Classifications

• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C319/00—Preparation of thiols, sulfides, hydropolysulfides or polysulfides
  • C07C319/14—Preparation of thiols, sulfides, hydropolysulfides or polysulfides of sulfides
  • C07C319/20—Preparation of thiols, sulfides, hydropolysulfides or polysulfides of sulfides by reactions not involving the formation of sulfide groups
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/10—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of rare earths
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
  • B01J23/32—Manganese, technetium or rhenium
  • B01J23/34—Manganese
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
  • B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
  • B01J37/0063—Granulating
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
  • B01J37/04—Mixing
• • C—CHEMISTRY; METALLURGY
  • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
  • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
  • C12P11/00—Preparation of sulfur-containing organic compounds

Definitions

• the present invention relates to the catalytic conversion of 2-hydroxy-
• HMTBN 4-methylthiobutanenitrile
• HMTBM 2-hydroxy-4-methylthiobutanamide
• the HMTBM thus obtained can be used for example for the production of 2-hydroxy-4-methylthiobutanoic acid (HMTBA) hydroxyanalogue of methionine, methionine being an essential amino acid widely used as a feed additive in animal nutrition.
• HMTBA 2-hydroxy-4-methylthiobutanoic acid
• HMTBN 2-hydroxy-4-methylthiobutyronitrile
• HMTBM 2-hydroxy-4-methylthiobutyramide
• HMTBA 2-hydroxy-4-methylthiobutanoic acid
• HMTBM resulting in the co-production of a very large amount of inorganic products difficult to exploit. Indeed, the catalytic activity of the strong mineral acids with respect to the HMTBN is such that all the introduced HMTBN is transformed very rapidly.
• the HMTBM produced may especially react with water to form HMTBA and ammonia. In the case of sulfuric acid, for example, it may react with the ammonia released to form ammonium sulphate which must then be treated.
• one of the proposed alternatives to this acidic hydration is an enzymatic process in which a nitrile hydratase, such as Rhodococcus (according to US 6 900 037 B2 and US Pat.
• WO 2002/070717 A2 for example, can transform HMTBN into HMTBM.
• the major disadvantage that penalizes this process lies in the difficulty of synthesize enzymes and extract them from the reaction medium after obtaining HMTBM.
• a solution proposed by the patent WO 2002/00869 for extracting the enzymes from the reaction medium is the use of insoluble granules in water containing the enzyme.
• the process for obtaining these granules is complicated and the catalytic activity of the enzymes in the granules is very much reduced.
• the low catalytic activity makes it possible to be very selective in HMTBM but the duration of the transformation reaction of HMTBN into HMTBM must be lengthened.
• Heterogeneous catalysis methods are also known.
• the hydration of HMTBN is carried out in the presence of a mass-based manganese oxide catalyst in a water / acetone mixture (450/150).
• the amount of manganese oxide used is 0.75 moles per 1 mole of cyanohydrin. It appeared that this reaction is difficult to reproduce because it is strongly related to the nature of the manganese oxide used. For example, in the presence of pyrolusite, no hydration reaction occurs.
• the hydration conditions of the HMTBN according to this patent do not appear easy to optimize to obtain a reproducible yield in the absence of secondary products.
• Patent FR 2,750,987 describes the hydration reaction of HMTBN or methylpropioaminonitrile cyanohydrin to the corresponding amide at low temperature (between 0 ° C. and 60 ° C.) in water in the presence of a catalyst with base of manganese oxide deposited on silica without any appearance of oxidation products on the sulfur atom.
• the molar ratio MnO 2 / HMTBN or MnO 2 / cyanohydrin of the methylthiopropioaminotrile is between 0.05 and 1.5.
• the weight ratio of the manganese oxide to the silica is preferably between 5 and 10%. It appears in the examples of this patent FR 2,750,987 that supporting manganese oxide on silica makes it possible to improve the selectivity of the reaction, but the small amounts of deposited active phase require long reaction times and / or Cyanhydrin very weak.
• the amount of water used in the reaction medium is not critical for the reaction but that if the reaction time is too long and / or the temperature too high, part of the HMTBM formed can react with the water of the reaction medium to form HMTBA and / or produce secondary products of condensation of HMTBM.
• the ammonia released induces an increase the hydrogen potential (pH) of the reaction medium which, at basic pH, causes the degradation of HMTBN which has not yet reacted and therefore an overall decrease in the production of HMTBM.
• patent EP 0 601 195 A1 which describes a process for producing HMTBA in three successive stages, the first of which consists in the catalytic conversion of HMTBN into HMTBM in the presence of a heterogeneous catalyst, preferably of manganese oxide. or alkali metal borate (sodium tetraborate), it is recommended to substitute a portion of the amount of water of the reaction medium with a water-soluble organic solvent, such as acetone or methanol, and add sulfuric acid to improve the selectivity of the reaction. According to this patent, sulfuric acid is added to improve the performance of the reaction but in very limited amounts to prevent the formation of ammonia. In the examples, the best yield of HMTBM obtained after 6 hours of reaction at 60 ° C. in the presence of manganese oxide and sulfuric acid in a water / acetone solvent is 89%.
• the state of the art shows that it is difficult to reconcile a strong catalytic activity for the hydration of HMTBN and a good selectivity in HMTBM.
• the best performances are described for catalysts based on manganese oxide.
• the best selectivities are obtained for manganese oxide supported on silica.
• the low levels of supported manganese oxides involve long reaction times or reaction media containing very low concentrations of HMTBN.
• One of the aims of the present invention is to provide an alternative to the methods described above but which does not have the disadvantages.
• a first object of the present invention is to provide a sufficiently active and selective solid catalyst to produce 2-hydroxy-4-methylthiobutanamide (HMTBM) from 2-hydroxy-4-methylthiobutanenitrile (HMTBN) in short reaction times. to limit the formation of unwanted by-products and without the addition of strong mineral acids so as not to produce inorganic waste and to prevent degradation of HMTBN.
• HMTBM 2-hydroxy-4-methylthiobutanamide
• HMTBN 2-hydroxy-4-methylthiobutanenitrile
• a first object of the invention is a process for the catalytic conversion of HMTBN to HMTBM, in the presence of a solid catalyst comprising an active phase, said catalyst being shaped and said conversion taking place in a substantially free-flowing medium. strong mineral acid.
• substantially free of strong mineral acid is meant, if any, a trace presence at most, a proportion of less than 0.1% by weight relative to the total weight of the medium.
• HMTBN in HMTBM consists of at least one metal oxide.
• the proportion of this active phase is preferably at least 30% by weight relative to the total weight of the catalyst.
• the constituent metallic elements of these oxides are advantageously chosen from the group comprising copper, nickel, iron, zirconium, manganese, cerium and their combinations.
• the preferred metal oxides are manganese oxide and cerium oxide, they may be present alone or in combination to promote the selective hydration of HMTBN to HMTBM.
• the diluent is chosen from the group comprising zirconium oxide, titanium oxide, alumina, silica, clays such as bentonites, attapulgite, and combinations thereof. . Its proportion is preferably at most 70% by weight relative to the total weight of the catalyst.
• Preferred diluent of the invention include silica, alumina and combinations thereof.
• the shaping of the catalyst generally comprises at least a first step of shaping the active phase, followed by a second heat treatment step.
• a shaping process there may be mentioned processes using wet granulation or extrusion, in the presence of a binder.
• the heat treatment step is often a drying stage (low temperature) between 50 0 C and 100 0 C, followed by a calcination step with the aim to reveal the active phase between 200 ° C and 600 0 C.
• Binder means any binder selected from water, natural polymers, organic polymers and sugars, characterized in that it will ensure the cohesion of the active phase and the diluent during the preparation of the catalyst.
• natural polymer any natural polymer, such as, for example, starch, gelatin, alginic acid, sodium alginate and combinations thereof.
• organic polymer any organic polymer, such as, for example, polyvinylpyrrolidone, methylcellulose, polyethylene glycol and combinations thereof.
• Sugar means any sugar, such as glucose, sucrose, sorbitol and combinations thereof.
• any binder which makes it possible to improve certain properties of the invention is suitable, binders which do not generate toxic compounds or which are not themselves toxic to the environment or for the catalytic reaction being preferred.
• a mixture of active phase powders and diluent is prepared, the proportions of which are determined by the composition of the desired shaped catalyst; small granules ( ⁇ 1 mm) of desired formulation are generated which are called primers;
• the primers are introduced into the plate to be granulated, also called bezel or pan granulator, to which the mixture of the active phase powders and diluent previously prepared is slowly added continuously and the binder solution is sprayed simultaneously;
• Granules are produced which are "naturally selected by centrifugation", out of the plate as soon as the desired particle size is reached, via rotational speed and inclination of the plate;
• the granules are dried and calcined.
• a second embodiment of the process for obtaining these compositions by granulation in a mixer - granulator Low or High Shear is used.
• mixers are equipped with one or more pale-type rotors, pins or plowshares which allows the powder mixture to move.
• This mode includes the following steps. a mixture of active phase powders and diluent is prepared, the proportions of which are determined by the composition of the desired shaped catalyst;
• the binder is incorporated in the form of a spray, which makes it possible to ensure the growth of the granules and to control the particle size distribution by controlling the quantity of binder introduced.
• the other important granulation parameters are those of the speed of rotation and contact time.
• a third embodiment of the process for obtaining these compositions by extrusion comprises the following steps:
• a mixture of active phase powders and diluent is prepared, the proportions of which are determined by the composition of the desired shaped catalyst; the binder is introduced;
• the mixture is kneaded until a paste is obtained; the dough thus obtained is introduced into a die of the desired diameter;
• the extrudates are dried and calcined.
• the extrudates can be continuously produced with an extruder in which the mixture of powders, ie active phases and diluents, is introduced, followed by the binder.
• a paste is thus generated in situ, in the screw, for example single or double screw, then extracted in the form of "spaghetti" whose length is controlled by the formulation or mechanically, for example with a rotary knife. They are then dried and calcined.
• a catalyst of the invention has strong activities for the selective hydration of HMTBN in very high HMTBM at temperatures between 0 0 C and 100 0 C, more particularly between 20 0 C and 90 ° C.
• the reaction time is advantageously greater than 45 minutes and preferably greater than 60 minutes.
• the catalytic hydration of HMTBN in HMTBM can be carried out in the liquid phase or in the gas phase. Under these conditions, the HMTBN is in solution, at a rate of 20 to 80% relative to the total weight of the solution. It may be in solution in a solvent or a mixture of solvents chosen from water, water-soluble solvents such as acetone and methanol.
• the HMTBN is present in a reaction medium from which it originates. It can for example be obtained by reaction of hydrogen cyanide with aldehyde-3- (methylthio) propionic acid.
• the catalytic hydration of HMTBN in HMTBM can be carried out in a closed reactor or continuously.
• the reaction can be carried out in a continuous reactor on a fixed bed of catalyst or in a perfectly stirred reactor, and in particular a continuous reaction on a fixed bed of catalyst is preferred.
• the process of the invention finds an interesting application in the preparation of 2-hydroxy-4-methylthiobutanoic acid (HMTBA), according to the following steps: the conversion of HMTBN into HMTBM is carried out by a process of the invention as defined above,
• the step of converting HMTBM to HMTBA can be carried out under conditions well known to those skilled in the art.
• this step can be carried out catalytically in the presence of a catalyst based on one or more metal oxides, preferably chosen from titanium dioxide and zirconium dioxide.
• This conversion step may also be carried out by hydrolysis in the presence of an acid, such as a mineral acid chosen from H 2 SO 4, H 3 PO 4 and HCl.
• an acid such as a mineral acid chosen from H 2 SO 4, H 3 PO 4 and HCl.
• the acid is H 2 SO 4
• the reaction conditions are those described in application EP-A-1 097 130.
• HMTBA can also be prepared from HMTBM enzymatically in the presence of an amidase.
• HMTBS ammonium salt
• the ammonium salts optionally in admixture with the HMTBA undergo a conversion treatment, advantageously chosen from a neutralization, an electrodialysis, a distillation.
• the neutralization step can be carried out on resins, or by acid neutralization.
• Rhodia cerium oxide HSA-5
• a conditated SB3 alumina and water as binder are used.
• a mixture of powders composed of 90% by weight of cerium oxide and 10% by weight of alumina is prepared. 10% primer weight of this composition is prepared in a plate to be granulated on the plate. The powder mixture is then slowly fed continuously and the water is sprayed simultaneously for granulation to be effective.
• the granules produced are "naturally selected by centrifugation", removed from the plate as soon as the granulometry is reached (4-5 mm), via rotation speed and inclination of the plate. They are recovered, dried in the oven for 12 hours at 60 ° C. and then calcined for 2 hours at 500 ° C.
• the powders are mixed with 90% by weight of alpha manganese oxide and 10% by weight of alumina.
• a mixture of powders is introduced into a Brabender kneader and 32 ml of purified water are introduced in 8 minutes. The mixing time after introduction of water is 20 minutes. The paste obtained is then introduced into the multi-hole die 1.5 mm. Generated spaghetti is smooth and breaks easily. They are dried in an oven at 60 0 C for 18 hours. These dry spaghetti are then calcined at 400 0 C and then plateau for 2 hours.
• the extrudates thus obtained after calcination have lengths which range between 3 and 20 mm.
• KMnO 4 (15.6g, 95.9 mmol) was dissolved in water (24OmL) at room temperature in a 1 liter monocolon.
• Silica 60 (Merck, 240 g) is then added and mechanically stirred for 2 hours.
• the water is then evaporated under vacuum using a rotary evaporator (bath at 60 ° C.).
• the violet powder obtained is then gradually added to a vigorously stirred solution of MnSO 4 -H 2 O (37.2 g, 220.1 mmol) in water (40OmL). Stirred for three hours and filtered the brownish solid on sintered glass. This solid is washed with water until total disappearance of the manganous ions (characterized by formation of a precipitate by treatment with ammonia) in the washing water.
• This example gives the results of measurement of the conversion of 2-hydroxy-4-methylthiobutanenitrile in the presence of the compositions of the preceding examples and in the manner that follows.
• the reaction mixture composed of a solution of 23% by weight of
• HMTBN in water is introduced into the Schott tube containing the catalyst.
• a magnetized bar is then introduced into the Schott tube and stirred to homogenize the reaction mixture.
• the Schott tube thus charged is then heated to 75 ° C. The initial time of the reaction is considered when the temperature of 75 ° C is reached.
• HMTBN initially introduced and the selectivity to different reaction products, such as HMTBM and HMTBA, at time t is calculated with respect to the amount of this product formed at time t and the amount of HMTBN at moment t.
• compositions of the invention exhibit catalytic activities which are greater than the catalyst described in patent FR 2,750,987 (C).
• the conversions of HMTBN are greater than 90% for the examples of the invention and their selectivities in HMTBM are greater than 70% whereas the comparative catalyst ( C) shows only 13% conversion of HMTBN and 63% selectivity to HMTBM.
• This example gives the results of measurement of the conversion of 2-hydroxy-4-methylthiobutyronitrile in the presence of catalyst B over time and in the manner that follows.
• Example 2 80 ml of catalyst B described in Example 2 are introduced into a batch reactor fixed flow recirculation bed. 180 ml of industrial HMTBN flux diluted in water so as to have 28% by weight of HMTBN in the reaction stream are introduced into the reactor.
• the reaction flow is circulated in the reactor with a circulation rate of 121 / h.
• the reactor is heated to a temperature of 75 ° C.
• the initial time of the reaction is considered when the temperature of 75 ° C is reached.
• Flow samples are taken during the reaction to follow the progress of the reaction. The quantities taken are very small and it is considered that the volume of the flow remains constant throughout the reaction.
• the composition of the samples taken is determined by HPLC.
• the conversion of HMTBN at time t is calculated with respect to the HMTBN initially introduced and the HMTBM selectivity at time t is calculated with respect to the amount of HMTBM at time t and the amount of HMTBN. transformed at the instant t.
• catalyst B is very active with respect to the hydration of HMTBN and very selective in HMTBM.
• the HMTBM formed is very stable over time and does not degrade in HMTBA.

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• 2007
  • 2007-07-31 FR FR0705592A patent/FR2919607B1/fr not_active Expired - Fee Related
• 2008
  • 2008-07-30 CN CN200880100621A patent/CN101765586A/zh active Pending
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