Method of obtaining at least one product of partial propylene oxidation and/or ammoxidation

Mixed metal oxide catalyst based on antimonite in a catalytic active oxidation state has the empirical formula: Me_aSb_bX_cQ_dR_eO_f, where Me is at least one element from the group: Fe, Co, Ni, Sn, U, Cr, Cu, Mn, Ti, Th, Ce, Pr, Sm, or Nd; X is at least one element from the group: V, Mo, or W; Q is at least one element from the group: Li, Na, K, Rb, Cs, Be, Mg, Ca, Sr, Ba, Sc, Y, La, Zr, Hf, Nb, Ta, Re, Ru, Os, Rh, Ir, Pd, Pt, Ag, Au, Zn, Cd, Hg, Al, Ga, In, Tl, Ge, Pb, As, or Se; R is at least one element from the group: Bi, B, P, or Te; and the indices a, b, c, d, e and f denote atomic ratios: a has a value from 0.1 to 15; b has a value from 1 to 100; c has a value from 0 to 20; d has a value from 0 to 20; e has a value from 0 to 10 and f is a number, taken to fulfill the valency requirements of the metals answering for the oxidation degree they have in the composition of the catalyst. Method of obtaining such a catalyst includes the following stages. At first they are subjected to aqueous suspension of Sb₂O₃ with HNO₃ and with one or more compounds of Me, and voluntarily with one or more compounds from the groups: X, Q or R, for obtaining the first mixture (a). The first mixture is then heated and dried to form a solid product (b). After this the solid product is calcinated forming the catalyst. The particular metal oxide catalyst based on antimonite in the catalytic active oxidation state as per the invention has the empirical formula: U_a'Fe_aSb_bMo_cBi_eO_f, where the indices a, a', b, c, e and f denote atomic ratios: a has a value from 0.1 to 5; a' has a value from 0.1 to 5; b has a value from 1 to 10; c has a value from 0.001 to 0.2; e has a value from 0.001 to 0.2; and f is a number, taken to fulfill the valency requirements of Sb, U, Fe, Bi, and Mo, answering for the oxidation degree they have in the composition of the catalyst. Method of obtaining such a catalyst includes the following stages. At first they are subjected to aqueous suspension of Sb₂O₃ with HNO₃, oxides or nitrates of bismuth and oxides or nitrates of uranium to form the first mixture (a). The first mixture is then heated under temperature and in a period of time, enough for the induction of the process for the formation of the antimonic oxide crystals and formation of the second mixture (b). An aqueous solution of a ferric compound iss then added to the second mixture for the formation of a third mixture (c). The pH of the third mixture is regulated in the range of 7 - 8.5, a precipitate of a hydrated mixture of oxides in the aqueous phase is formed (d). The precipitate is separated from the aqueous phase (e). An aqueous suspension of precipitate components of hydrated mixed oxides is obtained (f). Molybdate is added to the suspension component of hydrated mixed oxides (g). A suspension of hydrated mixed oxides of Molybdate component in the form of dy particles is formed (h). Later the calcination of the dry particles with the formation of the catalyst is carried out (i).

Invention concerns improved method for obtaining (meth)acrylic acid involving steam phase catalytic oxidation of propylene, propane or isobutylene for production of reaction mix, absorption of oxidised reaction product in water to obtain water solution containing (meth)acrylic acid, concentration of water solution in the presence of azeotropic agent and distillation of obtained (meth)acrylic acid in distillation column to obtaining purified (meth)acrylic acid. During operation of distillation column, including operation interruption and resumption, the column is washed with water, and afterwards azeotropic distillation is performed in the presence of azeotropic agent.

Invention concerns improved method of catalytic oxidation in vapour phase which supplies effective removing of reactionary heat, excludes hot spot formation, and supplies effective receipt of base product. Method of catalytic oxidation is disclosed in the vapour phase (a) of propylene, propane or isobutene by the instrumentality of molecular oxygen for receiving (meth)acrolein, and/or oxidation (b) of (meth)acrolein by molecular oxygen for receiving (meth)acryl acid, by the instrumentality of multiple-tubular reactor, contained: cylindrical reactor vessel, outfitted by initial material supply inlet hole and discharge hole for product, variety of reactor coolant pipes, located around the cylindrical reactor vessel and used for insertion the heat carrier into cylindrical reactor vessel or for removing the heat carrier from it, circulator for connection of variety loop pipeline to each other, variety of reaction tube, mounted by the instrumentality of tube reactor lattices, with catalyst. Also multiple-tubular reactor contains: variety of partitions, located lengthways of reaction tubes and used for changing heat carrier direction, inserted into reactor vessel. According to this heat carrier coolant flow is analysed and there are defined zones in reactor which have heat-transfer coefficient of heat carrier less than 1000 W/(m²·K); also reaction of catalytic oxidation is averted in the vapour phase in mentioned zones of reactor and reaction of catalytic oxidation is implemented in the vapour phase in reactor.

Invention relates to an improved method for synthesis of acrolein or acrylic acid or their mixture. Method involves at step (A) propane is subjected for partial heterogenous catalyzed dehydrogenation in gaseous phase to form a gaseous mixture A of product comprising molecular hydrogen, propylene, unconverted propane and components distinct from propane and propene, and then from a gaseous mixture of product from step (A) distinct from propane and propylene at least partial amount of molecular hydrogen is isolated and a mixture obtained after this isolation is used as a gaseous mixture A' at the second step (B) for loading at least into one oxidation reactor and in at least one oxidation reaction propylene is subjected for selective heterogenous catalyzed gas-phase partial oxidation with molecular oxygen to yield as the end product of gaseous mixture B containing acrolein or acrylic acid, or their mixture, and the third (C) wherein in limits of partial oxidation of propylene at step (B) of gaseous mixture B acrolein or acrylic acid or their mixtures as the end product are separated and at least unconverted propane containing in gaseous mixture at step (B) is recovered to the dehydrogenation step (A) wherein in limits of partial oxidation of propylene at step (B) molecular nitrogen is used as additional diluting gas. Method provides significant decreasing of by-side products.

Invention relates to a method for synthesis of acrolein and/or acrylic acid from propane and/or propene. Method involves the following steps: (a) isolating propane and/or propene from gaseous mixture A containing propane and/or propene by their absorption with adsorbent; (b) isolating propane and/or propene from adsorbent to form gas B containing propane and/or propene, and (c) using gas B obtained in stage (b) for oxidation of propane and/or propene to acrolein and/or acrylic acid wherein the heterogeneous catalytic dehydrogenation of propane without feeding oxygen is not carried out. Method shows economy and maximal exploitation period of used catalyst without its regeneration.

Claimed method includes feeding of raw gas mixture through pipeline from raw material mixer into oxidation reactor and catalytic oxidation of raw mixture in vapor phase to produce (meth)acrolein or (meth)acrylic acid. Said pipeline is heated and/or maintained in heated state and temperature of gas mixture fed into oxidation reactor is by 5-25⁰C higher then condensation temperature of raw gas mixture.

Invention relates to the improved method for oxidation of (C₂-C₄)-alkane and preparing the corresponding alkene and carboxylic acid. Method involves addition of this alkane to contact with molecular oxygen-containing gas in oxidative reaction zone and optionally at least one corresponding alkene and water in the presence of at least two catalysts with different selectivity. Each catalyst is effective in oxidation of alkane to corresponding alkene and carboxylic acid resulting to formation of product comprising alkene, carboxylic acid and water wherein the molar ratio between alkene and carboxylic acid synthesized in the reaction zone is regulated or maintained at the required level by regulation the relative amounts of at least two catalyst in the oxidative reaction zone. Also, invention relates to the combined method for preparing alkyl carboxylate comprising abovementioned stage in preparing alkene and carboxylic acid in the first reaction zone. Then method involves the stage for addition of at least part of each alkene and carboxylic acid prepared in the first reaction zone to the inter-contacting in the second reaction zone the presence of at least one catalyst that is effective in preparing alkyl carboxylate to yield this alkyl carboxylate. Also, invention relates to a method for preparing alkenyl carboxylate comprising the abovementioned stage for preparing alkene and carboxylic acid in the first reaction zone and stage for inter-contacting in the second reaction zone of at least part of each alkene and carboxylic acid synthesized in the first reaction zone and molecular oxygen-containing gas in the presence of at least one catalyst that is effective in preparing alkenyl carboxylate and resulting to preparing this alkenyl carboxylate.

Invention relates to improved C2-C4-alkane oxidation process to produce corresponding alkene and carboxylic acid, which process comprises bringing indicated alkane in oxidation reaction zone into contact with molecular oxygen-containing gas and corresponding alkene and optionally with water in presence of at least one catalyst efficient for oxidation of alkane into corresponding alkene and carboxylic acid. Resulting product contains alkene, carboxylic acid, and water, wherein alkene-to-carboxylic acid molar ratio in oxidation reaction zone is controlled or maintained at desired level by way of controlling alkene and optional water concentrations in oxidation reaction zone and also, optionally, controlling one or several from following parameters: pressure, temperature, and residence time in oxidation reaction zone. Invention also relates to integrated process of producing alkyl carboxylate including above-indicated stage of producing alkene and carboxylic acid in first reaction zone and stage of bringing, in second reaction zone, at least part of each of alkene and carboxylic acid obtained in first reaction zone in contact with each other in presence of at least one catalyst effective in production of alkyl carboxylate to produce the same. Invention further relates to production of alkenyl carboxylate including above-indicated stage of producing alkene and carboxylic acid in first reaction zone and stage of bringing, in second reaction zone, at least part of each of alkene and carboxylic acid obtained in first reaction zone plus molecular oxygen-containing gas into contact with each other in presence of at least one catalyst effective in production of alkenyl carboxylate to produce the same.

Invention relates to the improved method for preparing acrylic acid and selective oxidation of propylene to acrolein. Method involves carrying out reaction of propylene with oxygen in the first zone reaction with the first catalyst corresponding to the following formula: A_aB_bC_cCa_dFe_eBi_fMo₁₂O_x wherein A means Li, Na, K, Rb and Cs and their mixtures also; B means Mg, Sr, Mn, Ni, Co and Zn and their mixtures also; C means Ce, Cr, Al, Sb, P, Ge, Sn, Cu, V and W and their mixtures also wherein a = 0.01-1.0; b and e = 1.0-10; c = 0-5.0 but preferably 0.05-5.0; d and f = 0.05-5.0; x represents a number determined by valence of other presenting elements. Reaction is carried out at enhanced temperature providing preparing acrylic acid and acrolein and the following addition of acrolein from the first reaction zone to the second reaction zone containing the second catalyst used for conversion of acrolein to acrylic acid. Method provides high conversion of propylene to acrylic acid and acrolein.

Invention concerns organic synthesis field, particularly method of obtaining benzoic acid (C₆H₅COOH, benzenecarboxylic acid) by catalytic oxidation of benzyl alcohol in hydrogen peroxide solution, as well as catalysts for method implementation, and method of obtaining catalysts. Catalysts of benzoic acid production is nanostructurised bifunctional metallocomplex catalyst acting as oxidation and interphase transport catalyst. It is a complex compound of the general formula Q₃{PO₄[W(O)(O₂)₂]₄}, where: Q is quadruple ammonium cation [(R₁)₃N R₂]⁺, where: R₁ and R₂ contain 8 to 24 carbon atoms. The invention concerns method of obtaining catalyst for benzoic acid production by dissolution of compounds containing phosphor and tungsten in hydrogen peroxide solution with added interphase transport catalyst compound, with phosphor-tungsten heteropolyacids of Keggin or Dawson structure are used as compounds containing phosphor and tungsten, dissolution is performed at the following mol ratio: hydrogen peroxide to tungsten [H₂O₂]/[W]=15-50, with further addition of quadruple ammonium cation - [(R₁)₃N R₂]⁺ as interphase transport catalyst, where: R₁ and R₂ contain 8 to 24 carbon atoms. The invention also concerns method of obtaining benzoic acid by substrate oxidation in hydrogen peroxide in the presence of the catalyst described above.

Invention concerns improved method of catalytic oxidation in vapour phase which supplies effective removing of reactionary heat, excludes hot spot formation, and supplies effective receipt of base product. Method of catalytic oxidation is disclosed in the vapour phase (a) of propylene, propane or isobutene by the instrumentality of molecular oxygen for receiving (meth)acrolein, and/or oxidation (b) of (meth)acrolein by molecular oxygen for receiving (meth)acryl acid, by the instrumentality of multiple-tubular reactor, contained: cylindrical reactor vessel, outfitted by initial material supply inlet hole and discharge hole for product, variety of reactor coolant pipes, located around the cylindrical reactor vessel and used for insertion the heat carrier into cylindrical reactor vessel or for removing the heat carrier from it, circulator for connection of variety loop pipeline to each other, variety of reaction tube, mounted by the instrumentality of tube reactor lattices, with catalyst. Also multiple-tubular reactor contains: variety of partitions, located lengthways of reaction tubes and used for changing heat carrier direction, inserted into reactor vessel. According to this heat carrier coolant flow is analysed and there are defined zones in reactor which have heat-transfer coefficient of heat carrier less than 1000 W/(m²·K); also reaction of catalytic oxidation is averted in the vapour phase in mentioned zones of reactor and reaction of catalytic oxidation is implemented in the vapour phase in reactor.

Invention provides improved process for production of isobutyric acid suitable for use in production of higher carboxylic acid esters and drying oils. Process comprises oxidation of isobutyric aldehyde with air oxygen on heating in column-type reactor filled with zeolite of types CaX, CaA, NaX, or NaA with packing diameter-to-packing width ratio 1:(7.2-8), at volumetric air supply velocity 684.0-874.0 h-1, butyric acid-to oxygen molar ratio 1:(0.7-1.0), and temperature 62-66°C.

Synthesis involves oxidation of substrate with chlorine dioxide in organic solvent at 40-50°C, said selected from myrtenal or myrtenol and said organic solvent from acetone, benzene, and alcohol at molar ratio of myrtenal or myrtenol to chlorine dioxide 1:(0.5-3.5). Thus formed myrtenic acid is isolated in the form of its water-soluble salt and, when alcohol is used as solvent, in the form of ester.

Invention relates to a method for preparing 2-ethylhexanoic acid. Method involves catalytic hydrogenation of fraction isolating from the manufacturing waste in the presence of hydrogen by rectification method followed by oxidation of prepared hydrogenation product with air oxygen at temperature 30-80°C and under pressure 0.1-1.0 MPa. Vat residue from rectification of butyl alcohols in oxo-synthesis is used as raw for the process. Fraction with the total content of unsaturated and saturated C₈-alcohols 65-95 wt.-% is isolated from vat residue by rectification and in residual pressure on column top 100-300 mm of mercury column. This fraction is subjected for hydrogenation in vapor phase under atmosphere pressure, temperature 220-270°C, volume rate of raw feeding 0.5 h^-1, volume ratio raw : hydrogen = 1:1 on copper-containing catalyst and the following isolation 2-ethylhexanal from catalyzate by rectification on two columns working at residual pressure on top of the first column 60-100 mm of mercury column and on top of the second column 20-80 mm of mercury column, and 2-ethylhexanal is oxidized with air oxygen. The end 2-ethylhexanoic acid is isolated from the prepared oxidized product by rectification on two columns working at residual pressure on top of column 20-70 and 10-60 mm of mercury column, respectively. Method provides enhancing the yield of 2-ethylhexanoic acid.

Invention relates to the improved method for preparing 2-keto-L-gulonic acid. This compound is an intermediate substance in synthesis of vitamin C. Method involves oxidation of L-sorbose in the presence of platinum-containing polymeric catalyst applied on Al₂O₃ in medium with the equimolar content of NaHCO₃ under atmosphere pressure, at the rate stirring 870-1 000 rev/min and bubbling pure oxygen as an oxidizing agent. Reaction is carried out in medium water : ethyl alcohol 7-10 vol. %, in the concentration of L-sorbose 0.29-0.6 mole/l, on spherical microparticles of catalyst in the amount 20-40 g/l with ultra-thin layer of polydiallyldimethylammonium chloride as cationic polyelectrolyte with platinum nanoparticles formed on it. The content of platinum in catalyst is 1-2%. The feeding rate of oxidizing agent is 400-450 ml/min. The end product is obtained with high yield 97-99%.

The invention relates to chemical technology, in particular to an improved method for producing a saturated monocarboxylic acids WITH₄-C₈by oxidation of the corresponding aldehydes with oxygen, aldehydes impose additional isopropanol at a volume ratio of isopropanol to the aldehyde, equal 0,0007-0,0038, and the reaction is carried out at a temperature of 50-70⁰With

The invention relates to a method for producing 2-keto-L-gulonovoy acid, which is an intermediate for the synthesis of vitamin C, the oxidation of L-sorbose in the presence of platinum source of catalyst in aqueous-alkaline medium with equimolar content of NaHCO₃at atmospheric pressure, intensive stirring and bubbling an oxidizing agent - pure oxygen - speed 440-460 ml/min

The invention relates to an improved method for producing alkoxyacetic acids (AUC) or their salts, which are used as surface-active substances, intermediates for the synthesis of pharmaceuticals and plant protection products

The invention relates to the production of a component of detergents

Invention concerns improved method of catalytic oxidation in vapour phase which supplies effective removing of reactionary heat, excludes hot spot formation, and supplies effective receipt of base product. Method of catalytic oxidation is disclosed in the vapour phase (a) of propylene, propane or isobutene by the instrumentality of molecular oxygen for receiving (meth)acrolein, and/or oxidation (b) of (meth)acrolein by molecular oxygen for receiving (meth)acryl acid, by the instrumentality of multiple-tubular reactor, contained: cylindrical reactor vessel, outfitted by initial material supply inlet hole and discharge hole for product, variety of reactor coolant pipes, located around the cylindrical reactor vessel and used for insertion the heat carrier into cylindrical reactor vessel or for removing the heat carrier from it, circulator for connection of variety loop pipeline to each other, variety of reaction tube, mounted by the instrumentality of tube reactor lattices, with catalyst. Also multiple-tubular reactor contains: variety of partitions, located lengthways of reaction tubes and used for changing heat carrier direction, inserted into reactor vessel. According to this heat carrier coolant flow is analysed and there are defined zones in reactor which have heat-transfer coefficient of heat carrier less than 1000 W/(m²·K); also reaction of catalytic oxidation is averted in the vapour phase in mentioned zones of reactor and reaction of catalytic oxidation is implemented in the vapour phase in reactor.