METHOD FOR THE CONTINUOUS SYNTHESIS OF PARACETAMOL

Abstract

A continuous paracetamol preparation method, including a nitration step or a nitrosation step to obtain p-nitrophenol or p-nitrosophenol respectively. P-nitrophenol or p-nitrosophenol can then be converted into paracetamol by hydrogenation, followed by acylation. This continuous paracetamol preparation method makes it possible to obtain paracetamol with a very good regioselectivity and excellent yields.

Claims

1-47. (canceled)

48. A method for preparing paracetamol, wherein the method comprises a step A of nitration, or nitrosation, of a compound of Formula 1 with a nitration agent, or a nitrosating agent suitable for obtaining a compound of Formula 2: ##STR00019## wherein R represents: a hydrogen atom, a protective group selected from a benzyl or acetate, and wherein X represents a nitro group or a nitroso group, said step A of nitration being carried out continuously: either under microwaves, either under ultrasound, either under microwave followed by ultrasound, or, optionally under microwaves and / or ultrasound, the nitration agent being sodium nitrite, in the presence of an oxidizing agent, in particular in the presence of HNO.sub.3, said step A of nitrosation being carried out continuously: the nitrosating agent being sodium nitrite.

49. The method according to claim 48, wherein step A is a nitration step, R being as defined above, and X being a nitro group, to obtain a nitro compound wherein the compound of Formula 2 has the structure of a compound of Formula 2a: ##STR00020## .

50. The method according to claim 48, wherein step A is a nitrosation step, R being as defined above, and X being a nitroso group, to obtain a nitroso compound wherein the compound of Formula 2 has the structure of a compound of Formula 2b: ##STR00021## .

51. The method according to claim 48, wherein step A of nitration is carried out with a nitration agent selected from HNO.sub.3 and NaNO2, to obtain a compound of Formula 2 wherein X is a nitro group.

52. The method according to claim 48, wherein step A of nitration comprises: a feeding system to a reactor with a solution, in particular aqueous of the compound of Formula 1, in particular in concentration of about 0.4 M, and with the nitration agent, in solution, in particular aqueous, in particular at a concentration of about 0.3 to 0.4 M, to obtain a reaction medium, the formation of the compound of Formula 2.

53. The method according to claim 48, wherein step A of nitration is carried out with an initial ratio of nitration agent / compound of Formula 1 comprised from 1.1 to 1.6, preferably from 1.2 to 1.5.

54. The method according to claim 48, wherein step A of nitration is carried out in at least two microwave reactors in series, preferably at least three microwave reactors in series and particularly preferably at least four microwave reactors in series comprising, between each reactor in series, a cooling step so as to adjust the temperature to a temperature of 20 to 40° C., preferably from 20 to 30° C.

55. The method according to claim 48, wherein step A of nitrosation is carried out in an acidic medium, in particular in an aqueous solution of hydrochloric acid or sulfuric acid.

56. The method according to claim 48, comprising a step A of nitrosation, wherein a reactor is powered by an aqueous solution of the compound of Formula 1, and by NaNO.sub.2 in aqueous solution in an acid, in particular in hydrochloric acid.

57. The method according to claim 48, wherein step A of nitrosation is carried out at a temperature below 10° C., in particular comprising from -5 to 5° C., in particular at a temperature of about 0° C.

58. The method according to claim 48, wherein step A of nitration, or nitrosation leads to the formation of the compound of Formula 2, in particular p-nitrophenol or p-nitrosophenol, in particular p-nitrosophenol, with a regioselectivity greater than 60%, in particular greater than 80%, in particular wherein the ratio of ortho / compound of Formula 2 is less than 2/8, and is in particular about ⅑.

59. The method according to claim 48, wherein said method further comprises, after step A of nitration or nitrosation, a step B of hydrogenation of the compound of Formula 2, to obtain: 4-Aminophenol, where R is a benzyl group or a hydrogen atom, or or O-acetyl-4-aminophenol, in the case where R is an acetate group ##STR00022## R and X being as defined above, said step B of hydrogenation being carried out continuously or in batch, preferably continuously, in the presence of hydrogen, a solvent and a catalyst.

60. The method according to claim 59, wherein step B of hydrogenation is carried out in the presence of a catalyst selected from Pd / C, Pt / C and Fe / HCl, optionally wherein step B of hydrogenation is carried out in the presence of Siliacat Pd (0) as a catalyst, wherein step B of hydrogenation is carried out in the presence of a solvent selected from ethanol or methanol, in particular ethanol, wherein step B of hydrogenation is carried out at a temperature of 50 to 130° C., in particular from 80° C. to 100° C., wherein step B of hydrogenation is carried out at a hydrogen pressure of 10 to 50 bars, in particular comprising from 15 to 30 bars, in particular about 20 bars.

61. The method according to claim 59, wherein step B of hydrogenation is carried out in at least two reactors in series, preferably at least three reactors in series and particularly preferably three or five reactors in series.

62. The method according to claim 59, wherein said method further comprises, after step B of hydrogenation, a step C of acylation of p-aminophenol to obtain paracetamol: ##STR00023## said step C of acylation being carried out continuously or in batch, preferably continuously.

63. The method according to claim 62, wherein step C of acylation is carried out with acetic anhydride as an acylation agent, optionally wherein step C of acylation is carried out at a temperature of 60 to 100° C.

64. A method for preparing paracetamol comprising: ##STR00024## ##STR00025## a step A of nitration or nitrosation of a compound of Formula 1, to obtain a compound of Formula 2, said step A of nitration being carried out, either continuously, or continuously and under microwaves, or continuously and under ultrasound, or continuously and under microwaves and ultrasound, either continuously and optionally under microwaves and / or ultrasound, the nitration agent being sodium nitrite, in the presence of an oxidizing agent, in particular in the presence of HNO.sub.3 said step A of nitrosation being carried out continuously, the nitrosating agent being sodium nitrite, R and X being as defined above, a step B of hydrogenation of the compound of Formula 2, to obtain: 4-Aminophenol, where R is a benzyl group or a hydrogen atom, or paracetamol, where R is an acetate group, or said step B of hydrogenation being carried out continuously or in batch, preferably continuously, and a step C of acylation of 4-aminophenol, to obtain paracetamol, said step C of acylation being carried out continuously or in batch, preferably continuously.

65. The method according to claim 64, comprising: a step A of phenol nitration, to obtain p-nitrophenol, said step A of nitration being carried out continuously and under microwaves, a step B of hydrogenation of the compound of p-nitrophenol, to obtain p-aminophenol: said step B of hydrogenation being carried out continuously in three reactors in series, and a step C of acylation of 4-aminophenol, to obtain paracetamol, said step C of acylation being carried out continuously.

66. The method according to claim 64, comprising: a step A of nitrosation of phenol, to obtain p-nitrosophenol, said step A of nitrosation being carried out continuously, at a temperature below 10° C., a step B of hydrogenation of the compound of p-nitrosophenol, to obtain p-aminophenol: said step B of hydrogenation being carried out continuously in three reactors in series, and a step C of acylation of 4-aminophenol, to obtain paracetamol, said step C of acylation being carried out continuously.

67. The method according to claim 64, further comprising a step D of purification of paracetamol, in particular by continuous distillation, continuous liquid-liquid extraction and or by crystallization, in particular by continuous crystallization.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0187] FIG. 1 shows different chemical pathways for the production of Paracetamol.

[0188] FIG. 2 illustrates the evolution of the temperature of the mixture over time of the reaction mixture as it passes through the circuit formed by several microwave reactors in series, wherein each couple of microwave reactors is interconnected by a cooling circuit.

[0189] FIG. 3 schematizes a facility to perform the first step where the phenol/HNOs mixture is introduced into a facility with multiple microwave reactors in series, where each couple of microwave reactors is interconnected by a cooling circuit.

[0190] FIG. 4 shows an installation to perform the second hydrogenation stage where several hydrogenation reactors are mounted in series.

[0191] FIG. 5 shows a flowchart of the method for the continuous synthesis of paracetamol, including a nitration step.

[0192] FIG. 6 shows a flowchart of the method of continuous synthesis of paracetamol, including a nitrosation step.

[0193] FIG. 7 shows the conversion of a hydrogenation reaction in a system of 3 reactors in series, according to Example 5.2.

[0194] The nitration reaction is carried out by the mixture of phenol and nitric acid.

[0195] This reaction is carried out in the presence of a strong acid such as sulfuric acid, hydrofluoric acid, perchloric acid or boron trifluoride. Preferably, this reaction is carried out in the presence of sulfuric acid.

[0196] Now, in addition to the microwave step, the inventors have shown that the ratio between the concentration of nitric acid and phenol also has a strong influence on the regioselectivity and obtaining of p-nitrophenol rather than o-nitrophenol. Thus, the use of excess nitric acid promotes the formation of o-nitrophenol. Under such conditions, the inventors were able to obtain up to 82% p-nitrophenol (for 18% o-nitrophenol).

[0197] Advantageously the ratio between HNO.sub.3 / Phenol ratio within the starting mixture is between 1.1 and 1.6, preferably between 1.2 and 1.5.

[0198] The concentration of the starting mixture in phenol is between 0.2 and 0.6M, preferably between 0.25 and 0.5 M.

[0199] The concentration of the starting mixture in HNO.sub.3 is between 0.25 and 0.8M, preferably between 0.3 and 0.7M.

[0200] The proportion of water of the starting mixture is between 40 and 95% (in volume relative to the volume of the mixture at this point), preferably between 50 and 90%.

[0201] As for step 1, the residence time of the mixture within the microwave reactor is such that the mixture is brought to a temperature between 70 and 110° C., preferably between 80 and 100° C. The change to a higher temperature affects the regioselectivity and tends to increase the proportion of o-nitrophenol.

[0202] The inventors were able to show that it is possible to further increase the regioselectivity by increasing the residence time of the mixture in the microwave reactor, but without increasing the temperature.

[0203] To do this, the inventors have put in series microwave reactors between which are interspersed cooling circuits.

[0204] According to a preferred embodiment, step 1) is carried out in at least two consecutive microwave reactors, preferably at least three consecutive microwave reactors and particularly preferably at least four consecutive microwave reactors, with a cooling circuit between each microwave reactor so as to bring the mixture to a temperature between 20 and 40° C., preferably between 20 and 30° C.

[0205] Typically, the residence time in all microwave reactors is between 2 and 20 minutes, preferably between 2 and 15 minutes.

[0206] Preferably, each of the microwave reactors (possibly apart from the first) includes a nitric acid feeding system.

[0207] Thus, it is possible to maintain the HNO.sub.3 / Phenol ratio within the mixture between 1.1 and 1.6, preferably between 1.2 and 1.5, throughout the nitration reaction (within the different microwave reactors).

[0208] FIG. 2 illustrates the evolution of the temperature (°C.) with the time (minutes) of the reaction mixture as it passes through the circuit formed by the microwave reactors (MO) interconnected via a cooling circuit.

[0209] FIG. 3 schematizes an installation to perform the first step where the phenol / HNO.sub.3 mixture is introduced into a first microwave reactor (MO) in which it passes through a first cooling circuit before circulating in a second, third and then fourth microwave reactor to form mostly p-nitrophenol with, each time, a passage through a cooling circuit between each microwave reactor.

[0210] To optimize the balance of the reaction, it is necessary to achieve a cooling as fast as possible, typically between 0.5 and 3 minutes, preferably between 1 and 2 minutes.

[0211] At the end of step 1), it is possible to simply separate the 2 isomers o-nitrophenol and p-nitrophenol.

[0212] Such purification can be carried out by an intermediate step (between steps 1 and 2) of steam distillation of o-nitrophenol (see U.S. Pat. 3,933,929), filtration and washing by an aqueous solution of 70% sulfuric acid and then by water (see patent EP 0626366), solubilization (using the difference in solubility in various solvents of the two isomers, N-pentane to remove o-nitrophenol), ultrafiltration (Yudiarto et al., Separation and Purification Technology, vol. 19, p:103-112, 2000), HPLC (SMB type (Simulated Moving Bed) or VARICOL).

[0213] According to a preferred embodiment, p-nitrophenol is purified at the end of step 1) and prior to step 2).

[0214] Now it is also possible to start step 2) without purification and separate p-aminophenol from o-aminophenol at the end of step 2).

[0215] Concerning the second step of reduction of p-nitrophenol to p-aminophenol, it can be carried out from choice via:

[0216] A) addition of dihydrogen under pressure in the presence of catalyst type Pd/C, Pt/C, Fe/HCl or equivalent.

[0217] B) addition of a hydrogen donor (e.g. NaBH.sub.4) in the presence of a solid catalyst (gold nanoparticles, etc.).

[0218] According to a preferred embodiment, step 2) is carried out by adding dihydrogen under pressure in the presence of catalyst of Pd / C, Pt / C, Fe / HCl or equivalent.

[0219] Advantageously, the mixture corresponds to the choice of p-nitrophenol in an aqueous medium in the presence of an acid (preferably sulfuric acid because it gives better yields than hydrochloric acid in particular) or p-nitrophenol in solution in alcohol, preferably ethanol or methanol.

[0220] Advantageously, the hydrogenation of p-nitrophenol is carried out in solution of alcohol, preferably in ethanol.

[0221] The concentration of the mixture in alcohol is advantageously between 70% and 95% (in volume compared to the volume of the mixture upstream of the hydrogenation reactor), preferably between 80% and 90%.

[0222] Preferably, the catalyst used is Pt/C. It is indeed this one that gives the best yields. The catalyst charge within the hydrogenation reactor is included is greater than or equal to 1% (by weight relative to the weight of the mixture within the reactor), preferably greater than or equal to 2% and, particularly preferably, it is equal to 5%.

[0223] The pressure within the hydrogenation reactor is advantageously greater than 20 bars.

[0224] Preferably, the pressure within the hydrogenation reactor is between 20 and 100 bars, preferably between 20 and 50 bars.

[0225] The temperature of the mixture within the hydrogenation reactor is advantageously higher than 80° C.

[0226] Preferably, the temperature of the mixture within the hydrogenation reactor is between 80 and 180° C., preferably between 100 and 150° C.

[0227] To increase the conversion yield, the inventors put several hydrogenation reactors in series.

[0228] According to a preferred embodiment, step 2) is carried out in at least two consecutive hydrogenation reactors, preferably at least three consecutive hydrogenation reactors and particularly preferably at least four consecutive hydrogenation reactors.

[0229] Preferably, an on-line analysis of the mixture is carried out between each hydrogenation reactor in order to control the kinetics of the reaction and, therefore, to control the possible deactivation of the catalyst in order to change it when necessary.

[0230] FIG. 4 schematizes an installation to perform the second step where the mixture comprising p-nitrophenol in solution in ethanol is introduced into a first hydrogenation reactor comprising solid catalyst (Pt / C) and in which dihydrogen is injected under pressure before passing into a second, third and fourth hydrogenation reactor to form mostly p-aminophenol.

[0231] At last, the inventors were able to obtain a conversion yield of p-nitrophenol to p-aminophenol of the order of 97%.

[0232] It should be noted that this second step also has a large number of advantages over conventional methods. Indeed, it guarantees high productivity with a small size due to its continuous operation, it offers great safety because of the small volume required for reactors, it allows the use of catalysts to the maximum of their service life.

[0233] At the end of step 2), and preferably in the event that p-nitrophenol has not been purified at the end of step 1) and prior to step 2).

[0234] According to another preferred embodiment, p-aminophenol is purified at the end of step 2). Such a separation can be achieved simply by the skilled person with regard to his general knowledge, for example by using the differences in solubility between these 2 isomers.

[0235] Concerning the third step of acylation of p-aminophenol to paracetamol, it is carried out by the addition to the mixture, and at the exit of the (last) hydrogenation reactor, of an acylation agent.

[0236] By acylation agent, both acetic acid and acetic anhydride are considered.

[0237] Advantageously, the ratio of acylation agent / p-aminophenol within the mixture, and after the addition of the acylation agent, is between 1 and 10, preferably between 1 and 4.

[0238] In the case where the acylation agent is acetic anhydride, the mixture includes alcohol as a solvent, preferably ethanol or methanol.

[0239] The acylation reaction is then carried out by heating, preferably heating the mixture to a temperature between 20 and 90° C. and for a time between 0.5 and 10 minutes, and particularly preferably by heating the mixture to a temperature between 20 and 60° C. and for a time between 1 and 4 minutes.

[0240] In the case where the acylation agent is acetic acid, it is possible to carry out this acylation in the same way as with acetic anhydride, but without the presence of alcohol and with acetic acid. The temperatures used and the reaction time must then be increased

[0241] Typically, the acylation reaction carried out by heating a temperature between 50 and 130° C. and for a time between 1 and 40 minutes, and especially preferably by heating at a temperature between 60 and 100° C. and for a time between 10 and 20 minutes.

[0242] Now, the inventors have also demonstrated that this acylation reaction can be carried out very quickly with acetic acid in a microwave reactor. It should also be noted that, in this case, acetic acid can be used as a solvent which considerably simplifies the method since the solvent can be reused by simple distillation of the mixture out of the microwave reactor. Concerning acetic anhydride, in addition to the higher cost, its use then requires the removal of the solvent used (ethanol or methanol)

[0243] According to a preferred embodiment, step 3 uses acetic acid and is carried out under microwaves.

[0244] Preferably, this step 3 does not use any additional solvent (in addition to acetic acid).

[0245] Typically, the p-aminophenol / acetic acid ratio is between ⅕ and ⅒, preferably between ⅙ and ⅑.

[0246] To do this, the residence time of the mixture within the microwave reactor is such that the mixture is brought to a temperature between 80 and 120° C., preferably between 90 and 110° C.

[0247] Typically, the residence time in all microwave reactors is between 1 and 60 minutes, preferably between 10 and 30 minutes.

[0248] At the end of the acylation reaction, paracetamol is continuously purified.

[0249] Typically, this purification step can be performed by a simple distillation aimed at removing the solvent.

[0250] Advantageously, this purification step may include a washing step, with purified water, especially under inert gas, argon or equivalent.

[0251] The method according to the invention, of which a flowchart is presented in FIG. 5, makes it possible to synthesize paracetamol with an excellent yield (greater than 70%).

[0252] The following examples are provided for illustrative purposes only and cannot limit the scope of the present invention.

EXAMPLES

1) Phenol Nitration:

[0253] In a microwave reactor with a volume of 6 ml, 50mg of phenol was introduced with 0.7ml of nitric acid 6% by weight with 1.07ml of H.sub.2O.

[0254] The reactor is then set to obtain a temperature of 160° C. for one minute and 30 seconds before cooling at 55° C., before initiating a new heating step at 120° C. for one minute and 30 seconds followed by a new cooling at 55° C.

[0255] The results of HPLC analyses have shown that a conversion of phenol to nitrophenol is obtained with a yield of 99.35% overall, but especially with a proportion of nearly 60% p-nitrophenol (and about 40% o-nitrophenol).

[0256] Subsequent tests have shown that the faster the cooling step, the more the regioselectivity, and therefore the proportion of p-nitrophenol, increases.

[0257] For the continuous nitration reaction, the experiments are carried out in a continuous microwave (SAIREM) with a 2.45GHz wave generator and a 450W power with coaxial transition / waveguide equipped with a cooler.

2) Hydrogenation of P-nitrophenol to P-aminophenol

[0258] In a continuous hydrogenation reactor (total volume 400ml), separated into different zones each equipped with agitators, the pure solvent is introduced with the catalyst Pt/C. The temperature in the reactor is controlled and maintained at the desired temperature by several thermostatic baths that heat or cool the different areas of the continuous reactor. The hydrogen pressure is kept constant at the desired pressure in each area.

[0259] The p-nitrophenol is then continuously introduced into the solvent at a certain rate and concentration.

[0260] Output samples are taken to measure conversion and selectivity.

[0261] For a flow rate of 800ml/h composed of a solution of p-nitrophenol 0.5M in ethanol, or 13.3ml/min, the catalyst charge Pt/C was 2% (weight/weight of the mixture within the reactor) at a constant temperature of 80° C. in each zone.

[0262] The results showed a conversion of 99% with a selectivity of 98% for a residence time of 30 minutes within the reactor.

[0263] Optimization is underway regarding the reaction parameters (reaction volume in each zone, catalyst load in each zone, temperature and Pressure H.sub.2 in each zone and overall flow rate).

[0264] Already, the results have shown that the Pt/C catalyst provides the best results (at about 1% w/w). Now, for a hydrogenation reactor capable of withstanding a hydrogen pressure of 100 bars and a temperature of 150° C., it is possible to increase the catalyst charge up to 5% (w/w) which induces a sharp increase in productivity by reducing the residence time that can be reduced between 15 to 30 minutes, while maintaining good catalyst activity.

3) Acylation of P-aminophenol to Paracetamol:

3.1) Temperature Conversion Tests

[0265] The tests are carried out in the VAPOURTEC R2+ and R3 type reactor of volume 10ml, which is filled by peristaltic pumps. The samples are then recovered at the exit of the VAPOURTEC to be analyzed by HPLC.

[0266] In a first test, the p-aminophenol solution (0.3M in methanol) is injected into the VAPOURTEC at a rate of 5ml/min and at room temperature. Simultaneously, the acetic anhydride solution (0.3M in methanol) is injected into the VAPOURTEC at a rate of 5ml/min at room temperature. The total flow rate is 10ml/min with a passage time of 1mn in the VAPOURTEC.

[0267] Analyses showed a p-aminophenol conversion of 99.9%, with a selectivity of 98.7% for paracetamol.

[0268] In a second test, the p-aminophenol solution (0.14M in ethanol) is injected into VAPOURTEC at a rate of 5ml/min and at a temperature of 60° C. Simultaneously, the acetic anhydride solution (0.14M in ethanol) is injected into the VAPOURTEC at a rate of 5ml/min at 60° C. The total flow rate is 10ml/min with a passage time of 1min in the VAPOURTEC.

[0269] Analyses showed a p-aminophenol conversion of 99.9%, with a selectivity of 98.9% for paracetamol.

[0270] In a third test, the p-aminophenol solution (0.14M in ethanol) is injected into VAPOURTEC at a rate of 3.3ml/min and room temperature. Simultaneously, the acetic anhydride solution (0.14M in ethanol) is injected into the VAPOURTEC at a rate of 3.3ml/min at room temperature. The total flow rate is 6.6 ml/min with a passage time of 1.5 minutes in the VAPOURTEC.

[0271] Analyses showed a p-aminophenol conversion of 99.9%, with a selectivity of 98.9% for paracetamol.

3.2) Microwave Conversion Test

[0272] The microwave used was the MONOWAVE 300 (ANTON PAAR) and whose magnetron power is 850 watts. For this one, the power is adapted to the desired temperature.

[0273] The various reagents are fed into a 10 mL reactor with stirring that is placed in the microwave enclosure. Once the cycle is complete, the reactor is cooled before taking a sample and performing an HPLC analysis.

[0274] In a first test, p-aminophenol is introduced into a solution of acetic anhydride in water (30/70) at a concentration of 7.77 M. The reactor is then introduced into the microwave for 10 seconds and at a temperature of 40° C.

[0275] The results showed that a 99.9% conversion of p-aminophenol with a selectivity of 97% for paracetamol was obtained.

[0276] In a second test, p-aminophenol is introduced into an acetic acid solution at a concentration of 5M. The reactor is then introduced into the microwave for 20 minutes and at a temperature of 100° C.

[0277] The results showed that a 95% conversion of p-aminophenol was achieved with a selectivity of 93.5% for paracetamol.

4) Nitration of Phenol by Nitric Acid, Continuously

4.1) Uncooled Tubular Continuous Reactor: SAIREM “AVOCADO” Cavity

[0278] The reactions were carried out in a 500 mL borosilicate tubular reactor inserted into a cavity of the “AVOCAT” type (SAIREM company) and coupled to a GMS 450 microwave generator that can deliver a maximum power of 450 W thanks to a quartz window transmission. The total volume irradiated is 160 mL.

[0279] 350 ml of a 0.4 M phenol solution and 0.375 M nitric acid (1.25 eq.) were injected into the cavity at a rate of 16 ml/min. Thus, the time of passage in the irradiated zone was 10 minutes.

[0280] The reaction is carried out by microwave irradiation with a power of 250 W, with a microwave generator operating at 2.45 GHz.

[0281] Thus, para-nitrophenol was obtained with a productivity of 25 g/h, and a ratio o/p of 20/80.

4.2) Cooled Tubular Continuous Reactor: SAIREM “DOWNSTREAM” Cavity

[0282] This device consists of a borosilicate tubular reactor (60 mL, internal diameter 12 mm) inserted into a second borosilicate tube (double envelope, internal diameter 23 mm) equipped with coolant inlet and outlet channel. The assembly is inserted into a cavity type “DOWNSTREAM” (company SAIREM) and coupled to a microprobe generator GMS 1000 that can deliver a maximum power of 1000 W thanks to a transmission by quartz window. The total volume irradiated is approximately 10 mL. This device was also equipped with a temperature probe (optical fiber) immersed in the reactor. To cool the internal reactor, a specific oil, of zero dielectric permittivity (therefore transparent to the microwaves), was used. The coolant can be maintained between -10° C. and 0° C. thanks to a cryostat.

[0283] An aqueous solution of 0.4 M phenol and 0.375 M nitric acid (1.25 eq.) was injected into the cavity at a rate of 10 ml/min. Thus, the time of passage in irradiated area was 6 minutes.

[0284] The test demonstrated that microwave heating with cooling allows perfect control and stable temperature throughout the method.

5) Hydrogenation of P-nitrophenol With Siliacat Pd(0) as a Catalyst

5.1) Batch Test

[0285] The batch reaction was performed on a single closed reactor. The reactor is preloaded with a solution of 6.95 g of p-nitrophenol in 100 mL of EtOH and 0.208 mg of SiliaCat P(0) (reagents purchased from Aldrich and catalyst from SiliCycle). The reactor was then purged by dinitrogen (3 purges, 5-7 bars) and then pressurized with hydrogen (H.sub.2 Alphagaz, Air Liquide) under 15 bars. The agitation is set at 1000 rpm (revolutions per minute rotation per minute).

[0286] When the reactor is heated at T = 80° C., a conversion of 86% is obtained in 80 minutes and when the reaction is made at 100° C., a conversion of 88% was obtained in 60 minutes

5.2) Continuous Test

[0287] The same conditions as those used in Example 2 were used, using the catalyst Siliacat Pd(0) (SiliCycle, Quebec Canada, Ref RD-R815-SiliaCat® Pd0),, at a rate of 0.5 mol%.

[0288] A total conversion was achieved in 90 minutes.

5.3) Test on 3 Continuous Reactors in Series- Reactors of Increasing Size

[0289] The hydrogenation reaction was carried out using 3 reactors in series. The following results were achieved.

TABLE-US-00001 Parameters Operating conditions R1 Operating conditions R2 Operating conditions R3 (modélisation) Volume 0,1 L 0,15 L 0,4 L Flow rate 12 ml/mn 12 ml/mn 12 ml/mn Pressure 20 Bar 12 Bar 5 Bar Temperature 100 °C. 110 °C. 130 °C. Mcata Siliacat Pd 0,70% 1,70% 2% Conc p-nitrophenol input 1 mol/l 0,64 mol/l 0,163 mol/l Conc p-nitrophenol output 0,64 mol/l 0,16 mol/l 0,011 mol/l Conversion 0,36 0,73 0,93 Overall conversion % 35,95 83,62 98,85

[0290] In the table above, the amount of catalyst “Mcata” is expressed in mol%.

[0291] A productivity of 3.7kg/L/day of p-aminophenol was achieved with 3 reactors in series.

[0292] FIG. 7 shows the conversions for each reactor.

5) Hydrogenation of P-nitrophenol on a Cascade of Two or Three Perfectly agitated continuous reactors

5.1) Batch Focus

[0293] The reaction in batch mode is carried out on a single closed reactor. The reactor is pre-charged with a solution of 6.95 g of p-nitrophenol in 100 mL of EtOH and 9.75 mg of Pt/C (Sigma Aldrich). The reactor is then purged of dinitrogen (3 purges, 5-7 bars) and then pressurized with hydrogen (H.sub.2 Alphagaz, Air Liquide) under 15 bars. The agitation is fixed at 1000 rpm and the reactor is heated to 80° C. by its double envelope for 1h20. At the end of the reaction, the reactor is inerted by a purge of the dinitrogen and the reaction medium is analyzed by HPLC (reverse phase, column C18). The analysis shows a conversion of 92% of p-nitrophenol to p-aminophenol without trace of reaction co-product.

5.2) Cascade Reaction

[0294] The same device used in Example 5.1, is reused to perform the reaction on a cascade of two perfectly agitated continuous reactors. The outlet line of the first reactor, always equipped with a 5 .Math.m filtering candle to maintain the catalytic loading of the autoclave constant, is connected at the entrance of a second reactor at any point similar to the first. Both reactors are charged with 20 mg Pt/c 10% w/w (Sigma Aldrich). A conversion of 50% is simulated in the first reactor (2.72 g of p-aminophenol for 3.48 g of p-nitrophenol) and a conversion of 75% is simulated in the second reactor (4 g of p-aminophenol per 1.8 g of p-nitrophenol). Under the conditions described above, but with a slightly decreasing pressure (80° C., 15 bars, 1000 rpm in the first reactor; 80° C., 12 bars, 1000 rpm in the second reactor), the cascade is fed by a solution of p-nitrophenol in ethanol (0.3 M) at a flow rate of 3 mL/min (passage time, 30 minutes per reactor) for 5 hours. The withdrawal valve of the second reactor is set to have an output flow rate approximately equal to the input flow rate. No events occur during the 5 hours of reaction. Samples are taken every 4 minutes. HPLC analyses show that the conversion oscillates between 70 and 83% for 20 minutes before stabilizing around 80% without co-product formation.

[0295] In another case, a third reactor is connected to the cascade. Similarly, this reactor is loaded with 20 mg Pt/C, and a starting conversion of 90% is simulated (4.9 g p-aminophenol per 695 mg p-nitrophenol). Under the conditions described above (80° C., 1000 rpm, 15 bars; 12 bars; 10 bars), the waterfall is fed for 4 hours at a flow rate of 4 mL/min (passage time 25 minutes). No events occur. At the reactor outlet, samples are taken every 4 minutes. HPLC analyses show that the conversion oscillates between 80 and 96% for 20 minutes before stabilizing at 95% for 4 hours.

6) Phenol Nitrosation and Hydrogenation - Batch Protocol

6.1) Nitrosation

[0296] To a solution of HCl 35% (40 ml) under air, stirring at T = 0° C., was added drop by drop a solution of NaNO.sub.2 (42% in water, 2 eq.). The solution turned orange and released a small amount of orange gas. A solution of phenol in water (80% in water, 1 g, 1 eq.) was added drop by drop to the solution (Final phenol concentration = 0.3M). The solution gradually turned black and the mixture had become denser. After 30 minutes, an HPLC analysis shows that phenol has been totally consumed. The mixture was diluted in 500 mL of H2O and was extracted by AcOEt (3*250 mL). The organic phases were collected, dried on Na.sub.2SO.sub.4, filtered and evaporated dry to obtain a mixture of 2-nitrosophenol, and 4-nitrosophenol.

6.2) Hydrogenation of Pure P-nitrosophenol a Mixture of Para and Ortho-nitrosophenol

[0297] The dry crude mixture, obtained in Example 6.1, was solubilized in MeOH, Pt / (C) (mass %) was suspended, the mixture was then under hydrogen (1 atm) under stirring. After 2 hours, the mixture showed no trace of 2-nitrosophenol and 4-nitrosophenol. The solution was filtered on celite, and evaporated dry to obtain a mixture of 2-aminophenol and 4-aminophenol in a ratio of o / p = 10/90.

[0298] Two further hydrogenation tests of pure p-nitrosophenol were performed under pressure (P=15 bars) at T=80° C., using the catalyst Pt/C and the catalyst SiliaCat Pd(0). It was obtained a conversion of the order of 99.9% with an excellent yield of 99.8% (control by HPLC)

7) Phenol Nitrosation - Continuous Protocol

[0299] The same ratios used in Example 6.1 were tested continuously. However, after 5 minutes of residence time in the continuous reactor, the aqueous solution of phenol was added, and after a residence time of 5 minutes nitrosophenol was obtained continuously. The extraction was done in batch to carry out batch hydrogenation, according to the conditions of Example 6.2, to obtain a mixture of 2-aminophenol and 4-aminophenol in a ratio of o / p = 10 / 90.