre-provided methanol 3 to give a product mixture containing dimethyl ether, water, and methanol, ii-2) A step of converting a starting material containing dimethyl ether, water, and methanol in any case from the aforementioned product mixture to propene E by contacting it at a temperature above 200 °C with a catalyst, preferably at least one zeolite compound as the catalyst, ii-3) A step of converting propene E by at least oxidation 5 of propene E to acetone, And a step of synthesizing acetone thereby, Including, b) A step 8 of providing phenol which is a process product of at least one manufacturing process including at least the following steps, i) At least one organic aromatic compound according to formula (I)

Chemical formula

[0116] Bisphenol A obtained from step c) of the bisphenol A production process according to the first subject of the present invention or its embodiments, and post-treated as necessary, is suitable for the production of polycarbonate. Therefore, the second subject of the present invention comprises at least the following steps: A step of producing bisphenol A by the bisphenol A production process of the first subject of the present invention, A step of producing at least one carbonate derivative selected from phosgene, diester carbonate, or a mixture thereof, A step of reacting the above-mentioned carbonate derivative with at least one diphenol, wherein at least pre-prepared bisphenol A is used as the diphenol. This is a manufacturing process for polycarbonate, which includes [the specified material].

[0117] The production of bisphenol A is described in the first subject of the present invention. All embodiments of the first subject can also be used in the processes of the second subject of the present invention, depending on the priority of the individual process steps described therein.

[0118] The production of the carbonate derivative phosgene from at least carbon monoxide and chlorine is known, for example, from European Patent Application Publication No. 0881986, European Patent Application Publication No. 1640341, German Patent Application Publication No. 3327274, British Patent Application Publication No. 583477, International Publication No. 97 / 30932, International Publication No. 96 / 16898, or U.S. Patent No. 6,713,035. According to the present invention, it is found to be preferable to provide carbon monoxide (CO) for phosgene production by a process in which carbon monoxide is a process product of at least partial reduction from CO2 to CO and / or a process product of at least partial oxidation from an organic material to CO, wherein at least one organic material is selected from at least one organic solid compound, methane of biological origin, or a mixture thereof. A correspondingly appropriate and preferred embodiment of this provision of CO is similar to that described in step a)i-1) of the first subject matter of the present invention (see above).

[0119] The production of carbon dioxide derivatives, such as diester carbonates, is carried out, for example, by producing phosgene and subsequently reacting the phosgene with an organic monohydroxy compound, such as phenol, or by a catalytic reaction of phenol, carbon monoxide, and oxygen, as described in German Patent Application Publication No. 102009011874. According to the present invention, it is preferable to use diphenyl carbonate as the diester carbonate.

[0120] The production of polycarbonates is carried out by known processes using at least one diphenol (wherein at least bisphenol A produced in the above process is used as such a diphenol (hereinafter, diphenols are also called dihydroxyaryl compounds)), the carbonate derivative, and optionally a chain arrestor and optionally a branching agent. For the production of polyester carbonates, a portion of the carbonate derivative is replaced with an aromatic dicarboxylic acid or a derivative of a dicarboxylic acid, specifically with an aromatic dicarboxylic acid ester structural unit depending on the carbonate structural unit to be replaced in the aromatic polycarbonate.

[0121] In the case of homopolycarbonates, the process according to the second subject of the present invention uses only bisphenol A as the diphenol; however, when producing copolicarbonates, bisphenol A is used together with at least one additional diphenol. Preferably, the additional diphenol that can be used is selected from at least one diphenol from the group consisting of 4,4'-dihydroxydiphenyl, 1,1-bis(4-hydroxyphenyl)phenylethane, 2,2-bis(3,5-dimethyl-4-hydroxyphenyl)propane, 1,1-bis(4-hydroxyphenyl)cyclohexane, and 1,1-bis(4-hydroxyphenyl)-3,3,5-trimethylcyclohexane (bisphenol TMC (BPTMC)).

[0122] Aromatic dicarboxylic acids suitable for the production of polyester carbonates include orthophthalic acid, terephthalic acid, isophthalic acid, tert-butylisophthalic acid, 3,3'-diphenyldicarboxylic acid, 4,4'-diphenyldicarboxylic acid, 4,4-benzophenonedicarboxylic acid, 3,4'-benzophenonedicarboxylic acid, 4,4'-diphenyletherdicarboxylic acid, 4,4'-diphenylsulfonedicarboxylic acid, 2,2-bis(4-carboxyphenyl)propane, and trimethyl-3-phenylindan-4,5'-dicarboxylic acid.

[0123] Among aromatic dicarboxylic acids, terephthalic acid and / or isophthalic acid are particularly preferred.

[0124] Dicarboxylic acid derivatives include dicarbonyl dihalides and dialkyl dicarboxylates, particularly dicarbonyl dichlorides and dimethyl dicarboxylates.

[0125] The substitution of carbonate groups with aromatic dicarboxylic acid ester groups is substantially stoichiometric and quantitative, and therefore the molar ratio of the reactants is maintained in the final polyester carbonate. The aromatic dicarboxylic acid ester groups may be incorporated either randomly or in a blocky manner.

[0126] Those skilled in the art are aware of the process of reacting diphenol with the above-mentioned carbonate derivative.

[0127] Polycarbonates can be produced, for example, by transesterifying molten diphenyl carbonate and bisphenol A in a stirred reactor or screw extruder under slightly reduced pressure (e.g., 0.1 kPa to 20 kPa) at approximately 200°C to 350°C. The phenol is removed by distillation, and the polycarbonate is obtained in the form of strands, which are then pelletized or granulated (V. Serini "Polycarbonates" in: Ullmann's Encyclopedia of Industrial Chemistry, Wiley-VCH, Weinheim, 2000).

[0128] Polycarbonates can also be produced, for example, by reacting phosgene with at least bisphenol A as at least one diphenol. According to the present invention, this method is preferred. In a continuous interface process for producing polycarbonates known from European Patent Application Publication No. 0304691, an aqueous phase of diphenol(s) and the required amount of alkali metal hydroxide is mixed in a tube using a static mixer with an organic phase containing phosgene as the above-mentioned carbonate derivative. The phosgene excess is very high, from 20 mol% to 100 mol%, and the residence time in the reaction tube in the first reaction step is 10 to 75 seconds. This process can only be used to produce prepolymers having molecular weights of 4000 g / mol to 12000 g / mol. Further condensation reactions must be carried out using at least one catalyst to reach the desired molecular weight. Suitable catalysts are tertiary amines and onium salts. The use of tributylamine, triethylamine, and N-ethylpiperidine is preferred.

[0129] The amine catalyst used may be linear or cyclic, with triethylamine and N-ethylpiperidine being particularly preferred. The catalyst is preferably used as a solution of 1% to 55% by weight.

[0130] Here, onium salt is understood to mean compounds such as NR4X, where R can be an alkyl group and / or an aryl group and / or H, and X is an anion, such as a chloride ion, hydroxide ion, or phenoxide ion.

[0131] The reaction mixture, containing at least trace amounts (less than 2 ppm) of aryl chlorocarbonate, is precipitated and phase separation is performed. The alkaline aqueous phase (reaction wastewater) is removed, and the organic phase is extracted with dilute hydrochloric acid and water. The combined aqueous phase is sent to post-wastewater treatment, where the solvent and catalyst components are removed by stripping or extraction and recycled. Subsequently, after adjusting the pH to a specific level, for example, 6-8, by adding hydrochloric acid, any remaining organic impurities, such as monophenols and / or unconverted diphenols / multiple unconverted diphenols, are removed by treatment with activated carbon, and the aqueous phase is sent to chlorine-alkaline electrolysis.

[0132] In another variation of the post-treatment, the reaction wastewater is not combined with the washing phase, but is stripped or extracted to remove solvent and catalyst residues, then adjusted to a specific pH, for example, 6-8, by adding hydrochloric acid, and after any remaining organic impurities, such as monophenols and / or unconverted diphenols or multiple unconverted diphenols, are removed by treatment with activated carbon, it is sent to a chlorine-alkali electrolysis.

[0133] After removing the solvent and catalyst components by stripping or extraction, the washing phase may be returned to the synthesis as needed.

[0134] Phosgene may be used in liquid or gaseous form, or dissolved in an organic solvent.

[0135] After introducing phosgene, the organic phase and aqueous phase are mixed for a certain period of time, after which it may be advantageous to add a branching agent (if diphenolate is not added), a chain arrester, and a catalyst as needed. Such post-reaction time may be advantageous after any additions. These further stirring times, insofar as they are included, are 10 seconds to 60 minutes, preferably 30 seconds to 40 minutes, and particularly preferably 1 to 15 minutes.

[0136] Thus, all contaminants of any kind, whether alkaline, ionic, or catalytic, must be removed from the organic phase containing polycarbonate.

[0137] Even after one or more precipitation processes, assisted as necessary by passing through a sedimentation tank, agitator, coalescer, or separator, and / or a combination thereof (where water may be added as needed to each or some of the separation steps using an active or passive mixing device, depending on the circumstances), the organic phase still contains components of a fine droplet aqueous alkaline phase and a catalyst, which is generally a tertiary amine.

[0138] After this rough separation of the alkaline aqueous phase, the organic phase is washed once or twice with a dilute acid, mineral acid, carboxylic acid, hydroxycarboxylic acid, and / or sulfonic acid. Aqueous mineral acids, particularly hydrochloric acid, phosphorous acid, and phosphoric acid, or mixtures thereof are preferred. The concentration of these acids is preferably in the range of 0.001% to 50% by weight, more preferably 0.01% to 5% by weight.

[0139] Furthermore, the organic phase is subjected to repeated washing with demineralized water or distilled water. After each washing step, if necessary, the separation of a portion of the aqueous phase from the dispersed organic phase is carried out using a sedimentation tank, a stirring tank, a coalescer, a separator, and / or a combination thereof, where the washing water may be added during the washing steps using an active or passive mixing device as necessary.

[0140] During or after these washing steps, an acid may be optionally added, preferably dissolved in the solvent used for the polycarbonate solution. Hydrogen chloride gas and phosphoric acid or phosphorous acid are preferred, and these may be used as a mixture if necessary.

[0141] After the final separation operation, the purified polycarbonate solution thus obtained should preferably contain 5% by weight or less, preferably less than 1% by weight, and most preferably less than 0.5% by weight of water.

[0142] To isolate polycarbonates, the first step involves replacing a low-boiling solvent, such as methylene chloride, with a high-boiling solvent, such as chlorobenzene. This is done using an exchange column.

[0143] The isolation of polycarbonates from solutions containing high-boiling point solvents, such as chlorobenzene, can be performed by evaporation of the solvent using temperature, vacuum, or heated entrained gas.

[0144] When the concentration of a polycarbonate solution and, if necessary, the isolation of the polycarbonate are achieved by distillation of the solvent, and, if necessary, by superheating and reduced pressure, this is called a "flash process" (see also "Thermische Trennverfahren" [Thermal separation methods], VCH Verlagsanstalt 1988, page 114). On the other hand, when a heated carrier gas is sprayed together with the solution to be concentrated, this is called "spray evaporation / spray drying," as described, for example, in Vauck's "Grundoperationen chemischer Verfahrenstechnik", [Basic operations in chemical process engineering] Deutscher Verlag fuer Grundstoffindustrie 2000, 11th edition, page 690. All of these processes are described in patent literature and manuals and are well known to those skilled in the art.

[0145] Highly concentrated polycarbonate molten materials are obtained by removing the solvent by temperature (distillation) or by a technically more effective flash process. In known flash processes, the polycarbonate solution is repeatedly heated under slightly positive pressure to a temperature above its boiling point at atmospheric pressure, and these superheated solutions are then reduced to a lower pressure, such as atmospheric pressure. It may be advantageous to choose a two- to four-stage process rather than making the concentration stage, or in other words, the superheating temperature stage, excessively large.

[0146] To remove solvent residue from the highly concentrated polycarbonate molten product obtained in this manner, a vented extruder (Belgian Patent No. 866991, European Patent Publication No. 0411510, U.S. Patent No. 4980105, West German Patent Publication No. 3332065), a thin-film evaporator (European Patent Publication No. 0267025), a drip-film evaporator, a strand evaporator, or frictional compression (European Patent Publication No. 0460450) is used. In such cases, an entraining agent such as nitrogen or carbon dioxide may be added as needed, or a vacuum may be used (European Patent Application Publication No. 003996, European Patent Application Publication No. 0256003, U.S. Patent No. 4423207). Alternatively, it can also be directly removed from the molten material by subsequent crystallization (West German Patent Application Publication No. 3429960) and bake-out of solvent residue in the solid phase (U.S. Patent No. 3986269, West German Patent Application Publication No. 2053876).

[0147] Granules can be obtained, where possible, by directly spinning the molten material and then granulating it, or by using a discharge extruder and spinning it from there in air or liquid, usually water. When using an extruder, the molten material can be mixed with additives upstream of the extruder, either using a static mixer as needed, or via a lateral extruder within the extruder.

[0148] Adding additives to polycarbonate / polycarbonate compounds can help extend the service life or color (stabilizers), simplify processing (e.g., mold release agents, flow aids, antistatic agents), or adapt the properties of the resulting polycarbonate material to specific loads (impact modifiers such as rubber, flame retardants, colorants, glass fibers).

[0149] The third subject of this invention is, i) A volume filled with acetone, which is the process product of step a) of the first subject of the present invention, ii) A volume filled with phenol, which is the process product of step b) of the first subject of the present invention, iii) At least one reactor for the production of bisphenol A, comprising at least one inlet for acetone and at least one inlet for phenol, wherein the inlet for acetone is fluid-connected to the volume of acetone and the inlet for phenol is fluid-connected to the volume of phenol, This is a multi-component system for the production of bisphenol A by the aforementioned manufacturing process, comprising the first subject of the present invention.

[0150] A "fluid connection" is a part of a multi-component system that connects the other parts of the system to each other, allowing matter to be transported from one part to the next as a material flow, regardless of its state. A supply conduit in the form of a pipe is an example of this. The expression "fluidly connected" means that designated parts of a multi-component system are connected to each other via a fluid connection.

[0151] The "acetone-filled volume" in the multicomponent system may be, for example, the volume of a storage container or the volume of a pipeline. If the volume is a storage container, in a further embodiment, it is preferable that the multicomponent system additionally includes at least one discharge device for a movable, sealed transport container fluidly connected to the acetone inlet of the reactor for producing bisphenol A.

[0152] For delivery, acetone is preferably supplied in a movable, sealed transport container as a process product in the context of step a) of the process according to the present invention, and is transferred therefrom to a storage container for temporary storage as needed. The movable, sealed transport container may be, for example, a tanker wagon, a tanker ship, or a tanker truck. "Sealed" means that the transport container is sealed in its equipment for loading or unloading the transported material during transport.

[0153] According to the present invention, a storage container is a container located in a fixed place, such as a tank farm. The storage container is part of or part of the capacity of the fixed facility.

[0154] For delivery, the phenol is preferably supplied in a mobile, sealed transport container as a process product in the context of step b) of the process according to the present invention, and, if necessary, transferred therefrom to a storage container for temporary storage. The mobile, sealed transport container may be, for example, a tanker wagon, a tanker ship, or a tanker truck. "Sealed" means that the transport container is sealed in its equipment for loading or unloading the transported material during transport.

[0155] All embodiments of step a) of the bisphenol A production process according to the present invention are also applicable to multi-component systems.

[0156] All embodiments of step b) of the bisphenol A production process according to the present invention are also applicable to multi-component systems.

[0157] A further subject is the use of a mixture containing acetone as a product of a process comprising at least steps a)i) and a)ii) described in the first subject of the present invention, and containing phenol as a product of a process comprising at least steps b)i) and b)ii) described in the first subject of the present invention, for the production of bisphenol A.

[0158] All embodiments of step a) of the bisphenol A manufacturing process according to the present invention shall also apply mutatis mutandis to this use.

[0159] All embodiments of step b) of the bisphenol A manufacturing process according to the present invention also apply mutatis mutandis to this use.

[0160] The following examples are provided as illustrations of the present invention and do not limit the present invention to the disclosures of the examples. [Examples]

[0161] Figures 2 and 3 show exemplary embodiments of the process according to the present invention.

[0162] Example 1: Figure 2 shows an embodiment of the process according to the present invention. The reference numerals in the figure have the following definitions: A1=CO2 B1 = Hydrogen gas as a product of water electrolysis A product gas mixture containing C=CO D = Synthesis gas E=propene F = Bisphenol A G1 = Plastic waste as high-molecular organic compounds H1 = benzene as a precursor according to equation (I), R 1 =hydroxyl group and R 2 = Not a hydrogen atom H2 = Cumene hydroperoxide as an oxidized aromatic compound I = phenol J = gaseous pyrolysis product 1a=CO provision by RWGS 2=CO and conversion of hydrogen gas B1 to methanol Providing methanol from 3=2 4 = Conversion of methanol to propene by the MTP process 5 = Oxidation of propene E to acetone 6 = Provision of acetone 7 = Synthesis of bisphenol A using provided acetone and provided phenol 8 = Provision of phenol 9 = Conversion of starting material G1 to benzene as precursor H1 9a = Thermal decomposition for the conversion of starting material G1 into gaseous pyrolysis products. 9b = Catalytic conversion of gaseous pyrolysis products Conversion of the precursor from 10a=9a to cumene hydroperoxide 10b = Conversion of cumene hydroperoxide to acetone and phenol 11 = Electrolysis of water using electric current from renewable energy sources

[0163] The synthesis of bisphenol AF 7 is carried out after the provision of acetone 6. The provided acetone is necessarily the product of a process in which acetone is produced as an intermediate via the provided methanol 3. At least carbon monoxide in the carbon monoxide-containing product gas stream C is necessarily obtained in the reverse water-gas shift reaction 1a (RWGS) by reducing carbon dioxide A1 with hydrogen gas B1 obtained from water electrolysis 11. The synthesis gas D obtained after the purification of carbon monoxide from the product gas stream C carried out in process gas treatment (points in Figure 2) and the addition of hydrogen gas B1 is converted to methanol, which methanol is further converted to propene E in the MTP process 4, where propene E for oxidation 5 is first converted to cumene using benzene as a precursor H1, the resulting propane-2-yl residue after oxidation at the 2 position of cumene is converted to the 2-hydroperoxypropane-2-yl residue of cumene hydroperoxide H2 10a, and then converted to acetone 10b by oxidative elimination.

[0164] The synthesis of bisphenol AF 7 is carried out similarly after the provision of phenol 8. The provided phenol is necessarily the product of the process in which phenol is produced from benzene as a precursor H1, where benzene is also the product of the catalytic conversion 9b of gaseous pyrolysis product J from the pyrolysis 9a of a polymeric organic compound G1 in the form of plastic waste. The benzene for the provided phenol is first converted to cumene hydroperoxide 10a in oxidation 5 of propene as described above, and then converted to phenol 10b in oxidative elimination.

[0165] Example 2: Figure 3 shows an embodiment of the process according to the present invention. Unless otherwise specified below, the reference numerals in the figure are as defined in Example 1: A1 = Plastic waste as an organic solid compound B2 = Oxygen-containing gas (e.g., O2 as a product of water electrolysis 11) 1b = CO donation through partial oxidation

[0166] The synthesis of bisphenol AF 7 is carried out after the provision of acetone 6. The provided acetone is necessarily the product of a process in which acetone is produced as an intermediate via the provided methanol 3. At least carbon monoxide in the carbon monoxide-containing product gas stream C is necessarily obtained by the partial oxidation 1b of plastic waste A1 with oxygen gas B2 obtained from water electrolysis 11, and the synthesis gas D obtained after the purification of carbon monoxide from the product gas stream C carried out in process gas treatment (point in Figure 2) and the addition of hydrogen gas B1 is converted to methanol, which methanol is further converted to propene E in the MTP process 4, where propene E for oxidation 5 of propene is first converted to cumene using benzene as a precursor H1, the resulting propane-2-yl residue after oxidation at the 2 position of cumene is converted to the 2-hydroperoxypropane-2-yl residue of cumene hydroperoxide H2 10a, and then converted to acetone 10b by oxidative elimination.

[0167] The synthesis of bisphenol AF 7 is carried out similarly after the provision of phenol 8. The provided phenol is necessarily the product of a process in which phenol is produced with benzene as the precursor H1, where benzene is the product of catalytic conversion 9b of a gaseous pyrolysis product J from the pyrolysis 9a of a polymeric organic compound G1 in the form of plastic waste. The benzene for the provided phenol is first converted to cumene hydroperoxide 10a in oxidation 5 of propene as described above, and then converted to phenol 10b in oxidative elimination.

Claims

1. A process for producing bisphenol A(F) for the manufacture of polycarbonate, comprising at least the following steps: a) A step (4) of providing acetone, which is a process product of a process including at least the following steps: i) At least the following steps: i-1) A step of obtaining methanol by conversion of CO (2), wherein the CO is CO ２ Process products of at least partial reduction (1) from to CO, and / or process products of at least partial oxidation (1) from an organic material to CO, wherein at least one organic material (A) is selected from at least one organic solid compound, methane from a biological origin, or a mixture thereof, (3) A step of providing methanol, which is a process product of a process including, ii) From the previously provided methanol (3), at least the following steps: A step (4) of providing propene as a product of a process including at least the following steps, ii-1) A step of converting the previously provided methanol (3) to obtain a product mixture containing dimethyl ether, water, and methanol, ii-2) A step of converting a starting material containing dimethyl ether, water, and methanol from the product mixture into propene (E) by contacting it with a catalyst and preferably at least one zeolite compound as a catalyst at a temperature exceeding 200°C, ii-3) A step of converting the propene (E) by oxidation (5) of the propene (E) to acetone, The process of synthesizing acetone by, Processes including, b) A step (8) providing phenol which is a process product of at least one manufacturing method comprising at least the following steps: i) At least one organic aromatic compound according to formula (I) 【Chemistry 1】 (In the formula, R １ is a hydrogen atom, a hydroxyl group, methyl, carboxyl, carboxylate, or -CHR ３ R ４ This represents, and here, R ３ and R ４ (C １ ~C ３ ) - Represents an alkyl group, or forms an aliphatic hydrocarbon ring with the residual molecule, R ２ represents a hydrogen atom, methyl, carboxyl, or carboxylate, provided that when R １ represents -CHR ３ R ４ in which case R ２ represents a hydrogen atom, and when R １ represents a hydroxyl group, R ２ represents a hydrogen atom, carboxyl or carboxylate, Here, the process provides an organic aromatic compound which is a process product of the transformation (9) of at least one starting material selected from the group consisting of polymeric organic compounds, carbohydrates, and methane of biological origin. In the organic aromatic compound from step i) according to formula (I), R １ does not represent a hydroxyl group, R ２ If does not represent a hydrogen atom, ii) Steps ii-1) and / or ii-2) and / or iii-3) ii-1) A step of reacting the organic aromatic compound (H) from step i) with propene to obtain a propane-2-yl substituted aromatic organic compound as a product; ii-2) A step of oxidizing the organic aromatic compound (H) from step i) and / or the product from step ii-1) to obtain at least one oxidized aromatic organic compound; ii-3) A step of removing at least one carbon-containing substituent from the organic aromatic compound (H) from step i) and / or from the oxidation by step ii-2); At least one of the following steps, Processes including, c) A step of carrying out a reaction (7) of a mixture containing the provided acetone and the provided phenol to obtain bisphenol A(F), A process that includes this.

2. The CO used in the reaction (2) by step a) i-1) is at least CO ｘ The process according to claim 1, characterized in that the process product is the at least partial reduction of a gas stream containing (wherein x = 1 or 2) and optionally hydrogen gas (B).

3. In step a) i-1), the CO is, in particular, H provided by electrolysis. ２ From the reverse water-gas shift reaction using (B), CO ２ From the electrochemical reduction of CO to CO, or a combination thereof, selected from CO ２ The process according to claim 1 or 2, characterized in that the process product is at least a partial reduction of to CO.

4. In step a) i-1), the CO is provided by electrolysis. ２ (B) is a process product of at least one reverse water-gas shift reaction, or CO ２ The process according to any one of claims 1 to 3, provided by the electrochemical reduction of to CO, or a combination thereof, wherein electrical energy generated from renewable energy is used.

5. The process according to any one of claims 1 to 4, characterized in that the conversion of methanol in step a) ii-1) is carried out by contacting methanol, preferably methanol in the gas phase, with a catalyst.

6. The process according to any one of claims 1 to 5, characterized in that, in step a) ii-1), the methanol provided has a temperature in the range of 200°C to 350°C.

7. The process according to any one of claims 1 to 6, characterized in that the conversion of the starting material by step a) ii-2) is carried out at a temperature of 350°C to 600°C, particularly 380°C to 550°C.

8. In step a) ii-3), the oxidation (5) of propene (E) is carried out by the following method: 1) A method of producing acetone by the reaction of propene(E) with water using a catalyst system composed of palladium(II) chloride and copper(II) chloride, according to the Wacker-Hoechst process; 2) A method of hydroxylating propene(E) with water to obtain 2-propanol, followed by catalytic dehydrogenation of 2-propanol to obtain acetone; 3) A method of obtaining acetone in each case by converting propene(E) to cumene and carrying out the cumene hydroperoxide method, or by converting propene(E) to diisopropylbenzene and carrying out the cumene hydroperoxide method using diisopropylbenzene hydroperoxide instead of cumene hydroperoxide; The process according to any one of claims 1 to 7, characterized in that it is carried out according to at least one of the following.

9. In formula (I), residue R ３ and residue R ４ The process according to any one of claims 1 to 8, characterized in that the molecule is independently selected from methyl, ethyl, and propyl, or together with the residual molecule, forms a six-membered aliphatic hydrocarbon ring, particularly a cyclohexyl molecule.

10. In formula (I), residue-CHR ３ R ４ The process according to any one of claims 1 to 9, characterized in that the selection is made from propan-2-yl, sec-butyl, or cyclohexyl.

11. The process according to any one of claims 1 to 10, characterized in that the starting material in step b) i) is at least one compound selected from the group consisting of polysaccharides, trisaccharides, C-6 monosaccharides, C-5 monosaccharides, methane of biological origin, and homopolymer and copolymer compounds from the group consisting of cellulose, lignin, polyester, polyamide, polyurethane (PUR), polyurea, polyisocyanurate (PIR), and polycarbonate.

12. The process according to any one of claims 1 to 11, characterized in that step b)i) includes providing benzene as the organic aromatic compound, introducing the benzene into the oxidation (5) of propene (E) in step a)iii-3), where it reacts with the propene (E) provided from step a)iii-2) to yield cumene, and then oxidizing the formed cumene to yield phenol and acetone.

13. The process according to any one of claims 1 to 12, characterized in that step b)i) includes providing the organic aromatic compound, in particular toluene and / or benzene, by thermal decomposition of the starting material at a temperature of 400°C to 1000°C.

14. At least the following steps: A step of producing bisphenol A, which is a process product of the process described in any one of claims 1 to 13, A step of producing at least one carbonate derivative selected from phosgene, diester carbonate, or a mixture thereof, A step of reacting the carbon dioxide derivative with at least one diphenol, wherein at least pre-prepared bisphenol A is used as the diphenol. The manufacturing process for polycarbonate, including [the specified component].

15. The production of the aforementioned carbonate derivative is carried out using H as a process product of water electrolysis. ２ From RWGS using CO ２ The process according to claim 14, characterized by providing carbon monoxide as a starting material, which is at least one process product selected from electrochemical reduction from to CO, or a combination thereof.

16. i) a volume filled with acetone which is the process product of step a) of the process according to any one of claims 1 to 13, ii) A volume filled with phenol, which is the process product of step b) of the process according to any one of claims 1 to 13, iii) At least one reactor for the production of bisphenol A, comprising at least one inlet for acetone and at least one inlet for phenol, wherein the inlet for acetone is fluid-connected to the volume of acetone and the inlet for phenol is fluid-connected to the volume of phenol, A multi-component system for producing bisphenol A by the manufacturing process described in claims 1 to 13, comprising the above.

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