EP3997257A1 - Procédé d'électro-dicarboxylation d'au moins un alcène avec du dioxyde de carbone co2 en présence d'hydrogène h2 - Google Patents

Procédé d'électro-dicarboxylation d'au moins un alcène avec du dioxyde de carbone co2 en présence d'hydrogène h2

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Publication number
EP3997257A1
EP3997257A1 EP20749813.0A EP20749813A EP3997257A1 EP 3997257 A1 EP3997257 A1 EP 3997257A1 EP 20749813 A EP20749813 A EP 20749813A EP 3997257 A1 EP3997257 A1 EP 3997257A1
Authority
EP
European Patent Office
Prior art keywords
reactor
mpa
anode
hydrogen
cathode
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
EP20749813.0A
Other languages
German (de)
English (en)
Inventor
Maximilian NEUMANN
Reinhard SCHOMÄCKER
Peter Strasser
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Technische Universitaet Berlin
Original Assignee
Technische Universitaet Berlin
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Technische Universitaet Berlin filed Critical Technische Universitaet Berlin
Publication of EP3997257A1 publication Critical patent/EP3997257A1/fr
Pending legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B3/00—Electrolytic production of organic compounds
    • C25B3/20—Processes
    • C25B3/25—Reduction
    • C25B3/26—Reduction of carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B11/00—Electrodes; Manufacture thereof not otherwise provided for
    • C25B11/02—Electrodes; Manufacture thereof not otherwise provided for characterised by shape or form
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B3/00—Electrolytic production of organic compounds
    • C25B3/01—Products
    • C25B3/07—Oxygen containing compounds
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B3/00—Electrolytic production of organic compounds
    • C25B3/20—Processes
    • C25B3/25—Reduction
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B3/00—Electrolytic production of organic compounds
    • C25B3/20—Processes
    • C25B3/29—Coupling reactions
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/17—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof
    • C25B9/19—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms

Definitions

  • the present invention relates to a process for the electrodicarboxylation of at least one alkene, in particular at least one diene, with carbon dioxide CO 2 in the presence of hydrogen H 2 and a reactor for carrying out such a process.
  • adipic acid is a starting material for the large-scale production of polyamide 6.6 (nylon) and is produced industrially via the partial oxidation of "KA-Oil" in the order of 2.5 million tons per year.
  • the by-product inherent in production is nitrous oxide Greenhouse gas with 298 times the global warming potential of CO 2.
  • the stoichiometric use of nitric acid is necessary, the production of which is subject, for example, to the energy-intensive Ostwald process.
  • KA-Oil for its part, is represented by the partial oxidation of cyclohexanone and cyclohexanol of fossil origin.
  • a difficulty This is due to the low conversion (4-1 1%) with a single pass through the reactor, which means that recycling and adipic acid production steps are necessary.
  • a counter reaction is required which releases the required electrons.
  • a sacrificial component which for this purpose has to be oxidized stoichiometrically.
  • Aluminum, zinc or a redox system for example, are used as sacrificial components or materials, which are either reduced in a tandem process or then separated and recovered.
  • the product phase after the reaction contains the target substance hex-3-endioic acid (dihydromuconic acid) in the form of a sacrificial anode salt (product 1. in scheme). It is extremely time-consuming and difficult to separate the product fraction or to develop a method for technical implementation for this purpose, which is contrary to technical implementation and is particularly due to the sacrificial anode salt.
  • a method for the electrodicarboxylation of at least one diene with carbon dioxide CO 2 in the presence of hydrogen H 2 with the formation of at least one unsaturated dicarboxylic acid comprising at least one cathode as a working electrode for the cathodic activation of CO 2 , at least one Anode is carried out as a counter electrode for anodic oxidation of H 2 and, if necessary, at least one reference electrode.
  • a total pressure p g in the reactor between 2 and 4 MPa, preferably between 3 and 4 MPa, for example 3.4 MPa, 3.5 MPa, and 3.7 MPa
  • a mean current density j between 5 and 15 mA / cm 2 , preferably between 10 and 12.5 mA / cm 2 .
  • the present process optimizes the anode, using hydrogen H 2 as an anode reaction (counter reaction), which greatly simplifies any technical process.
  • the following scheme 2 summarizes the reaction using the example of the dicarboxylation of 1,3-butadiene:
  • the dicarboxylation can be followed by the conversion of the unsaturated dicarboxylic acid to the saturated dicarboxylic acid, such as, for example, hex-3-enedioic acid to form the target substance adipic acid, by means of an either homogeneous or heterogeneously catalyzed hydrogenation.
  • an either standard catalysts such as a platinum metal on activated carbon, silica or titanium dioxide or the very well-known Wilkinson catalyst can be used under suitable reaction conditions. It has been shown that this first requires a separation of the electrolyte from the electrodicarboxylation (1.). Separation of the hydrogenation catalyst, the hydrogenation medium and any by-products from the dicarboxylation that may still be present is then necessary down to the adipic acid.
  • the present method has various advantages over the previously known approaches.
  • the use of anodic sacrificial materials or sacrificial electrodes can thus be dispensed with. This in turn leads to the avoidance of the use of aluminum and the production of product aluminum salts which are difficult to purify, which leads to various cost savings in a corresponding process.
  • the savings relate to the omission of aluminum as a component with high specific costs, the avoidance of the process steps of the described separation of the aluminum product salt, as well as the avoidance of constant maintenance of the reactor, which would be justified by replacing used sacrificial electrodes.
  • the purification steps for an industrial process to be developed are greatly simplified. In addition, there is a higher conversion of the diene to the corresponding dicarboxylic acid, while at the same time the formation of by-products, in particular of monocarboxylic acids, is reduced.
  • Grinberg et al. Electrochemical reduction of CO 2 in the presence of 1, 3-butadiene using a hydrogen anode in a non-aqueous medium; Russian Chemical Bulletin, 1999, 48 (2), 294-299)
  • Gas diffusion electrodes (GDE) used at only low overpressures , a GDE is dispensed with according to the present procedure and the total pressure is increased. A gas mixture is used.
  • Grinberg et al. a lower Faraday efficiency.
  • the hydrogen H 2 with a partial pressure p 0, H2 is between 0.75 and 2 MPa, preferably between 1 and 1.5 MPa, particularly preferably between 1.1 and 1.4 MPa, for example 1.25 MPa in the reactor.
  • the carbon dioxide CO 2 is present in the reactor with a partial pressure p 0, CO 2 between 2 and 4 MPa, particularly preferably between 3 and 4 MPa, for example 3.75 MPa.
  • the at least one diene is metered into the reactor in liquid form.
  • the concentration of the diene metered in can be 1-5 mol / l, preferably 1.5-3 mol / l, particularly preferably 1.5-2 mol / l.
  • liquid butadiene can be introduced into the reactor at a concentration of 1.62 mol / l.
  • a diene is to be understood as a collective term for a group of substances in which at least two double bonds occur conjugated or also isolated.
  • the at least one diene can be a linear conjugated diene, linear conjugated dienes including, for example, 1,3-butadiene, pentadiene, hexadiene, 1,3,5-hexatriene, cyclohexadiene.
  • dienes can include, for example, linear dienes with non-conjugated double bonds.
  • Dienes can, for example, have at least one terminal double bond, for example a, w-dienes such as 1,7-octadiene (OD), 1,9-decadiene, 1,1-dodecadienes, 1,13-tetradecadienes.
  • OD 1,7-octadiene
  • 1,9-decadiene 1,1-dodecadienes
  • 1,13-tetradecadienes 1,13-tetradecadienes.
  • the stated process parameters for the present electrodicarboxylation enable an increase in the Faraday efficiency.
  • the Faraday efficiency shows what proportion of the total flow stoichiometrically allotted to the desired products or by-products, e.g. "Faraday efficiency with regard to component X".
  • a Faraday efficiency FE EC can be achieved for the sum of all dicarboxylation products that is between 10-55%, preferably 15-30%, particularly preferably between 20-25%.
  • the Faraday efficiency depends on which electrode geometry, partial pressures, butadiene concentrations were selected and whether a mediator is used, as will be explained further below.
  • Mediator denotes an additional component from the class of organometallic compounds that is added to the reaction and which can influence the Faraday efficiency in an unknown manner.
  • the Faraday efficiency FE EC for the sum of all dicarboxylation products that can be used to produce linear, unbranched dicarboxylic acids is between 5-30%, preferably between 10-25%, particularly preferably between 15-20%, e.g. 13.3% or 26 , 2%.
  • the reaction is carried out in a dried, organic solvent containing at least one conductive salt.
  • the organic solvent is selected from dimethylformamide (DMF); Dimethyl propylene urea (DMPU) and N-methyl-2-pyrrolidone (NMP); DMF is preferred.
  • the at least one conductive salt is an alkylammonium bromide, preferably t-n-butylammonium bromide (TBAB).
  • the electrodicarboxylation is carried out in the presence of a mediator.
  • the component known as the mediator is an organometallic compound, for example a transition metal complex.
  • the effect on the reaction was surprisingly found to be given, but was not foreseeable.
  • Mediators are commonly found in electrochemistry in general, but are very specific for certain reactions and can only be generalized for similar reactions in rare cases.
  • the mediator is preferably a transition metal complex, in particular a Rh, Pt, Pd, Ru or Fe complex.
  • Particularly preferred mediators are platinum metal complexes with phosphane ligands (eg Xanthphios) and ferrocene.
  • mediators leads to a reduction in the electropolymerization tendency and an increase in the Faraday efficiency.
  • Any mediator applied preferably does not have any function in the sense of a catalyst in the reaction itself, but can reduce the macroscopic polymerization tendency of 1,3-butadiene and influence the efficiency of the electrodicarboxylation.
  • the dicarboxylation can be followed by the conversion of the unsaturated dicarboxylic acid to the saturated dicarboxylic acid.
  • This can be done by means of a homogeneous or heterogeneously catalyzed hydrogenation using known catalysts, such as platinum metal on a suitable support or a homogeneous catalyst complex, such as a platinum metal in the form of a metal-phosphine complex, e.g. the Wilkinson catalyst under suitable reaction conditions.
  • the method is carried out in a reactor which has at least one cathode as a working electrode for the cathodic activation of CO 2 , at least one anode as a counter electrode for the anodic oxidation of H 2 and at least one reference electrode.
  • the anode and cathode are arranged parallel to one another.
  • the anode and cathode are arranged concentrically to one another.
  • the anode is arranged concentrically around the cathode; i.e. the cathode can for example be arranged in the middle of an annular anode and consist for example of a narrow, polished nickel sheet.
  • electrocarboxylation selectivity relate to the subset of the dicarboxylic acids based on the total amount of electrocarboxylation products generated.
  • the anode can consist of a platinum metal, an alloy of at least one platinum metal or a platinum-plated or platinum-coated foreign metal carrier. It Platinum was preferably used here and can be in the form of a helix, a mesh, a fabric, immobilized platinum particles on a suitable carrier or a sheet, for example a flat, flat or concentrically shaped sheet.
  • the anode material platinum is largely inert and does not contaminate the system described.
  • the cathode consists of graphite, a transition metal, preferably a platinum metal, preferably nickel, and can be in the form of a flat sheet.
  • the cathode material is preferably subjected to a pretreatment of consecutive grinding, polishing, washing and drying steps.
  • the anode and cathode compartment can either be divided (e.g. by a membrane) or preferably undivided.
  • anode compartment and cathode compartment are separated from one another, in particular by means of a membrane, e.g.
  • Figure 1 is a schematic view of a first embodiment of a
  • Electrode arrangement (parallel arrangement);
  • Figure 2 is a schematic view of a second embodiment of a
  • Electrode arrangement (concentric arrangement).
  • the apparatus arrangement used comprises a pressure-stable stirred tank with the built-in electrodes, a 1,3-butadiene metering system and a gas mixing system.
  • the pressure reactor used contains an inert inley, internals and the electrode arrangement. Convective mixing took place by means of a magnetically coupled stirrer below the cathode at a constant distance.
  • An insert made of PTFE (Teflon) and a cover made of PEEK with corresponding through-holes for the supply lines and electrodes enable the functional elements to be electrically isolated as far as possible.
  • the arrangement of Inley, internals and electrodes was placed in the described PTFE insert during the reaction and the reactor was completely closed. Electrically insulated contacts then enable a voltage to be applied to the electrodes through the pressure-resistant stainless steel jacket.
  • the reactor was then subjected to the corresponding target pressure from a prepared CO 2 / H2 mixture.
  • the reaction medium an aprotic, anhydrous organic solvent with a conductive salt soluble in it, was added via a metering system which comprises a high-pressure pump, an expansion unit and a mixer. The precise metering in of a specific amount of 1,3-butadiene takes place during this.
  • the reactor was slowly depressurized using an automated standard procedure and the reaction chamber was flushed with a slight positive pressure of nitrogen for about one hour in order to safely remove the escaping 1,3-butadiene.
  • the reaction mass removed was concentrated and evaporated to dryness.
  • the product composition was then determined by GC / MS. A consistency check was carried out using several individual samples from a reaction run, multiple determination of the samples, as well as a separate analysis of the total amount of coupling products by HPLC / DAD / ELSD (high performance liquid chromatography with diode grid detector and evaporative light scattering detector, high performance liquid chromatography (HPLC), diode array detector (DAD), Evaporative light scattering detector (ELSD)).
  • HPLC / DAD / ELSD high performance liquid chromatography with diode grid detector and evaporative light scattering detector, high performance liquid chromatography (HPLC), diode array detector (DAD), Evaporative light scattering detector (ELSD)
  • the organic solvent to be used was dehydrated using a drying agent such as phosphorus pentoxide or sodium hydride and vacuum distilled.
  • the dried solvent was poured onto predried conductive salt under an argon atmosphere and stored over a freshly heated molecular sieve (4A).
  • DMF dimethylformamide
  • DMPU dimethylpropylenurea
  • NMP N-methyl-2-pyrrolidone
  • TBAB Tetra-n-butylammonium bromide
  • Electrode either a platinum coil or a platinum sheet served as the counter electrode, which was first cleaned and then shaped.
  • all electrodes were electrically insulated with Teflon sleeves at the points not to be exposed to the electrolyte.
  • the Teflon reactor insert was rinsed with aqua regia, thoroughly cleaned and then dried.
  • the working and counter electrodes were pretreated as described and inserted into the reactor.
  • the reference electrode bridge (Luggin capillary) was prepared and filled with electrolyte, then inserted into the reactor insert and the reactor then closed. After checking the contacts for short circuits or insufficient electrical resistance, the reactor was filled with a specific amount of electrolyte solution and 1,3-butadiene via the metering system. The total volume of electrolyte and 1,3-butadiene in each experiment was 28.00 ml.
  • a gas mixture of hydrogen and carbon dioxide in the composition to be achieved was prepared in a pressure-stable storage container (500 ml).
  • FIGS. 1 and 2 The electrode arrangements used for this are shown in FIGS. 1 and 2.
  • Figure 1 shows a parallel arrangement with Pt coil 1 as anode, polished Ni sheet 2 as cathode, Luggin capillary with frit 3, and silver-silver bromide electrode 4.
  • Figure 2 shows a concentric arrangement with Pt sheet 1 as anode , polished Ni sheet metal 2 as cathode, Luggin capillary with frit 3, and Ag / Ag + electrode 4.
  • the additives (mediators) used can significantly increase the Faraday efficiencies.
  • the additives (mediators) used can significantly increase the Faraday efficiencies.
  • ferrocene up to 51.8%, when using PdCl2 in conjunction with Xantphos from 29.5%.
  • a reduction in the polymerisation tendency of 1,3-butadiene is surprisingly observed.
  • the inhibitory effect on the polymerization of RhCl3 in connection with Xantphos and PdCl2 in connection with Xantphos are comparable (TOC), but the latter shows the overall higher Faraday efficiency.
  • the product spectrum of the reaction runs comprises a number of different dicarboxylation products and is listed in Table 2.
  • Table 2 Analysis of the product phase The results given in Table 2 show that a higher CO 2 partial pressure is necessary in order to achieve the very limited Faraday efficiency of the electrodicarboxylation of Grinberg et al. to increase significantly (from 3.8% to 20%).
  • Examples 1 and 2 were given for this purpose.
  • the formation of branched products was found to be increased when a parallel arrangement was used.
  • a concentric electrode arrangement greatly reduced the formation of the undesired methyl pentenedioic acid derivative.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
  • Electrodes For Compound Or Non-Metal Manufacture (AREA)

Abstract

La présente invention concerne un procédé d'électro-dicarboxylation d'au moins un diène avec du dioxyde de carbone CO2 en présence d'hydrogène H2, avec la formation d'au moins un acide dicarboxylique insaturé, la réaction étant réalisée dans un réacteur comprenant au moins une cathode comme électrode de travail pour l'activation cathodique de CO2, au moins une anode comme contre-électrode pour l'oxydation anodique de H2, avec un rapport volumétrique hydrogène H2 à dioxyde de carbone CO2 entre 1:1 et 1:3; une pression totale pg dans le réacteur entre 2 et 4 MPa, en particulier de préférence entre 3 et 4 MPa; et une densité de courant j moyenne entre 5 et 15 mA/cm2, en particulier de préférence entre.. et 12,5 mA/cm2.
EP20749813.0A 2019-07-10 2020-07-10 Procédé d'électro-dicarboxylation d'au moins un alcène avec du dioxyde de carbone co2 en présence d'hydrogène h2 Pending EP3997257A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP19185462.9A EP3763848A1 (fr) 2019-07-10 2019-07-10 Procédé d'électrodicarboxylation d'au moins un alcine avec du dioxyde de carbone co2 en présence d'hydrogene h2
PCT/EP2020/069587 WO2021005216A1 (fr) 2019-07-10 2020-07-10 Procédé d'électro-dicarboxylation d'au moins un alcène avec du dioxyde de carbone co2 en présence d'hydrogène h2

Publications (1)

Publication Number Publication Date
EP3997257A1 true EP3997257A1 (fr) 2022-05-18

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EP19185462.9A Withdrawn EP3763848A1 (fr) 2019-07-10 2019-07-10 Procédé d'électrodicarboxylation d'au moins un alcine avec du dioxyde de carbone co2 en présence d'hydrogene h2
EP20749813.0A Pending EP3997257A1 (fr) 2019-07-10 2020-07-10 Procédé d'électro-dicarboxylation d'au moins un alcène avec du dioxyde de carbone co2 en présence d'hydrogène h2

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EP19185462.9A Withdrawn EP3763848A1 (fr) 2019-07-10 2019-07-10 Procédé d'électrodicarboxylation d'au moins un alcine avec du dioxyde de carbone co2 en présence d'hydrogene h2

Country Status (4)

Country Link
US (1) US11913127B2 (fr)
EP (2) EP3763848A1 (fr)
JP (1) JP2022540185A (fr)
WO (1) WO2021005216A1 (fr)

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3032489A (en) 1959-06-15 1962-05-01 Sun Oil Co Electrolytic production of acyclic carboxylic acids from hydrocarbons
DE2037782A1 (de) 1970-07-30 1972-02-03 Badische Anilin-& Soda-Fabrik Ag, 6700 Ludwigshafen Verfahren zur Herstellung von Adipinsäure
JPS507579B1 (fr) 1971-06-18 1975-03-27
US3864225A (en) 1972-11-17 1975-02-04 Monsanto Co Electrolytic Carboxylation of Substituted Olefins
GB2069533A (en) * 1980-02-19 1981-08-26 Shell Int Research Process for the electrochemical preparation of alkadienedioic acids
US4552976A (en) 1984-08-27 1985-11-12 Texaco Inc. Process for oxidative dicarbonylation of butadiene
CN103555643B (zh) 2008-03-27 2016-08-10 基因组股份公司 用于产生己二酸和其他化合物的微生物
CN101691664B (zh) * 2009-09-30 2011-07-20 华南理工大学 一种利用电化学反应合成3-烯-1,6-二酸的方法

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US11913127B2 (en) 2024-02-27
US20220251717A1 (en) 2022-08-11
EP3763848A1 (fr) 2021-01-13
JP2022540185A (ja) 2022-09-14
WO2021005216A1 (fr) 2021-01-14

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