EP2528884A1

EP2528884A1 - Method for carboxylizing aromates and heteroaromates using co2

Info

Publication number: EP2528884A1
Application number: EP10788351A
Authority: EP
Inventors: Christian Severins; Sigurd Buchholz; Kilian Tellmann; Jürgen WIESCHEMEYER; Klaus Weidemann
Original assignee: Bayer Pharma AG
Current assignee: Bayer Intellectual Property GmbH
Priority date: 2009-12-21
Filing date: 2010-12-17
Publication date: 2012-12-05
Also published as: CN102822132A; WO2011076679A1; DE102009060033A1; JP2013515027A; US20120323019A1

Abstract

The invention relates to a method for producing aromatic and heteroaromatic carbolic acids using CO₂.

Description

Process for the carboxylation of aromatics and heteroaromatics with CO

The present invention relates to a process for the preparation of aromatic and heteroaromatic carboxylic acids using CO ₂ . Aromatic and heteroaromatic carboxylic acids have been known for a long time. They are therefore, among other building blocks of many pharmaceutical products and their selective synthesis of crucial importance. As an example of a heteroaromatic carboxylic acid may be mentioned thiophene-2-carboxylic acid whose derivatives have a microbicidal action. There are many different production methods for aromatic and heteroaromatic carboxylic acids. Almost all methods are multi-level. Particularly widespread is a two-step process consisting of an acylation of the aromatics or heteroaromatics with subsequent oxidation to the corresponding carboxylic acids. The corresponding Friedel-Crafts acylations are usually carried out in the presence of stoichiometric amounts of Lewis acids in anhydrous solvents (see, for example, DE102007032451 A1, EP178184A1).

The transfer of such reactions from the laboratory to an industrial scale always poses a significant problem because the solvents are polluting in different ways. Also, product isolation involves relatively large amounts of high salinity wastewater that needs to be worked up. The oxidation of the aryl ketone is usually carried out with organic peroxides or inorganic oxidizing agents (Dodd et al., Synthesis 1993, 295-297, US5739352). The transfer of such oxidations to the industrial scale is also a significant problem, since the oxidizing agents pollute the environment in different ways and the reactions are highly exothermic.

An efficient method of preparation of aromatic and heteroaromatic carboxylic acids is a so-called direct carboxylation with CO ₂ . CO ₂ is also a non-toxic and readily available, inexpensive source of Cr. However, there are only a few literature examples for the direct carboxylation of aromatics and heteroaromatics with CO ₂ .

Such a direct carboxylation of heteroaromatics is described in US2948737. There it is disclosed that the direct carboxylation with gaseous CO ₂ at temperatures> 300 ° C in the presence of acid-binding reagents at a reaction pressure of 1570 bar in an autoclave with moderate yields (8%) succeeds. In US3138626 it is described that direct carboxylation with gaseous CO _{2 can be carried out} from temperatures of 100 ° C. in the presence of AICI ₃ at a reaction pressure of 200 bar in an autoclave with moderate yields (22%). The transfer of such reactions on an industrial scale represents a significant problem because of the high reaction temperatures, since many carboxylic acids of aromatics and Heteroaroma- ten have significantly lower decomposition temperatures.

Ohishi et al. (Angew Chem Int Ed., 2008, 47, 5792-5795) describe experiments in which aromatic and heteroaromatic carboxylic acids in organic solvents using mixtures of boronic acid esters, a homogeneous copper-carbene catalyst and CO ₂ at clearly lower temperatures (70 ° C) were produced.

Oshima et al. (Org. Lett., 2008, 10, 2681-2683) disclose experiments in which aromatic carboxylic acids were prepared at room temperature using mixtures of organic zinc compounds, a homogeneous nickel-phosphorus catalyst and gaseous CO ₂ .

The problem with the transfer of these reactions in an industrial process is the use of costly homogeneous catalysts that are not recyclable. Also fall in product isolation relatively large amounts of wastewater with high salt content, which must be worked up.

There is therefore a need for a simple and inexpensive process for the preparation of aromatic and heteroaromatic carboxylic acids, which can also be carried out on an industrial scale.

Starting from the known state of the art, the technical problem thus arises of providing a process for the preparation of aromatic and heteroaromatic carboxylic acids which is comparatively easy to carry out and inexpensive and leads to higher yields. The process sought should continue to have as low as possible environmentally hazardous potential and safe temperature control. The formation of large quantities of salt-like wastewater should be avoided. The process should be usable in particular for the carboxylation of thiophene and / or furan and / or their derivatives.

According to the invention, this object is achieved by a method according to claim 1. Preferred embodiments can be found in the dependent claims. The process according to the invention for the carboxylation of aromatics and heteroaromatics comprises at least the following steps: a) provision of a first liquid component comprising an aromatic and / or heteroaromatic compound,

b) providing a second liquid component comprising an organic and / or inorganic base,

c) mixing the first and second liquid components,

d) mixing the mixture from step c) with CO ₂ under reaction of the aromatic or heteroaromatic compound with CO ₂ .

In step a) of the process according to the invention, a first liquid component, at least comprising an aromatic compound and / or a heteroaromatic compound is provided. An aromatic compound is also referred to here for short as aromatic and a heteroaromatic compound as heteroaromatic.

One or more aromatics and / or heteroaromatics are used in the inventive method as starting material and carboxylated.

The provision of the starting material takes place in liquid form. The educt (aromatic, heteroaromatic) may already be present in liquid form. In this case, the component referred to in step a) as the first liquid component may be the liquid educt. Likewise, it is conceivable first to dissolve the educt in a solvent and to provide this solution as the first liquid component.

Aromatics and heteroaromatics are understood as meaning organic compounds which have a planar, cyclic structural motif of conjugated double bonds and / or lone pairs of electrons or unoccupied p orbitals.

In the conjugated double bonds there are comparatively low energy levels for the bonding electrons, which is why conjugated double bonds are characterized by decreased and altered reactivity over other (non-conjugated) double bond systems.

While the cyclic structural motif of aromatics is formed only by carbon atoms, heteroaromatics have one or more heteroatoms, i. Non-carbon atoms in the ring skeleton, e.g. Oxygen, nitrogen and / or sulfur.

As the aromatic or heteroaromatic compound, benzene derivatives, especially with heteroatoms in the side chain such as anisole or dimethylaniline, six-membered heteroaromatics such as pyridine, five-membered heteroaromatics such as pyrrole, seven-membered aromatics such as azepine, thiepin, oxepin can be used. Preference is given to using heteroaromatics which have one or more heteroatoms which function as π-electron donors and increase the electron density in the ring.

Preference is given to using aromatics and / or heteroaromatics which have a five-membered ring, since in this case the electron density is increased in comparison with a six-membered ring.

Very particular preference is given to using thiophene and / or furan and / or derivatives of thiophene and / or furan in the process according to the invention. By a derivative is meant a chemical compound which can be derived from a parent (here, for example, furan or thiophene). A derivative is characterized in that at least one point of the molecule of the ground substance another atom or atom group sits.

By carboxylation is meant the introduction of a carboxyl group into an organic compound. Carboxylation is a reaction to produce carboxylic acids.

In step b) of the process according to the invention, a second liquid component is provided at least comprising an organic and / or inorganic base. The second liquid component may be the base itself; it is also conceivable that the second liquid component is a solution in which an organic and / or inorganic base is contained.

Preference is given to using n-butyllithium, t-butyllithium, methyllithium, phenyllithium, lithium diisopropylamide (LDA) and / or hexyllithium as the base.

In step c) of the process according to the invention, the first and second liquid components are mixed.

The merging of the liquid components is preferably carried out at a temperature in the range of -100 ° C to 40 ° C and at a pressure of 1 to 60 bar. The aim of step c) is to produce as homogeneous a mixture as possible of the two liquid components.

In step d) of the process according to the invention, the mixture of the mixture obtained from step c) is mixed with CO ₂ . CO ₂ can be added in gaseous, liquid, solid or supercritical state or in solution to the mixture of the base and the aromatic and / or heteroaromatic. Preferably, the addition of CO ₂ takes place in the gaseous or liquid state.

The mixing in step d) is preferably carried out at a temperature in the range of -100 ° C to 60 ° C and at a pressure of 1 to 60 bar. With the addition of CO ₂ , the carboxylation of the aromatic and / or heteroaromatic is initiated. The reaction between the aromatic and / or the heteroaromatic with CO ₂ is carried out to the desired or achievable conversion.

Preferably, after reaction of the reactants, the reaction mixture is worked up to isolate and optionally purify the desired carboxylated product. The process according to the invention therefore preferably comprises a further step e) following step d): e) collecting the mixture from step d) and isolating the carboxylated product.

To isolate the carboxylated aromatic or heteroaromatic, the reaction mixture is preferably first provided with acid to bind remaining amounts of base. The carboxylated product can be isolated, for example, by extraction and / or distillation and / or chromatography.

The process according to the invention can be carried out continuously or batchwise. Likewise, it is conceivable to carry out some steps of the method according to the invention continuously and the remaining steps discontinuously. At least steps c) and d) are preferably carried out continuously.

Continuous steps in the sense of the invention are those in which the feed of compounds (starting materials) into a reactor and the discharge of compounds (products) from the reactor take place simultaneously but spatially separated, while in discontinuous steps the consequence is the feed of compounds (educts) , if necessary, chemical reaction and discharge of compounds (products) take place consecutively. The continuous procedure is of economic advantage, since reactor down times due to filling and emptying processes and long reaction times due to safety requirements, reactor-specific heat exchange performance as well as heating and cooling processes, as they occur in batch processes (batch processes) are avoided. The preferably continuous mixing of compounds in step c) and / or in step d) is preferably carried out by means of a static mixer.

While in dynamic mixers, the homogenization of a mixture by moving organs such as stirrer is achieved, in static mixers, the flow energy of the fluid is exploited: A conveyor unit (eg a pump) presses the liquid, for example, through a pipe provided with static mixer fittings the main flow axis following liquid in Partial flows is divided, which are swirled and mixed with each other depending on the type of internals.

An overview of various types of static mixers, as used in conventional process engineering, for example, the article "Static mixers and their applications", MH Pähl and E. Muschelknautz, Chem.-Ing.-Techn. 52 (1980) No. 4, pp. 285-291.

As an example of static mixers, SMX mixers may be mentioned here (cf US Pat. No. 4,062,524). They consist of two or more mutually perpendicular lattices of parallel strips, which are interconnected at their crossing points and are employed at an angle to the main flow direction of the mixed material to divide the liquid into partial streams and mix. A single mixing element is unsuitable as a mixer, since a mixing takes place only along a preferred direction transverse to the main flow direction. Therefore, several mixing elements, which are rotated by 90 ° to each other, must be arranged one behind the other.

The use of micro process technology is advantageous for the process according to the invention or for steps of the process according to the invention.

The modular micro process technology or micro reaction technology offers the possibility to assemble different micro process modules according to a modular principle into a complete production plant in the smallest format.

Modular microreaction systems are commercially available, e.g. by Ehrfeld Mikrotechnik BTS GmbH. The commercially available modules include mixers, reactors, heat exchangers, sensors and actuators and much more.

The mixing in step c) and / or step d) preferably takes place by means of one or more so-called micromixers.

The term "micromixer" used here is representative of microstructured, preferably continuously operating reactors, which are known under the name microreactor, mini-reactor, micro-heat exchanger, mini mixer or micromixer. Examples are microreactors, micro-heat exchangers, T and Y mixers and micromixers from a wide variety of companies (eg Ehrfeld Mikrotechnik BTS GmbH, Institute for Microtechnology Mainz GmbH, Siemens AG, CPC-Cellular Process Chemistry Systems GmbH and others), as known to those skilled in the art Generally, a "micromixer" in the sense of the present invention usually has characteristic / determining internal dimensions of up to 1 mm and contains static mixing internals.As an example of a static micromixer, the diamond mixer described in DE20219871U1 may be mentioned. Due to the reduction of the characteristic dimensions, mixing processes in micromixers are considerably faster than in conventional mixers, in addition to heat transport processes. Thus, the process speeds in micromixers are sometimes higher by orders of magnitude than in conventional apparatus, and the mixing distances are reduced to a few millimeters. The reaction of an aromatic and / or heteroaromatic in step d) of the process according to the invention is preferably carried out by passing the reaction mixture through a residence zone. The residence section preferably has one or more static mixers.

The metering rate of all components and the flow rate of the reaction mixture through the residence zone depend primarily on the desired residence times and / or achievable conversions. The higher the maximum reaction temperature, the shorter the residence time should be. As a rule, the reactants in the reaction zone have residence times of between 20 seconds (20 seconds) and 400 minutes (400 minutes), preferably between 1 minute. and 400 min., most preferably between 1 min. and 20 min.

The residence time can be controlled, for example, by the volume flows and the volume of the reaction zones. The course of the reaction is advantageously followed by various measuring devices. Particularly suitable for this purpose are devices for measuring the temperature, the viscosity, the thermal conductivity and / or the refractive index in flowing media and / or for measuring infrared and / or near-infrared spectra.

It is conceivable to feed CO ₂ to the reaction mixture along part of the residence zone or along the entire residence zone.

The process according to the invention can preferably be carried out in temperature-controlled flow reactors. In a preferred embodiment, the reaction plant for carrying out the method according to the invention comprises at least two zones which can be tempered independently of one another. In the first zone, the mixing of the liquid components takes place, comprising an aromatic and / or heteroaromatic compound and an inorganic and / or organic base (step c)). In the second zone, the reaction zone, the addition of CO ₂ and the reaction of the aromatic and / or heteroaromatic compound (step d)) takes place. At the end of the reaction zone, the product is preferably collected and collected to isolate the desired product in a subsequent step (step e)). The invention is explained in more detail below by means of examples, without, however, limiting them to them. example 1

Preparation of 5-chlorothiophene-2-carboxylic acid by direct carboxylation with CO ₂

A solution of 12.5 parts by mass of 2-chlorothiophene and 87.5 parts by mass of THF was charged to the original 1. A solution of 23 parts by weight of n-butyllithium and 77 parts by weight of hexane was charged in the original 2. The two templates were connected by a pre-tempering line (0 ° C) with a static mixer (volume 0.3 ml), at its outlet channel a 4.3 cm ³ volume and a surface area to volume ratio of 22.6 cm ² / cm ^"3 (0 ° C) was connected and led to an inlet of another static mixer (volume 0.3 ml) At the second inlet of the static mixer a CCV gas cylinder was connected via a pressure reducing valve (1.3 bar) its outlet channel was connected to a 0.9 cm ³ volume and surface area to volume ratio of 40 cm ² / cm ³ (0 ° C.) The solution from template 1 was added at a volume flow of 56 ml / h and the solution The total residence time was 3.5 min and the reaction was monitored regularly by HPLC, the relative yield of 5-chlorothiophene-2-carboxylic acid being> 70%. The product stream was at 0 ° C quenched on 5.7 M HCl solution. After phase separation and washing of the aqueous phase with n-hexane, the combined organic phases were concentrated to dryness. The 5-chlorothiophene-2-carboxylic acid was taken up for purification in a mixed solution of 50 parts by mass of hexane, 35 parts by mass of methanol and 15 parts by mass of water. The aqueous phase was then concentrated in vacuo to remove the methanol. 5-chlorothiophene-2-carboxylic acid crystallizes after cooling the mother liquor to 5 ° C in the form of white needles.

Example 2

Preparation of 2-furanic acid by direct carboxylation with CO ₂

A solution of 5 parts by weight of furan and 95 parts by mass of THF was charged to the original 1. A solution of 23 parts by weight of n-butyllithium and 77 parts by weight of hexane was charged in the original 2. The two templates were connected by a pre-tempering line (-30 ° C) with a static mixer (volume 0.3 ml), at its outlet channel a 5.4 cm ³ volume and a surface-to-volume ratio of 26, 3 cm ² / cm ³ (-30 ° C), and was connected to an inlet of another static mixer (volume 0.3 ml) .At the second inlet of the static mixer was a pressure reducing valve (1.3 bar) C0 ₂ gas flask connected to the outlet channel of a residence element with 3.8 cm ³ volume and a surface area to volume ratio of 18.2 cmVcrn ³ (0 ° C), followed .. The solution from template 1 was with a volume flow of 139 ml / h and the solution from template 2 with a volume flow of 40 ml / h continuously pumped through the reactor. The total residence time was 2.0 min. The reaction was monitored regularly by HPLC. The relative yield of 2-furanic acid was> 80%. The product stream was quenched at 0 ° C to 5.7 M HCl solution. After phase separation and washing of the aqueous phase with n-hexane, the combined organic phases were concentrated to dryness. The 5-chlorothiophene-2-carboxylic acid was taken up for purification in a mixed solution of 50 parts by mass of hexane, 35 parts by mass of methanol and 15 parts by mass of water. The aqueous phase was then concentrated in vacuo to remove the methanol. 2-furanic acid crystallizes after cooling the mother liquor to 5 ° C in the form of yellowish needles.

Claims

claims

A process for the carboxylation of aromatics and heteroaromatics comprises at least the following steps: a) providing a first liquid component comprising an aromatic and / or heteroaromatic compound,

c) mixing the first and second liquid components,

d) mixing the mixture from step c) with CO ₂ with reaction of the aromatic or heteroaromatic compound with CO ₂ .

Method according to claim 1, comprising the further step e) following step d):

e) collecting the mixture from step d) and isolating the carboxylated product.

Method according to one of the preceding claims, characterized in that step c) and / or step d) is carried out continuously.

Method according to one of the preceding claims, characterized in that the mixing in step c) and / or in step d) is carried out by means of static mixer.

Method according to one of the preceding claims, characterized in that the reaction of CO ₂ with an aromatic and / or heteroaromatic compound is carried out in a microreaction plant.

Method according to one of the preceding claims, characterized in that at least one compound from the following series is used as the aromatic and / or heteroaromatic compound: derivatives of benzene, in particular with heteroatoms in the side chain such as anisole or dimethylaniline, six-membered heteroaromatic compounds such as pyridine, five-membered heteroaromatic such as pyrol, thiophene or furan and derivatives of these compounds, seven-membered aromatics such as azepine, thiepin or oxepin.

7. The method according to any one of the preceding claims, characterized in that at least one compound from the following as inorganic and / or organic base Series is used: n-butyllithium, t-butyllithium, methyllithium, phenyllithium, lithium diisopropylamide (LDA) or hexyllithium.

8. The method according to any one of the preceding claims, characterized in that CO _{2 is added} in gaseous or liquid state.

9. The method according to any one of the preceding claims, characterized in that the reaction mixture is passed through a residence section in step d), wherein the residence section has one or more static mixer.

10. The method according to any one of the preceding claims, characterized in that the reaction mixture in step d) spends a residence time in the range of 20 seconds to 400 minutes in a residence zone.