ELECTROCHEMICAL SYNTHESIS OF SUBSTITUTED AROMATIC AMINES IN BASIC MEDIA

Abstract: Substituted amino aromatic compounds such as 3-amino-4-hydroxybenzoic acid are prepared by electrolytically reducing the corresponding nitro aromatic compound in a basic medium at temperatures below 60°C and current densities greater than 50 milliamps per square centimeter. The animohydroxy­ benzoic acids are useful in the preparation of polybenzoxazoles which are used to make fibers and composites having high strength and thermal stability.

Description: This invention relates to the preparation of specific substituted aromatic amines. More specifically, it pertains to a process for the electrolytic reduction of specific substituted nitro aromatic compounds to produce their corresponding amines. Of the substituted aromatic amines, aminohydroxybenzoic acids are known to be useful as monomers in the preparation of polybenzoxazoles. Polybenzoxazoles can be prepared by the condensation of certain multifunctional aromatic compounds such as the aminohydroxybenzoic acids of the present invention. Polybenzoxazole fibers have high tensile and compressive strengths and thermal stability and are desirable for military, aerospace and other applications requiring rigid materials. The reduction of nitro aromatic compounds to their corresponding amines is well-known. For example, US-A-3,475,299 describes an electrolytic reduction of a nitro aromatic compound in an acidic medium in the presence of hydrogen sulfide. US-A-3,424,659 discloses a process for electrolytically reducing nitro aromatic compounds in an electrolytic cell with an acidic catholyte and a basic anolyte. US-A-3,475,300 describes a process for reducing nitro aromatic compounds in the presence of sulfuric acid. All of the above processes relate to an electrolytic reduction in acidic medium. The acidic environment of the aforementioned processes may induce a Bamberger type rearrangement of reaction intermediates, especially at elevated temperatures. The acidic medium makes aromatic compounds susceptible to nucleophilic attack by moieties present in the solution such as water. Therefore, the presence of an acidic medium may lead to the formation of undesirable by-products if direct reduction of the nitro aromatic compound to its corresponding amine is desired. Thus, the selectivity of the electrolytic reduction is decreased. The limited electrolytic reduction of nitro aromatic compounds in the presence of base has been previously described. For example, Brown and Warner, J.Phys.Chem. , 27, 455-465 (1923) describe the reduction of o-nitrophenol by electrolysis to o-amidophenol. Probably o-aminophenol was intended in an alkaline medium in the presence of various metals such as zinc, lead and copper as the cathodic material. Belot et al., Tetrahedron Letters , Vol. 25, No. 47, 5347-5350 (1984) disclose the electrocatalytic hydrogenation of nitro compounds to amines in an alkaline medium in the presence of Devarda copper and Raney nickel electrodes. Belot et al. teach that the reduction is very inefficient and produces unwanted azobenzene when a conventional copper electrode is employed. Organic Electrochemistry, M. M. Baizer & H. Lund, 2nd Ed., Marcel Dekker, Inc., 295-313 (1983) teaches that the electrolytic reduction of various nitro aromatic compounds in an alkaline medium most often yields dimers and other coupled products. An electrolytic process is needed that would provide for the selective reduction of functionalized nitro aromatic compounds in basic media to their corresponding amines. A process is also needed that would provide a high current efficiency and thereby minimize the amount of power consumed by the reaction. This object is attained by a process for preparing an aminohydroxybenzoic acid comprising electrolytically reducing either a 3-nitro-4-hydroxybenzoic acid or a 3-hydroxy-4-nitrobenzoic acid in an alkaline medium at a temperature less than 60°C and a current density of from 100 to 300 mA/cm². The process of the present invention preferably yields at least 50 percent of the desired amine. Contrary to teaching of the prior art, the process of the present invention when carried out in an alkaline medium and in the presence of a copper cathode is very selective for the reduction of several substituted nitro aromatic compounds to their corresponding amines. Surprisingly, this process enables the high conversion of nitro group to amino group with very little, if any, dimer products such as azo compounds or hydroxylated products. Further advantages of the process of this invention include (1) non-corrosive basic medium, (2) lower cell voltage and lower overall voltage requirements, (3) easier separation or isolation and recovery of products, (4) less electrode fouling and (5) lower temperature operation. In addition, this process enables the use of high current densities with minimal evolution of hydrogen. As a result of these advantages, this process is a very efficient and economical method for the selective conversion of nitro aromatic compounds to aromatic amines. In the practice of this invention, any electrolytic cell which permits the reduction of a nitro compound to an amine under alkaline conditions is suitable. The preferred electrolytic cell includes (1) a cathode of copper or similar metal which does not corrode significantly during the reduction process, (2) an anode of nickel, (3) a basic aqueous medium having a pH greater than 7, preferably greater than 8, and a means for separating the cathode from the anode. Most preferably, the electrolytic cell has a two-chamber design. The cathode suitably comprises a conductive material which is inert in the alkaline medium under the conditions of the process. Preferably, the conductive material is a non-corrosive metal such as copper, stainless steel or nickel, with copper being most preferred. The conductive material used for the cathode can also be a conductive carbon-containing material such as graphite, glassy carbon and reticulated vitreous carbon. The anode can be comprised of any stable conductor which is capable of generating oxygen in basic conditions. Typical anodic materials include ruthenium on titanium, platinum, palladium and nickel, with nickel being most preferred. In addition, it is possible and sometimes preferred to simultaneously oxidize an organic compound at the anode as in a "paired reaction". Thus, while the desired amine is being produced at the cathode, another organic compound such as nitrotoluene is being oxidized to nitrobenzoic acid at the anode. The separation means used to define the catholyte and anolyte of the electrolytic cell can be any material which will enable the conductance of a current via ion transport through the material. Typical separators include cation- and anion-exchange membranes, diaphragms such as a porous unglazed cylinder or a sintered-glass diaphragm, glass frits, and other porous materials like clay. The separator is preferably composed of an ion exchange membrane. Most preferably, the separator is composed of a cation-exchange membrane. The alkaline medium employed in the process of this invention is preferably a liquid medium having a pH of at least 8. The medium comprises a compound capable of acting as the electrolyte in the electrolytic cell. For the purposes of this invention, an electrolyte is a compound which dissociates in solution and provides an electrically conductive medium. Preferably, the electrolyte is a base such as alkali or alkaline earth metal hydroxides, quaternary ammonium hydroxides, ammonium hydroxide, borates, and carbonates. More preferred bases include alkali metal hydroxides with sodium hydroxide being most preferred. The solvent for the electrolyte is suitably any liquid having a dielectric constant of at least 10 and being capable of dissolving at least 0.4 weight percent of the electrolyte. Preferably, the solvent is water, a polar organic liquid such as alcohol, lower alkyl nitriles such as acetonitrile, lower alkyl amides such as dimethylformamide, cyclic ethers such as tetrahydrofuran and mixtures of water and one or more of such polar organic liquids. More preferred solvents are water and alcohols such as methanol and ethanol and mixtures of water and such alcohols, with water being the most preferred. Thus, the more preferred alkaline media are aqueous and alcoholic solutions containing from 0.4 to 40 weight percent of dissolved alkali metal hydroxide or alkaline earth hydroxide. Most preferred are aqueous solutions of from 4 to 20 weight percent of an alkali metal hydroxide, especially sodium hydroxide. Such alkaline media preferably have pH values in the range from 14 to 15, most preferably 14. The process is suitably practiced by dispersing the substituted nitro aromatic compound in the alkaline medium in the electrolytic cell in proportions sufficient to permit the desired reduction to occur at a reasonable rate. Preferably, the nitro compound is present in the catholyte in a concentration in the range from 0.05 to 1, more preferably from 0.25 to 0.75, moles per liter of catholyte. The current passed through the electrolytic cell is that which is sufficient to provide a desired rate of reduction of the nitro compound to its corresponding amine. Normally, such current is expressed as current density which is defined herein as the number of coulombs per second passing through a given area (cm²) of the cathode surface. Preferably, the current density employed in the process of the present invention is in the range of from 100 mA/cm² to 300 mA/cm². The current density is more preferably in the range from 100 to 250 mA/cm², with an average current density from 100 to 150 mA/cm² being most preferred. This process can be carried out in a continuous or batchwise manner. The reaction temperature in the electrolytic reduction of this invention is less than 60°C. For example, the electrolytic reduction is preferably performed at 0°C to 60°C, more preferably from 17°C to 30°C. For the electrolysis of some compounds, higher temperatures cause undesirable side reactions and the decomposition of the nitro aromatic compound or the amine product. The electrolytic reduction of this invention is most preferably carried out at ambient temperatures. The reaction times depend upon the quantity of the starting material, the current density, the electrode area, and the current efficiency for conversion. The end point of the reaction is generally the point when the nitro compound is consumed. For example, the end point may be found by monitoring the reaction by high performance liquid chromatography. In a preferred embodiment, the process of this invention is carried out by electrolytic reduction of the starting nitro aromatic compound under basic condition using copper as the cathode. In this embodiment, an organic solvent may be added to the cathode chamber if the nitro compound is insoluble or only slightly soluble in water. The organic solvent used for this purpose should be an inert organic solvent which is miscible with water and dissolves the nitro compound. An example of such a solvent or cosolvent is an alcohol such as methanol, ethanol, etc. It is desirable that a blanket of nitrogen or other inert gas be employed in the electrolytic cell to prevent reoxidation of the amine product. The process of the present invention surprisingly exhibits high current efficiencies and selectivities at high current density. Low power consumption is characteristic of the process of the present invention. Therefore, the present invention provides for an economic means for producing the aminohydroxybenzoic acids which may be used as monomers in the production of polybenzoxazoles as hereinbefore described. The following examples are included for the purposes of illustration only. Unless otherwise indicated, all parts and percentages are by weight. Example 1 In order to investigate the effect of various parameters on the reduction of 3-amino-4-hydroxybenzoic acid, an all-glass, two-chamber, flange-type cell was constructed which allowed easy disassembly and short electrolysis times. The catholyte and anolyte reservoirs were 30 ml capacity with water jacketing for temperature control. Convection was achieved via N₂ sparge through the bottom of each compartment. Mass transport was not ideal in this cell, but parameter evaluation could be done in an efficient manner with it. The electrodes were approximately 6 cm² and current densities were reported below for the actual geometric areas. An ion-exchange membrane (typically Nafion 324 ® obtained from duPont) was pressed between gaskets to expose 6 cm² area. A 14/20 ground-glass joint on top of each chamber allowed for a condenser and/or an oil-filled 'bubbler' to keep a nitrogen head over the easily oxidized amine. The electrode to electrode separation was about 2.5 cm. Example 1a: As an initial experiment, the following standard conditions were utilized. The cathode was a flag of 99.9 percent copper (6.3 cm²) and the anode a nickel expanded metal flag of equal projected area. The anolyte and catholyte were separated by a cation-exchange membrane having an exposed area of 6.3 cm². The catholyte was composed of 1 g of 3-nitro-4-hydroxybenzoic acid dissolved in 20 ml of IN NaOH (initial pH 13-14). The anolyte consisted of 20-25 ml of 5N NaOH. The reaction temperature was maintained at 25 (±1)°C in this example. A constant current of 0.500 amps (i.e., current density of 79.4 mA/cm²) was applied through the cell after nitrogen sparging the cell for 5 minutes. Nitrogen sparge was continuously applied for mixing the catholyte and anolyte. Liquid chromatographic analyses were performed throughout the run on aliquots of the catholyte to follow the course of the reaction. The theoretical charge for conversion of the starting material to the amine was calculated as Q t = (solute (g)/183 g/mole) x (96485 C/eq) x (6 eq/mole). The chemical yield, current efficiency (CE), and conversion were calculated with a correction for the small (but linear) increase in catholyte volume with charge passed due to water migration through the cation-exchange membrane. At Q t = 100 percent, the conversion is 83 percent, CE = 85 percent, and the yield 85 percent. At Q t = 125 percent, the corresponding values are conversion = 93 percent, CE = 71 percent and yield = 89 percent. Example 1i: Example 1a was duplicated with the exception that the current density was 150 mA/cm². The results of the preceding examples are summarized in Table I. Example 1 Q t = 100% Q t = 125% % Conv % CE % Yield % Conv % CE % Yield a 83 85 85 93 71 89 i 80 65 53 86 64 80 As evidenced by the data of Table I, the process of this invention can be practiced using different current densities. Example 2 The cathode material was varied to determine the effects of this parameter. All conditions were held constant as in Example 1a above except for the variance of cathode material and current density. The area for calculation of current density was taken to be the area of one side of the flag. Run No. 2i: Graphite The cathode was a cylinder of graphite. The area was estimated as the circumference times the length of the immersed portion of the rod. The results of these examples are recorded in Table II. Example 3 Cell Design: The electrochemical cell used in this example was a parallel-plate, two-chamber design and was machined out of polypropylene. A copper cathode and a nickel anode (both(30 inches x 5 inches) 76 cm x 15 cm ) were separated by a cation-exchange membrane which was physically supported by titanium screens on each side. Flow distribution was accomplished via (1/8-inch) 0.3 cm holes on (1/4-inch) 0.6 cm centers on top and bottom of each chamber. Electrolysis: The general procedure for electrolysis was to fill the anolyte reservoir with 5 liters of 5N NaOH which was supplemented with additional base when necessary in order to prevent pitting of the anode. The catholyte was then placed in the 12-liter reservoir and circulated via a centrifugal-type pump through the cell. In the reservoir was a reaction mixture containing 104 g/liter of 3-nitro-4-hydroxybenzoic acid, 40 g/liter of sodium chloride and 80 g/liter of sodium hydroxide. A nitrogen sparge was kept over the catholyte at all times during the electrolysis. A small trickle current (approx. 25 mA) was kept flowing through the cell before and between runs to protect the copper from corrosion. After circulation of the anolyte and catholyte were started (typically 600 and 1500 ml/min, respectively), the main rectifier was connected and 100 amps was passed through the cell. Aliquots of the catholyte were taken at intervals and analyzed via liquid chromatography. The current was adjusted stepwise to minimize the amount of hydrogen evolution at the cathode. The average current density was about 100 mA/cm² and the temperature was ambient temperature. Product isolation was via acidification of the catholyte. This was accomplished via aspiration of aliquots of the catholyte into side-arm flasks which contain con-HCl and typically 10 g/liter of SnCl₂ (as antioxidant). Table III indicates some of the results obtained with this cell. As evidenced by the data in Table III, high purity products are produced by the practice of this invention using a simple cell design and work-up procedure. Example 4 Cell Design: In this example, the electrochemical cell was one of commercial design with a monopolar arrangement of 8 copper and 7 nickel electrodes to provide an active area of 5558 cm² (5.98 ft²) for the cathode and anode, respectively. A cation-exchange membrane was used to separate each anode and cathode. The monopolar arrangement precluded the possibility of a low-current, high-voltage system but allowed the use of both sides of an electrode. The overall dimensions of the cell were only 55 x 24 x 17 cm. Catholyte and anolyte reservoirs were (15-gallon) 0.057 cm³ polypropylene tanks which were fitted with one-inch 2.5 cm thick plexiglas tops and drilled for various fittings. The catholyte-reservoir top was fitted with a large o-ring to form an air-tight seal. Air-driven stirring was provided via stainless steel propellers, but was only used for the catholyte. Circulation through the cell was provided by 1/5 HP centrifugal pumps (3450 rpm). Magnetically coupled "paddle-wheel" type flow meters were placed in the line between the bottom of the reservoirs and the inlets of the cell. Simple shut-off valves were used on each side of the pumps in order to allow easy removal and to allow control of the flow rate. Self-priming of the pumps was accomplished by permanent elevation of the reservoirs. Stainless steel((¼-in.) 0.6 cm ) tubing was coiled in each reservoir and supplied with cold water for cooling. Nitrogen purging or padding minimized the formation of carbonate and prevented air oxidation of the amine. The power supply for the cell consisted of a rectifier capable of 18 volts (DC) and 2000 Amps (A). Five OO-welding cables provided adequate conduction to the cell to cause only slight voltage drop. A small power supply provided 0.25 A through the cell for cathodic protection whenever the main rectifier was shut off. Syntheses: The general procedure for the batch electrolysis was to fill the anolyte reservoir to approximately 50 liters of 5N NaOH. The catholyte consisting of 3-nitro-4-hydroxybenzoic acid (8-10 percent) in nominally 2N NaOH was pumped into a polyethylene reservoir, weighed and then transferred via slight N₂ pressure into the catholyte reservoir. The pumps were started and current applied quickly thereafter. Initial currents were varied from 600 to 1250 amps. Samples for liquid chromatographic analyses were taken at about every 20 percent of the theoretical charge. The anolyte was returned to original pH level after each batch electrolysis by addition of 50 percent NaOH. The current was controlled manually to minimize the amount of evolved hydrogen and to keep the cell voltage at or below 3V. Electrolysis was generally terminated at 115 to 125 percent of the theoretical charge (determined by a conversion greater than 97 percent). A final liquid chromatographic analysis, mass and density were obtained to give the final conversion, yield and current efficiency. Table IV shows the data and results for ten electrolyses. Isolated recrystallized yields are greater than 80 percent with greater than 99.9 percent purity. Cathode and anode corrosion are minimal. A high purity monomer is obtained in high yields in multi-Kg quantities with a power consumption significantly less than 2 kilowatt hour/lb. Electrolyses Results (Chromatographic) Run No. mole Nitro CD , mA/Cm² % Conv % Yield % CE % Q 1 19.2 77 98 99 86 115 2 22.2 103 98 97 84 116 3 21.2 121 98 96 83 115 4 22.2 134 98 100 84 120 5 20.0 131 97 100 83 121 6 24.0 137 98 91 79 115 7 20.5 133 97 96 81 120 8 21.5 134 98 99 82 121 9 20.0 133 98 103 82 126 10 20.7 137 98 101 84 120 Example 5 Several classes of nitro aromatic compounds were subjected to cathodic reduction in basic media at a copper electrode. The reactions were followed by liquid chromatography with a Hewlett Packard 1090A system which incorporated a diode array as the detector. Identification of the corresponding aniline products was accomplished via retention time match and spectral authentication. Quantitation of each product was via response factor for authentic amine, either purchased with known purity, or synthesized in-house by nonelectrochemical methods. Reaction conditions were identical to those in Example 2a unless stated differently. The major differences were changes in the solvent (usually addition of methanol) or temperature to increase the solubility of the nitro aromatic compound in the catholyte. The reactants and products are recorded in Table V. This example demonstrates that at least six classes of nitro aromatic compounds provide good to excellent yields of amines in basic media. Run A is 3-nitro-4-hydroxybenzoic acid Run B is 3-hydroxy-4-nitrobenzoic acid Run G is 2-nitrobenzoic acid Run H is 4-nitrobenzoic acid Run I is 3-nitrobenzoic acid Run S is aniline Run T is 2-chloroaniline Run U is 4-chloroaniline Run W is p-aminobenzenesulfonic acid Run No. Reactant¹ Product² Q t = 100% Q t = 125% % Yield % Conv % Yield % Conv A NHBA(3,4) AHBA(3,4) 85 83 89 93 B NHBA(4,3) AHBA(4,3) 88 92 96 100 G NBA(2) ABA(2) 24 72 - - H NBA(4) ABA(4) 23 100 - - I NBA(3) ABA(3) 0 100 - - S NB A 25 90 28 92 T CNB(1,2) CA(1,2) 49 95 48 100 U CNB(1,4) CA(1,4) 30 91 33 100 W NBSA(4) ABSA(4) 14 99 13 100

Claims: A process for preparing an aminohydroxybenzoic acid comprising electrolytically reducing either a 3-nitro-4-hydroxybenzoic acid or a 3-hydroxy-4-nitrobenzoic acid in an alkaline medium at a temperature less than 60°C and a current density of from 100 to 300 mA/cm². The process of claim 1 which is conducted in an electrolytic cell having a cathode of a metal which is non-corrosive under the conditions of the reduction process and an anode of a stable conductor which is capable of generating oxygen in the alkaline medium. The process of claim 1 wherein the cathode is copper, stainless steel, nickel or conductive carbon-containing material and the anode is ruthenium or titanium, platinum, palladium or nickel. The process of claim 2 wherein the cathode and anode are separated by an ion-exchange membrane. The process of claim 1 wherein the pH of the alkaline medium is at least 8 and the medium contains an electrolyte. The process of claim 5 wherein the electrolyte is an alkali metal hydroxide. The process of claim 1 wherein the current is applied using a copper cathode. A process of claim 1 wherein electrolytic reduction is carried out in an electrolytic cell having a catholyte and an anolyte both of which contain the alkaline medium and are defined by a separation means which enables the conductance of current via ion transport through the separation means.

Inventors: GREGORY, THOMAS DAVID, STUTTS, KENNETH JAMES
Applicants: THE DOW CHEMICAL COMPANY
Application year: 1988
Main classification: C25B3
IPC codes: C25B3