WO2001046130A1 - Process for the preparation of diphenyl ether compounds - Google Patents

Process for the preparation of diphenyl ether compounds Download PDF

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Publication number
WO2001046130A1
WO2001046130A1 PCT/GB2000/004731 GB0004731W WO0146130A1 WO 2001046130 A1 WO2001046130 A1 WO 2001046130A1 GB 0004731 W GB0004731 W GB 0004731W WO 0146130 A1 WO0146130 A1 WO 0146130A1
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Prior art keywords
fomesafen
solvent
process according
tolyloxy
trifluoro
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PCT/GB2000/004731
Other languages
French (fr)
Inventor
Stephen Martin Brown
Brian David Gott
James Peter Muxworthy
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Syngenta Limited
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Publication date
Application filed by Syngenta Limited filed Critical Syngenta Limited
Priority to EP00985526A priority Critical patent/EP1246796B1/en
Priority to DE60019337T priority patent/DE60019337T2/en
Priority to HU0204189A priority patent/HUP0204189A3/en
Priority to JP2001547041A priority patent/JP4619602B2/en
Priority to AT00985526T priority patent/ATE292620T1/en
Priority to US10/168,611 priority patent/US6790991B2/en
Priority to AU21939/01A priority patent/AU2193901A/en
Priority to IL14986900A priority patent/IL149869A0/en
Publication of WO2001046130A1 publication Critical patent/WO2001046130A1/en

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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C201/00—Preparation of esters of nitric or nitrous acid or of compounds containing nitro or nitroso groups bound to a carbon skeleton
    • C07C201/06—Preparation of nitro compounds
    • C07C201/08—Preparation of nitro compounds by substitution of hydrogen atoms by nitro groups
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C303/00—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides
    • C07C303/36—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides of amides of sulfonic acids
    • C07C303/40—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides of amides of sulfonic acids by reactions not involving the formation of sulfonamide groups

Definitions

  • the present invention relates to a process for the production of diphenyl ether compounds which are useful as herbicides.
  • it relates to a process for obtaining herbicidal diphenyl ether products on an industrial scale.
  • R 1 is hydrogen or C,-C 6 alkyl, C 2 -C 6 alkenyl or C 2 -C 6 alkynyl (any of which may optionally be substituted with one or more substituents selected from halogen and OH) or COOH, COH, COOR 4 , COR 6 , CONR 4 R 5 or CONHSO 2 R 4 ;
  • R 4 and R 5 are each independently hydrogen or C,-C 4 alkyl optionally substituted with one or more halogen atoms;
  • R 6 is a halogen atom or a group R 4 ;
  • R 2 is hydrogen or halo;
  • R 3 is C,-C 4 alkyl, C 2 -C 4 alkenyl or C 2 - C 4 alkynyl, any of which may optionally be substituted with one or more halogen atoms, or halo or, where appropriate, a salt thereof.
  • a preferred method of making fomesafen on an industrial scale is via acifluorfen which is made from 5-(2-chloro- ⁇ , ⁇ , ⁇ ,-trifluoro-4-tolyloxy)-benzoic acid (CTTBA).
  • CTBA 5-(2-chloro- ⁇ , ⁇ , ⁇ ,-trifluoro-4-tolyloxy)-benzoic acid
  • each step may be isolated at the end of the step or, more preferably, the steps may be telescoped together so that there is no isolation until the purified fomesafen end product is obtained.
  • Suitable solvents are haloalkanes (such as 1 ,2-dichloroethane or tetrachloroethylene), halobenzenes (such as fluorobenzene, chlorobenzene and dichlorobenzenes), alkoxybenzenes (such as anisole or phenetole), haloalkylbenzenes (such as benzotrifluoride), and esters (such as ethyl acetate or butyl acetate).
  • Preferred solvents are chloroalkanes especially 1 ,2-dichloroethane (or ethylene dichloride or EDC).
  • the acifluorfen is formed by nitration of
  • the CTTBA in the same solvent used to convert acifluorfen to fomesafen, the solvent being a chloroalkane, especially EDC.
  • the CTTBA is formed by the oxidation of the corresponding toluene and the CTTBA is extracted from the reaction mass using the same solvent that is used to convert acifluorfen to fomesafen, the solvent being a chloroalkane, especially EDC.
  • the CTTBA is suitably generated by the oxidation of the corresponding toluene using oxygen together with a catalyst (such as a cobalt or vanadium salt), at a temperature of 70°C to 150°C.
  • a catalyst such as a cobalt or vanadium salt
  • the product of the extraction step and/or the nitration step may be isolated at the end of the step or, more preferably, the steps may be telescoped together so that there is no isolation of product at the end of each of the extraction and nitration stages.
  • the nitrating agent may be nitric acid or a mixture of nitric and sulphuric acids although other types of nitrating agent may also be used. It is also advantageous to conduct the reaction in the presence of acetic anhydride and, in this case, it is preferred that the molar ratio of acetic anhydride to CTTBA is from about 1 :1 to 3:1.
  • the reaction temperature may be from about -15° to 15°C, more usually from about -10° to 10°C. It is advantageous to add the nitrating agent, over a period of time from 5 to 15 hours, or, more preferably, 6 to 12 hours. Most preferably the reaction is carried out using a mixture of nitric and sulphuric acids at 0 - 5°C.
  • the resultant product solution is water washed, to remove mineral acid and acetic acid then topped to remove residual water.
  • the conversion of acifluorfen to the acid chloride may be carried out by conventional methods, for example as set out in EP-A-0003416.
  • a suitable chlorinating agent such as thionyl chloride or phosgene
  • a catalyst such as triethylamine or dimethylformamide
  • the acid gases SO 2 and HCl may be removed, together with excess of the chlorinating agent by addition and distillative removal of further organic solvent.
  • the acid chloride may then be reacted with methane sulphonamide to give fomesafen.
  • This step may suitably be carried out by conventional methods, for example as set out in EP-A-0003416.
  • the acid chloride is coupled with MSAM using an excess of base such as potassium carbonate at 60 to 80°C, preferably at 80°C.
  • the inorganic by-products and excess MSAM are removed by washing with water.
  • the final product solution is topped to remove water.
  • the organic solvent level, in the final product solution is adjusted by topping off excess or by further additions and the product is then isolated by cooling to -10 to 30°C preferably 0°C.
  • a particular advantage in the use of EDC in the coupling reaction with MSAM is that the boiling point of the solvent is the upper temperature limit for process operation and thermal decomposition of the acid chloride during the reaction is avoided.
  • the product may then be purified using a chloroalkane solvent.
  • the purification may suitably involve filtration and washing with cold solvent or further recrystallisation from the solvent.
  • CTBA 5-(2-chloro- ⁇ , ⁇ , ⁇ ,-trifluoro-4-tolyloxy)-benzoic acid
  • composition of the topped oxidation mass was : 67% w/w CTTBA intermediate product 7% w/w organic impurities associated with CTTBA 25% w/w acetic acid
  • a 1 lb jar of the oxidation mass containing CTTBA was heated in a water bath to 95°C to melt the contents of the jar.
  • the molten contents were then charged to a 1 litre jacketed reaction vessel fitted with an anchor agitator, thermometer, Dean & Stark system with condenser and a nitrogen purge applied via a bubbler at the top of the condenser.
  • the reactor had been pre-charged with warm water (475ml at approx. 50 °C) which was agitated during the addition of the molten batch.
  • the product began to solidify and EDC (175 ml) was charged at which point the deposited solid dissolved and partitioned between the two layers.
  • the reactor contents were heated to approx.
  • # Mixed acid is a mixture of anhydrous nitric acid (33%) and sulphuric acid (67%) by weight.
  • the CTTBA solution in ECD (prepared as in step A) at 50°C, was charged to a clean dry 1 litre jacketed split reaction vessel fitted with thermometer, turbine agitator, Dean & Stark system fitted with condenser and a nitrogen purge attached via a bubbler to the top of the condenser.
  • the reactor contents were held at 50°C by jacket circulation and agitated whilst the sulphuric acid was charged.
  • the acetic anhydride was then charged and the reactor contents cooled to 0°C by applying external cooling to the reactor jacket.
  • the mixed acid was slowly charged to the reactor, using a syringe pump and teflon cannular via a suba seal cap on the reactor, over a period of approximately 2 hrs. During this addition the temperature was controlled at 0 - 5°C by periodically stopping the mixed acid addition. A sample was withdrawn for HPLC after a further 15 minute stir to check for completion of nitration - the analysis showed that the reaction was complete and needed no further mixed acid addition. The reaction mass was then quenched with 250 ml of cold water - the temperature rose to approximately 35°C and the reaction mass allowed to stand overnight without heating or agitation. The following day work-up was effected by agitating the reactor contents whilst heating to 60°C.
  • the acifluorfen in EDC solution at 50°C was charged to a clean dry 1 litre split reaction vessel fitted with turbine agitator, thermometer, Dean & Stark system fitted with condenser and a nitrogen purge fed in at the top of the condenser via a bubbler.
  • the reactor contents were heated to 70°C (by external bath heating - bath set at 75°C) and agitated.
  • the thionyl chloride was then charged, via syringe pump fitted with a Teflon cannular fed in through a suba seal on the reactor, over a period of just under 2 hrs . After complete addition of the thionyl chloride the reactor contents were agitated and heated at 70°C to ensure complete reaction.
  • the methanesulphonamide (MSAM) together with 70 gm of EDC were charged to a clean dry 1 litre jacketed split reaction vessel fitted with a turbine agitator, thermometer, Dean & Stark fitted with condenser and nitrogen purge fed in via a bubbler on the condenser outlet.
  • the mixture was heated up to 80°C whilst agitating at ⁇ 400 rpm.
  • Further EDC was added until the methanesulphonamide had dissolved at 80°C - a further 403.4 gm. Potassium carbonate was then charged to the reactor and the slurry stirred for a further 1 hr.
  • the required AA acid chloride (prepared as in step C) was then mixed with EDC to dilute to an AA acid chloride concentration of ⁇ 17%.
  • the diluted acid chloride solution was then charged to the reactor slurry over ⁇ 4 hrs.
  • the reaction mass was adjusted to 55°C, warm water (70 ml) added and the mixture stirred for 30 minutes before stopping the agitation and allowing the two phases to separate.
  • the upper aqueous layer was removed by vacuum.
  • a further warm water wash was then applied (100 ml) stirred for 30 minutes then separated as with the first wash.
  • the reactor contents were then heated up to reflux and were azeotropically dried before the purification stage.
  • the weight of product solution was determined and analysis carried out to determine the fomesafen yield. Yield : 87.9 % approximate crude product composition 2'-nitro 10.8 pph
  • the EDC solution of crude fomesafen after azeotrope drying , was held at 80° C in a 1 litre jacketed reaction vessel fitted with thermometer, turbine agitator, Dean & Stark fitted with condenser and nitrogen purge fed in via a bubbler on the condenser outlet.
  • the reactor contents were agitated at 400 rpm and heated to reflux in order to remove EDC (200 ml removed) - the circulating bath temperature was set to 98° C to achieve this.
  • the agitation was reduced to 100 m and the solution was cooled in 10° C steps and holding for 15 minutes for each step, down to a temperature of 0° C.
  • a 750 ml split reaction flask fitted with reflux condenser, thermometer, probe for bath controller and nitrogen purge was heated by an external oil bath and connected to a caustic scrubber system.
  • the reactor was charged with acifluorfen (62.0 gm ⁇ 0.166 equivalents), dimethyl formamide (0.185 gm ⁇ 0.0025 equivalents) and anisole (242 gm).
  • the mixture was heated to 70°C and agitated.
  • thionyl chloride (26.4 gm ⁇ 0.215 equivalents) was charged over an hour by syringe pump.
  • the reaction was then heated for a further 1.5 hour, after complete addition of the thionyl chloride, to give a clear yellow solution.
  • the reaction mass was then allowed to self cool to 50°C, at which point the apparatus was configured for distillation and a total of 2.5 gm of contaminated anisole

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)

Abstract

A process for producing fomesafen from acifluorfen comprises the steps of (a) converting acifluorfen to its acid chloride, (b) coupling the acid chloride so formed with methanesulphonamide to form crude fomesafen and (c) purifying the crude fomesafen, characterised in that each of the steps is carried out in a single common solvent, which is preferably a chloroalkane. Preferably the steps are telescoped together so that there is no isolation of the product for any step until fomesafen is obtained.

Description

PROCESS FOR THE PREPARATION OF DI PHENYL ETHER COMPOUNDS
The present invention relates to a process for the production of diphenyl ether compounds which are useful as herbicides. In particular, it relates to a process for obtaining herbicidal diphenyl ether products on an industrial scale.
The problems associated with producing diphenyl ether herbicides on an industrial scale are discussed in WO 97/10200 and WO 97/10199 in which there are disclosed processes for making compounds of formula
Figure imgf000002_0001
wherein R1 is hydrogen or C,-C6 alkyl, C2-C6 alkenyl or C2-C6 alkynyl (any of which may optionally be substituted with one or more substituents selected from halogen and OH) or COOH, COH, COOR4, COR6, CONR4R5 or CONHSO2R4; R4 and R5 are each independently hydrogen or C,-C4 alkyl optionally substituted with one or more halogen atoms; R6 is a halogen atom or a group R4; R2 is hydrogen or halo; R3 is C,-C4 alkyl, C2-C4 alkenyl or C2- C4 alkynyl, any of which may optionally be substituted with one or more halogen atoms, or halo or, where appropriate, a salt thereof. More especially the disclosures deal with the commercially known herbicides 5-(2-chloro-α,α,α-trifluoro-4-tolyloxy)-2-nitrobenzoic acid (acifluorfen) and 5-(2-chloro-α,α,α-trifluoro-4-tolyloxy)-N- methanesulphonyl- 2-nitrobenzamide (fomesafen).
A preferred method of making fomesafen on an industrial scale is via acifluorfen which is made from 5-(2-chloro-α,α,α,-trifluoro-4-tolyloxy)-benzoic acid (CTTBA). This compound is produced by oxidation of the corresponding tolyl compound which is in turn obtained from the condensation of 3-hydroxybenzoic acid and 3,4- dichlorobenzotrifluoride.
Because the final product (fomesafen) is required in sufficient purity to meet strict product registration standards the process normally also involves one or more purification procedures. The synthesis of acifluorfen and its conversion to fomesafen has been the subject of intensive research in an effort to improve one or more of the process steps. Thus for example in WO97/10200 there is disclosed a purification method for acifluorfen or fomesafen, while a set of improved nitration conditions is disclosed in WO97/10199. Another set of possible nitration conditions is disclosed in WO 98/19978. However no processes are known which can perform most or all of the above reactions using a single solvent. This is undoubtedly because the range of reaction conditions is very demanding and it is not at all apparent if a process using a single common solvent is possible.
The applicants have now devised a single common solvent process in which acifluorfen is converted to purified fomesafen. There is therefore provided a process for producing fomesafen from acifluorfen comprising the steps of
converting acifluorfen to its acid chloride
Figure imgf000003_0001
- coupling the acid chloride so formed with methanesulphonamide (MSAM) to form crude fomesafen and
Figure imgf000003_0002
- purifying the crude fomesafen characterised in that each of the steps is carried out in a single common solvent.
The product of each step may be isolated at the end of the step or, more preferably, the steps may be telescoped together so that there is no isolation until the purified fomesafen end product is obtained.
Suitable solvents are haloalkanes (such as 1 ,2-dichloroethane or tetrachloroethylene), halobenzenes (such as fluorobenzene, chlorobenzene and dichlorobenzenes), alkoxybenzenes (such as anisole or phenetole), haloalkylbenzenes (such as benzotrifluoride), and esters (such as ethyl acetate or butyl acetate). Preferred solvents are chloroalkanes especially 1 ,2-dichloroethane (or ethylene dichloride or EDC).
In a further aspect of the invention the acifluorfen is formed by nitration of
Figure imgf000004_0001
CTTBA in the same solvent used to convert acifluorfen to fomesafen, the solvent being a chloroalkane, especially EDC. In yet a further aspect of the invention the CTTBA is formed by the oxidation of the corresponding toluene and the CTTBA is extracted from the reaction mass using the same solvent that is used to convert acifluorfen to fomesafen, the solvent being a chloroalkane, especially EDC.
The CTTBA is suitably generated by the oxidation of the corresponding toluene using oxygen together with a catalyst (such as a cobalt or vanadium salt), at a temperature of 70°C to 150°C.
The product of the extraction step and/or the nitration step may be isolated at the end of the step or, more preferably, the steps may be telescoped together so that there is no isolation of product at the end of each of the extraction and nitration stages. In one suitable method for the nitration reaction, the nitrating agent may be nitric acid or a mixture of nitric and sulphuric acids although other types of nitrating agent may also be used. It is also advantageous to conduct the reaction in the presence of acetic anhydride and, in this case, it is preferred that the molar ratio of acetic anhydride to CTTBA is from about 1 :1 to 3:1. The reaction temperature may be from about -15° to 15°C, more usually from about -10° to 10°C. It is advantageous to add the nitrating agent, over a period of time from 5 to 15 hours, or, more preferably, 6 to 12 hours. Most preferably the reaction is carried out using a mixture of nitric and sulphuric acids at 0 - 5°C. The resultant product solution is water washed, to remove mineral acid and acetic acid then topped to remove residual water. The conversion of acifluorfen to the acid chloride may be carried out by conventional methods, for example as set out in EP-A-0003416. It is preferred to perform the reaction with a suitable chlorinating agent such as thionyl chloride or phosgene in the presence of a catalyst such as triethylamine or dimethylformamide at temperature of 60 to 80°C, preferably 70°C . The acid gases (SO2 and HCl) may be removed, together with excess of the chlorinating agent by addition and distillative removal of further organic solvent.
The acid chloride may then be reacted with methane sulphonamide to give fomesafen. This step may suitably be carried out by conventional methods, for example as set out in EP-A-0003416. In a preferred process the acid chloride is coupled with MSAM using an excess of base such as potassium carbonate at 60 to 80°C, preferably at 80°C. The inorganic by-products and excess MSAM are removed by washing with water. The final product solution is topped to remove water. The organic solvent level, in the final product solution, is adjusted by topping off excess or by further additions and the product is then isolated by cooling to -10 to 30°C preferably 0°C. A particular advantage in the use of EDC in the coupling reaction with MSAM is that the boiling point of the solvent is the upper temperature limit for process operation and thermal decomposition of the acid chloride during the reaction is avoided.
The product may then be purified using a chloroalkane solvent. The purification may suitably involve filtration and washing with cold solvent or further recrystallisation from the solvent.
Using the process invention, it is possible to obtain fomesafen of desired quality in good yield enabling the industrial operation of the process with a single solvent.
The invention will now be further illustrated with reference to the following examples.
EXAMPLE 1
The preparation of fomesafen in EDC
Step A
Extraction of 5-(2-chloro-α,α,α,-trifluoro-4-tolyloxy)-benzoic acid (CTTBA) from the oxidation reaction mass
Materials
Figure imgf000006_0001
* Composition of the topped oxidation mass was : 67% w/w CTTBA intermediate product 7% w/w organic impurities associated with CTTBA 25% w/w acetic acid
A 1 lb jar of the oxidation mass containing CTTBA was heated in a water bath to 95°C to melt the contents of the jar. The molten contents were then charged to a 1 litre jacketed reaction vessel fitted with an anchor agitator, thermometer, Dean & Stark system with condenser and a nitrogen purge applied via a bubbler at the top of the condenser. The reactor had been pre-charged with warm water (475ml at approx. 50 °C) which was agitated during the addition of the molten batch. The product began to solidify and EDC (175 ml) was charged at which point the deposited solid dissolved and partitioned between the two layers. The reactor contents were heated to approx. 77°C by external water bath circulation (bath at 80°C) for 30 minutes before stopping the agitation and allowing the reactor contents to separate. The upper aqueous layer was removed by suction and a warm water wash (506ml) was charged to the reactor, stirred for 30 minutes and then settled before removing the upper aqueous layer as before. The reactor contents were then heated to reflux to remove residual water. After the system had been azeotropically dried a fixed 'balance' charge of EDC was made to dilute the CTTBA in EDC solution to the safe concentration for the following nitration stage.
Yield : Product solution weight 1326.9 g, Product solution concentration 22.1 % 100% wt of CTTBA isolated 293.1 gm Step B
Nitration of CTTBA to acifluorfen
Materials
Figure imgf000007_0001
# Mixed acid is a mixture of anhydrous nitric acid (33%) and sulphuric acid (67%) by weight.
The CTTBA solution in ECD (prepared as in step A) at 50°C, was charged to a clean dry 1 litre jacketed split reaction vessel fitted with thermometer, turbine agitator, Dean & Stark system fitted with condenser and a nitrogen purge attached via a bubbler to the top of the condenser. The reactor contents were held at 50°C by jacket circulation and agitated whilst the sulphuric acid was charged. The acetic anhydride was then charged and the reactor contents cooled to 0°C by applying external cooling to the reactor jacket. On reaching 0°C the mixed acid was slowly charged to the reactor, using a syringe pump and teflon cannular via a suba seal cap on the reactor, over a period of approximately 2 hrs. During this addition the temperature was controlled at 0 - 5°C by periodically stopping the mixed acid addition. A sample was withdrawn for HPLC after a further 15 minute stir to check for completion of nitration - the analysis showed that the reaction was complete and needed no further mixed acid addition. The reaction mass was then quenched with 250 ml of cold water - the temperature rose to approximately 35°C and the reaction mass allowed to stand overnight without heating or agitation. The following day work-up was effected by agitating the reactor contents whilst heating to 60°C. After an hour stir the agitation was stopped and the two phases allowed to separate. The upper pale yellow aqueous layer was then separated, from the lower red organic layer, by suction. Two further 250 ml cold water washes were then applied, the reactor contents then heated to 60°C, with agitation, and treated in the same manner as the first wash. Residual interfacial material and water stayed with the organic phase after separation and the water was removed by agitating the reactor contents, heating the mixture to reflux via the Dean & Stark facilitating separation of the water and recycling the EDC. Yield 89.2 %
Step C
Chlorination to acifluorfen acid chloride
Materials
Figure imgf000008_0001
The acifluorfen in EDC solution at 50°C was charged to a clean dry 1 litre split reaction vessel fitted with turbine agitator, thermometer, Dean & Stark system fitted with condenser and a nitrogen purge fed in at the top of the condenser via a bubbler. The reactor contents were heated to 70°C (by external bath heating - bath set at 75°C) and agitated. The thionyl chloride was then charged, via syringe pump fitted with a Teflon cannular fed in through a suba seal on the reactor, over a period of just under 2 hrs . After complete addition of the thionyl chloride the reactor contents were agitated and heated at 70°C to ensure complete reaction. A sample of the acid chloride was taken for analysis by GLC. The analysis showed a little unreacted AA was still present - a calculated extra charge of thionyl chloride was added and the reaction heated until all gas evolution stopped. The reaction product obtained contained thionyl chloride, sulphur dioxide and hydrogen chloride gas impurities. In order to remove these impurities two successive additions of EDC were made, each addition being half the volume of the initial product solution, the additional EDC was then removed by distillation.
Yield : 92.6% Step D
Preparation of fomesafen from aciflourfen acid chloride
Materials
Figure imgf000009_0001
The methanesulphonamide (MSAM) together with 70 gm of EDC were charged to a clean dry 1 litre jacketed split reaction vessel fitted with a turbine agitator, thermometer, Dean & Stark fitted with condenser and nitrogen purge fed in via a bubbler on the condenser outlet. The mixture was heated up to 80°C whilst agitating at ~ 400 rpm. Further EDC was added until the methanesulphonamide had dissolved at 80°C - a further 403.4 gm. Potassium carbonate was then charged to the reactor and the slurry stirred for a further 1 hr. The required AA acid chloride (prepared as in step C) was then mixed with EDC to dilute to an AA acid chloride concentration of ~ 17%. The diluted acid chloride solution was then charged to the reactor slurry over ~ 4 hrs. The reaction mass was adjusted to 55°C, warm water (70 ml) added and the mixture stirred for 30 minutes before stopping the agitation and allowing the two phases to separate. The upper aqueous layer was removed by vacuum. A further warm water wash was then applied (100 ml) stirred for 30 minutes then separated as with the first wash. The reactor contents were then heated up to reflux and were azeotropically dried before the purification stage. The weight of product solution was determined and analysis carried out to determine the fomesafen yield. Yield : 87.9 % approximate crude product composition 2'-nitro 10.8 pph
6'-nitro 5.6 pph
5-CF3 7.3 pph acifluorfen 4.3 pph Step E
Purification of fomesafen
Materials
Figure imgf000010_0001
The EDC solution of crude fomesafen, after azeotrope drying ,was held at 80° C in a 1 litre jacketed reaction vessel fitted with thermometer, turbine agitator, Dean & Stark fitted with condenser and nitrogen purge fed in via a bubbler on the condenser outlet. The reactor contents were agitated at 400 rpm and heated to reflux in order to remove EDC (200 ml removed) - the circulating bath temperature was set to 98° C to achieve this. In order to obtain purified fomesafen the agitation was reduced to 100 m and the solution was cooled in 10° C steps and holding for 15 minutes for each step, down to a temperature of 0° C. At each step the agitation was stopped and the supernatant mother liquor sampled to determine the product concentration. The reactor contents were then filtered on a sintered nutche and the reactor washed clean with a little cold EDC which was then used to wash the product cake. The product cake was then air dried. Yield : 82.1%
Strength : 88.8%.
approximate crude product composition 2'-nitro 0.4 pph
6'-nitro 0.2 pph
5-CF3 2.2 pph acifluorfen 0.4 pph
where pph = parts of impurity x 100 parts of fomesafen 1 EXAMPLE 2
The preparation of fomesafen in anisole
Step A
Conversion of acifluourfen to its acid chloride
A 750 ml split reaction flask fitted with reflux condenser, thermometer, probe for bath controller and nitrogen purge was heated by an external oil bath and connected to a caustic scrubber system. The reactor was charged with acifluorfen (62.0 gm ≡ 0.166 equivalents), dimethyl formamide (0.185 gm ≡ 0.0025 equivalents) and anisole (242 gm). The mixture was heated to 70°C and agitated. On achieving temperature thionyl chloride (26.4 gm ≡ 0.215 equivalents) was charged over an hour by syringe pump. The reaction was then heated for a further 1.5 hour, after complete addition of the thionyl chloride, to give a clear yellow solution. The reaction mass was then allowed to self cool to 50°C, at which point the apparatus was configured for distillation and a total of 2.5 gm of contaminated anisole
(containing thionyl chloride HCl and SOCl2) was removed (at approx. 50°C pot temperature and 15 mbar pressure) - distillation was relatively smooth. Vacuum was relieved with nitrogen and the product solution bottled off and analysed by GLC.
Step B
Formation of crude fomesafen
A slurry of potassium carbonate (7.8 gm ≡ 0.055 equivalents), anisole (48.6 gm) and Methane Sulphonamide (MSAM 3.22 gm ≡ 0.0322 equivalents) was agitated in a 250 ml split reaction vessel and heated on an oil bath to 70°C. A portion of acifluorfen acid chloride (45 gm @ 22.2 % ≡ 0.0263 equivalents) was charged to a syringe pump and then run into the MSAM slurry over a period of approximately 3.5 hours. The reaction was then allowed to stir at 70°C for 30 minutes then sampled to check for completion of reaction. The reaction was quenched with water (100 gm) and the two phases separated, extra water was required to improve separation. The two layers were then separated and analysed giving a yield of 96.0% as fomesafen in the aqueous phase. Step C
Purification of crude fomesafen
Crude dry fomesafen paste (9.66 gm) was charged, in small portions, to anisole (50 gm) contained in a 100 ml four necked flask fitted with a thermometer and a ptfe paddle agitator. The slurry was agitated and heated, during the addition, with an oil bath to 130°C. Each portion of paste was charged after the previous sample had dissolved. When the system had reached saturation at 130°C the reaction mass was allowed to self cool and crystallise. The resultant product slurry was filtered off and the paste pulled 'dry' on a nutche before discharging, weighing and analysing. A grey paste (4.6 gm) of solids 94.3% and strength on dry of 84.3% was obtained giving a yield of 64% based on fomesafen charge.

Claims

1. A process for producing fomesafen from acifluorfen comprising the steps of
- converting acifluorfen to its acid chloride - coupling the acid chloride so formed with methanesulphonamide (MSAM) to form crude fomesafen and
- purifying the crude fomesafen characterised in that each of the steps is carried out in a single common solvent.
2. A process according to claim 1 wherein the steps are telescoped together so that there is no isolation of the product of any step until purified fomesafen is obtained.
3. A process according to claim 1 wherein the solvent is selected from haloalkanes, halobenzenes, alkoxybenzenes, haloalkylbenzenes and esters.
4. A process according to claim 3 in which the solvent is a chloroalkane.
5. A process according to claim 4 in which the solvent is 1 ,2-dichloroethane.
6. A process according to claim 4 in which the acifluorfen is produced by nitration of
5-(2-chloro-α,α,α,-trifluoro-4-tolyloxy)-benzoic acid in a chloroalkane.
7. A process according to claim 6 in which the nitrating agent is nitric acid or a mixture of nitric and sulphuric acids and in which the reaction takes place in the presence of acetic anhydride, the molar ratio of 5-(2-chloro-α,α,α,-trifluoro-4-tolyloxy)-benzoic acid to acetic anhydride being from about 1 : 1 to 3 : 1.
8. A process according to claim 6 or 7 in which the 5-(2-chloro-α,α,α,-trifluoro-4- tolyloxy)-benzoic acid is extracted from a reaction mass using a chloralkane as a solvent.
9. A process according to claim 8 wherein the 5-(2-chloro-α,α,α,-trifluoro-4-tolyloxy)- benzoic acid is generated by oxidation of the corresponding toluene using oxygen together with a catalyst it a temperature of from 70°C to 150°C to form a reaction mass from which the 5-(2-chloro-α, ,α,-trifluoro-4-tolyloxy)-benzoic acid is extracted.
10. A process according to claim 8 or 9 wherein the steps are telescoped together so that there is no isolation of the product of any step until purified fomesafen is obtained.
11. A process for producing fomesafen from 5-(2-chloro-α,α,α,-trifluoro-4-tolyloxy)- benzoic acid which comprises the steps of: (i) Extracting 5-(2-chloro-α,α,α,-trifluoro-4-tolyloxy)-benzoic acid from an oxidation reaction mass using a chloroalkane solvent;
(ii) nitrating 5-(2-chloro-α,α,α,-trifluoro-4-tolyloxy)-benzoic acid in the same chloralkane solvent to form acifluorfen
(iii) converting acifluorfen to its acid chloride (iv) coupling the acid chloride so formed with methanesulphonamide (MSAM) to form crude fomesafen and
(v) purifying the crude fomesafen wherein each of the steps (i) to (iv) is carried out in a single common chloroalkane solvent and the steps are telescoped together so that there is no isolation of the product for any step until fomesafen is obtained.
PCT/GB2000/004731 1999-12-22 2000-12-11 Process for the preparation of diphenyl ether compounds WO2001046130A1 (en)

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EP00985526A EP1246796B1 (en) 1999-12-22 2000-12-11 Process for the preparation of diphenyl ether compounds
DE60019337T DE60019337T2 (en) 1999-12-22 2000-12-11 PROCESS FOR PREPARING DIPHENYL ETHER CONNECTION
HU0204189A HUP0204189A3 (en) 1999-12-22 2000-12-11 Process for the preparation of diphenyl ether compounds
JP2001547041A JP4619602B2 (en) 1999-12-22 2000-12-11 Method for producing diphenyl ether compound
AT00985526T ATE292620T1 (en) 1999-12-22 2000-12-11 METHOD FOR PRODUCING DIPHENYL ETHER COMPOUND
US10/168,611 US6790991B2 (en) 1999-12-22 2000-12-11 Process for the preparation of diphenyl ether compounds
AU21939/01A AU2193901A (en) 1999-12-22 2000-12-11 Process for the preparation of diphenyl ether compounds
IL14986900A IL149869A0 (en) 1999-12-22 2000-12-11 Process for the preparation of diphenyl ether compounds

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GBGB9930369.5A GB9930369D0 (en) 1999-12-22 1999-12-22 Chemical process

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CN1315778C (en) * 2005-09-18 2007-05-16 大连理工大学 1,2-disubstituted ally/arylox yphthalate compounds and use thereof
CN102030655B (en) * 2010-10-21 2013-03-27 上虞颖泰精细化工有限公司 Synthesis method of diphenyl ether derivate, combined production method of oxyfluorfen and acifluorfen and synthesis method of oxyfluorfen
CN102329255B (en) * 2011-10-31 2013-11-13 江苏长青农化股份有限公司 Process for synthesizing fomesafen through directional nitration
CN102516085A (en) * 2011-12-13 2012-06-27 江苏长青农化股份有限公司 Synthesis method of 5-[2-chloro-4-(trifluoromethyl)phenoxy]-2-nitrobenzoic acid
CN115403488B (en) * 2021-05-27 2024-07-19 江苏联化科技有限公司 Preparation method of fomesafen

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GB2140417A (en) * 1983-05-17 1984-11-28 Rhone Poulenc Agrochimie A process for the preparation of N-aryloxybenzoyl sulphonamides
EP0274194A1 (en) * 1986-11-25 1988-07-13 Imperial Chemical Industries Plc Process for the preparation of 2-nitro-5-phenoxy-N-alkylsulfonyl benzamides by nitration
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GB9930369D0 (en) 2000-02-09
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AR043092A1 (en) 2005-07-20
KR100733515B1 (en) 2007-06-28
KR20020067558A (en) 2002-08-22
AU2193901A (en) 2001-07-03
CN1182110C (en) 2004-12-29
JP2003518088A (en) 2003-06-03
EP1246796B1 (en) 2005-04-06
DE60019337T2 (en) 2005-09-22
EP1246796A1 (en) 2002-10-09
US6790991B2 (en) 2004-09-14
IL149869A0 (en) 2002-11-10
CN1411437A (en) 2003-04-16
US20030045754A1 (en) 2003-03-06
DE60019337D1 (en) 2005-05-12
ATE292620T1 (en) 2005-04-15

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