Classifications

• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
  • C07C45/51—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by pyrolysis, rearrangement or decomposition
  • C07C45/52—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by pyrolysis, rearrangement or decomposition by dehydration and rearrangement involving two hydroxy groups in the same molecule
• • 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
  • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
  • B01J27/06—Halogens; Compounds thereof
  • B01J27/132—Halogens; Compounds thereof with chromium, molybdenum, tungsten or polonium
• • 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
  • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
  • B01J27/06—Halogens; Compounds thereof
  • B01J27/135—Halogens; Compounds thereof with titanium, zirconium, hafnium, germanium, tin or lead
• • 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
  • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
  • B01J27/14—Phosphorus; Compounds thereof
  • B01J27/182—Phosphorus; Compounds thereof with silicon
• • 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
  • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
  • B01J27/14—Phosphorus; Compounds thereof
  • B01J27/186—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
  • B01J27/188—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium with chromium, molybdenum, tungsten or polonium
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C319/00—Preparation of thiols, sulfides, hydropolysulfides or polysulfides
  • C07C319/02—Preparation of thiols, sulfides, hydropolysulfides or polysulfides of thiols
  • C07C319/12—Preparation of thiols, sulfides, hydropolysulfides or polysulfides of thiols by reactions not involving the formation of mercapto groups
• • 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
  • C07C319/18—Preparation of thiols, sulfides, hydropolysulfides or polysulfides of sulfides by addition of thiols to unsaturated compounds

Definitions

• the present invention relates to a catalytic process for the manufacture of acrolein by dehydration of glycerol and the applications of such a process.
• Glycerol or glycerine
• Glycerol is understood to mean a purified or non-purified glycerol of natural origin derived from the hydrolysis of vegetable oils and / or animal fats, or a glycerol of synthetic origin, derived from petroleum, more or less purified or refined, or crude.
• Purified glycerol has a purity greater than or equal to 98%, obtained by distillation.
• Unpurified or only partially purified glycerol may be in solution in methanol and / or water when it comes for example from a transesterification of triglycerides.
• Glycerol also known as glycerine
• glycerine has long been known as a source of acrolein by thermal transformation, it is a product that is widely found in nature, in the form of esters (triglycerides), especially in all animal or vegetable oils and fats, which makes it a starting reagent available in quantity and in this, usable industrially. It is known that glycerol decomposes to give acrolein when heated to temperatures above 280 ° C. This weakly selective reaction is accompanied by the formation of numerous by-products, including acetaldehyde and hydroxyacetone, in addition to the total oxidation products CO, CO 2 .
• a catalyst which may consist of a silicon oxide and a mixed zirconium and tungsten oxide or a titanium oxide and a mixed zirconium oxide and detung stè ne; according to WO201 1 / 157959A1, a catalyst consisting of a zirconium oxide, a silicon oxide and a tungsten oxide is known for carrying out this conversion.
• a catalyst consisting of a zirconium oxide, a silicon oxide and a tungsten oxide is known for carrying out this conversion.
• the object of the invention is to overcome the problems encountered with the known catalysts in the dehydration reaction of glycerol with acrolein.
• the object of the present invention lies in the implementation of catalysts which, while providing an improvement over the above limitations, remain robust and regenerable, making it possible to produce acrolein directly from glycerol, in particular derived from biomass. .
• the invention further relates to an application of this reaction to the synthesis of aldehyde-3- (methylthio) propionic acid (MMP), 2-hydroxy-4-methylthiobutyronitrile (H MTB N), methionine and its analogs such as 2-hydroxy-4-methylthiobutanoic acid (HMTBA) and 2-oxo-4-methylthiobutanoic acid, as well as metal chelates (Zn, Ca, Cr, Zn, Cu ...) and the esters of these acids, such as the isopropyl ester of HMTBA, from acrolein.
• MMP aldehyde-3- (methylthio) propionic acid
• H MTB N 2-hydroxy-4-methylthiobutyronitrile
• methionine and its analogs such as 2-hydroxy-4-methylthiobutanoic acid (HMTBA) and 2-oxo-4-methylthiobutanoic acid, as well as metal chelates (Zn, Ca, Cr, Zn, Cu ”).
• Methionine, HMTBA, esters and chelates thereof, and analogs thereof are used in animal nutrition and in their synthetic industrial processes, acrolein is generally obtained by oxidation of propylene and / or propane.
• the oxidation of propylene to acrolein by air in the presence of water is partial, and the resulting crude product, based on acrolein, also contains unreacted propylene and propane, water and water. by-products of the oxidation reaction, including acids, aldehydes and alcohols.
• the invention relates to a process for the preparation of acrolein from glycerol, in which dehydration of glycerol is carried out in the presence of a catalyst MWOA, where MWO represents a mixture of simple oxides and / or oxides mixtures of tungsten and at least one metal M selected from zirconium, silicon, titanium, alumina and yttrium and A represents one or more Lewis bases, a said Lewis base corresponding to formula B ( R 1) p (R 2) q (R 3) r, where B is a member selected from C, S, P, O, N and the halides, R 1, R 2 and R 3 represent, independently of each other, H, an alkyl group in C1-C6, O, OH or OR where R represents a C1-C6 alkyl group, and the sum of p, q and r varies from 0 to 4.
• M represents at least two metals selected from zirconium, silicon, titanium, alumina
• this Lewis base (s) makes it possible to significantly reduce the duration of the setting in regime, while maintaining a conversion rate in glycerol, a selectivity and a high yield of acrolein over long periods.
• a representing one or more Lewis bases the value of the indices p, q and r, whose sum varies from 0 to 4, and can thus be equal to 0, 1, 2, 3 or 4, will be chosen according to the nature of element B.
• Suitable Lewis bases are selected from phosphate, carbonate, carboxylate, sulphate, borate, alcoholate, alcohols and halide anions and mixtures thereof.
• the preferred bases are those chosen from H x PO 4 (x "3) phosphate ions, x ranging from 0 to 2, H 3 PO 4 , borate ions, and F “ , CI “ , Br “ , I “ halides. , as well as their mixtures.
• the molar ratio of A / M surface varies from 0.005 to 0.5, more preferably it varies from 0.015 to 0.09; A corresponding to the total amount of Lewis bases.
• the Lewis base boosts the surface of the catalyst oxides. It can be added at any time in the synthesis of the catalyst, and in particular during the synthesis or once the catalyst is formed. If several Lewis bases are added, they can be incorporated, respectively, at different stages or not of the synthesis of the catalyst. In addition, and in order to preserve the catalytic performance of the catalysts thus prepared, these same dopa nts ag ents may also be added via the feed of the reactants during operation of the reactor.
• the oxides present in the catalyst are determined by a molar ratio W / sum of the elements M, different from W; this ratio preferably varies from 0.005 to 0.4, and more preferably from 0.01 to 0.1.
• the reaction according to the invention can be carried out in the gas phase or in the liquid phase, preferably in the gas phase.
• different process technologies can be used to supply the reactants, namely fixed bed process, fluidized process, or circulating fluidized method.
• the supply of different reagents, applied to the aforementioned reactors can be done individually or already in the form of pre-mixtures. It operates at a pressure of the order of atmospheric pressure and, preferably, at a substantially higher pressure.
• the regeneration of the catalyst can be separated from the catalytic reaction. It can for example be done ex situ by conventional regeneration methods, such as combustion under air or with a gaseous mixture containing molecular oxygen. According to the method of the invention, the regeneration can be done in situ because the temperatures and pressures at which the regeneration is done are close to the reaction conditions of the process.
• the reaction can be carried out in a conventional reactor for reaction in phase on a solid catalyst, but also in a catalytic distillation type reactor with regard to the difference between n gicerol (290 ° C) and acrolein (53 ° C). It is also possible consider a liquid phase process at a relatively low temperature which allows a continuous distillation of acrolein produced, thus limiting the consequent degradation reactions of acrolein.
• the experimental conditions of the gas phase reaction are preferably a temperature between 250 and 400 ° C at a pressure of between 1 and 10 bar.
• the reaction is carried out between 150 and 350 ° C. and at a pressure ranging from 3 to 70 bars.
• Another advantage of the process of the invention lies in the form of starting glycerol which can be in pure form or partially purified or in solution, in particular aqueous.
• an aqueous solution of glycerol is used.
• the glycerol concentration is preferably at least 1%, at most it varies from 10 to 50% by weight and preferably between 15 and 30% by weight in the reactor.
• the glycerol concentration should not be too high in order to avoid the spurious reactions that constrain the yield of acrolein, such as the formation of glycerol ethers or acetalization reactions between acrolein produced and unconverted glycerol.
• the glycerol solution must not be too diluted, because of a prohibitive energy cost induced by the evaporation of glycerol.
• Another subject of the invention is a process for the manufacture of 3-aldehyde (methoxyethyl) peroxide (MMP), 2-hydroxy-4-methylthiobutyronitrile (HMTBN), methionine 2-hydroxy-4-methylthiobutanoic acid (HMTBA), its metal chelates (Zn, Ca, Cr, Zn, Cu ...), and its esters, in particular the isopropyl ester, and 2-oxo-4 acid - methylthiobutanoic (KMB), its metal chelates (Zn, Ca, Cr, Zn, Cu ...), and its esters, from acrolein, which comprises the dehydration step of glycerol acrolein according to the invention.
• MMP 3-aldehyde
• HMTBN 2-hydroxy-4-methylthiobutyronitrile
• HMTBA methionine 2-hydroxy-4-methylthiobutanoic acid
• KMB 2-oxo-4 acid - methylthiobutanoic
• acrolein produced by the aforementioned process may contain impurities different from the conventional process, both in terms of quantity and nature.
• synthesis of acrylic acid or methionine or its hydroxyanalogue it may be envisaged to purify acrolein according to techniques known to those skilled in the art.
• Another object of the invention is the use of a catalyst as defined above, for converting glycerol to acrolein.
• Catalysts of the prior art, A, C, D and F are the subject of Examples 1, 3, 4 and 7, respectively.
• the catalysts of the invention, B, E and G are the subject of Examples 2, 5 and 8, respectively.
• the comparison of the performance between the catalysts A, C and D on the one hand and the catalysts B and D on the other hand is illustrated in Example 6 and that between the catalyst F and the catalyst G is illustrated in FIG. example 9.
• Catalysts B, E and G are further characterized by the atomic surface ratio AM measured by XPS (X-ray photoelectron spectroscopy); A corresponding to the total amount of base (s) of Lewis.
• the glycerol dehydration reaction is conducted on the indicated catalysts, at atmospheric pressure or substantially higher pressure, in a straight bed fixed bed reactor. The reactor is placed in an oven which keeps the catalyst at the reaction temperature of 300 ° C. The reactor is fed with an aqueous solution containing 20% by weight of glycerol. The aqueous glycerol solution is vaporized using a CE evaporator. M (Controlled Evaporator Mixer) Bronkhorst® in the presence of a nitrogen flow. The relative molar ratio of glycerol / water / nitrogen is 2.3 / 46.3 / 51.4.
• the GHSV hourly space velocity
• Catalyst A is of the silicon doped tungstic zirconia type, that is, a catalyst consisting of a mixture of zirconium oxide, tungsten oxide and silicon oxide.
• the preparation of this solid comprises the following three steps.
• the second step is to stabilize the hydrated zirconia hydroxide with silicic species by adding a solution of tetraethyl ortho-silicate, TEOS, Si (OC 2 H 5 ) (AIdrich, 99.999%).
• TEOS tetraethyl ortho-silicate
• Si OC 2 H 5
• AIdrich 99.999%.
• the last step is the exchange with tungstic acid H 2 WO 4
• the atomic ratio A / M of surface is 0.09 (with A representing the base of Lewis based on phosphate).
• Catalyst C is a tungsten zirconia, a mixture of zirconium oxide and tungsten oxide synthesized by Daiichi Kigenso (supplier reference: Z-104).
• the specific surface area of this catalyst is 77 m 2 / g and its molar W / M composition is 3.3 / 96.7.
• the catalyst D is of the tungsten zirconia type doped with silica, that is to say that it consists of a mixture of zirconium oxide, tungsten oxide and silicon oxide.
• the preparation of this solid has the same steps as those of catalyst A, unlike the tungsten content.
• the atomic ratio A M of surface is 0.09 (with A representing the base of Lewis based on phosphate).
• Table 1 gives the performances obtained with the catalysts A, B, C, D and E at different reaction times. Catalysts A, B, D and E were evaluated with GHSV (gaseous space velocity) of 2900 h -1 against 1930 h -1 for catalyst C.
• GHSV gaseous space velocity
• Catalysts A, B, D and E allow a total (or almost) conversion of glycerol at 5 h and are significantly more stable than catalyst C despite the use of a higher GHSV.
• Catalysts B and E (according to the invention) make it possible to obtain better acrolein selectivities at 24 hours. In addition, they are quickly selective (at 5am) and remain so until 48-54h.
• the catalyst F is of silica-doped tungstic zirconia type, that is to say a catalyst comprising a mixture of zirconium oxide, tungsten oxide and silicon oxide.
• the preparation of this solid comprises the same steps as those of catalyst A, unlike the calcination temperature. Indeed, the solid obtained after addition of tungsten, filtration and drying is calcined in air at 650 ° C instead of 750 ° C.
• Silicon, phosphorus and fluorine doped tungstic zirconia catalyst i.e. a catalyst comprising a mixture of zirconium oxide, tungsten oxide and silicon oxide and two bases one of Lewis based phosphates, the other fluorine-based, is prepared according to the invention. It is prepared with the same protocol as that of catalyst F. The only difference for this catalyst is that it is treated in a Teflon flask containing an ammoniacal solution whose pH is adjusted to 1 1 .9. The mixture is stirred for 24h without addition of TEOS, then filtered and washed with deionized water. The material used and this treatment are responsible for the doping of the solid by the phosphate and fluorine ions.
• the atomic ratio P / M of surface is 0.02.
• the atomic ratio F / M of surface is 0.04 which gives an atomic surface ratio A / M of 0.06, M representing Zr and Si.
• Table 2 gives the performances obtained with catalysts F and G at different reaction times.
• Glycerol conversion 100 100 100 100 100 100 99
• the catalyst G doped with phosphate and fluorine ions makes it possible to obtain better selectivities (up to 79%) even after only 4 hours of testing.

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