Method of obtaining, at least, one product of partial oxidation and/or ammoxidising of propylene |
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IPC classes for russian patent Method of obtaining, at least, one product of partial oxidation and/or ammoxidising of propylene (RU 2347772):
                                                                                                                                                                                                                                                            
 Reactor system and method for ethylene oxide production / 2346738
Reactor system comprises reactor tube, which contains compressed layer of molded carrier material, which may include catalytic component. Molded carrier material, for instance, aluminium oxide, has geometric configuration of hollow cylinder. Catalyst contains silver. Hollow cylinder has ratio of rated length to rated external diameter from 0.5 to 2, and ratio of rated external diameter to rated internal diameter, which exceeds 2.7. Reactor system also has such combinations of reactor tube diameter and geometric parameters of molded catalyst carrier, which make it possible to produce compressed layer of catalyst in reaction system with high density of package with minimum pressure drop via compressed layer of catalyst.
Method of obtaining olefin oxide / 2345073
Invention relates to method of obtaining olefin oxide including interaction of initial mixture, which contains olefin and oxygen, in presence of silver-containing catalyst. According to claimed method, before catalyst reaches late stage of ageing, temperature of reaction is supported higher than 255°C, and content of olefin in initial mixture is supported within the range from higher than 25 mol % to at most 80 mol %, relative to general initial mixture, said reaction temperature and said olefin content being supported, at least, during period which is sufficient to obtain olefin oxide in amount 1000 kmole of olefin oxide per m3 of catalyst layer. "Late stage of ageing" of catalyst is determined by obtaining total olefin oxide in amount, at least, 10000 kmole of olefin oxide per m3 of catalyst layer. Invention also relates to method of obtaining 1,2-diole, ether, 1,2-diole or alkanolamine.
 Silver-containing catalysts, obtaining such catalysts and their application / 2342993
Catalyst contains silver, applied on profiled carrier with geometric configuration in form of hollow cylinder, in which ratio of length to outer diameter lies within interval from 0.3 to 2, and inner diameter constitutes up to 30% of outer diameter of said profiled carrier with assumption that when carrier contains more than one channel, inner diameter is considered to be the diameter of one channel with area of transverse section equal to the sum of areas of transverse sections of all channels. Described is method which includes obtaining profiled carrier with geometric configuration in form of hollow cylinder described above, and application of silver on profiled carrier. Described is method of obtaining ethylene oxide which includes: contacting under suitable epoxidation conditions of raw material flow, containing ethylene and oxygen, with described above catalyst. Also described is method of obtaining ethylene glycol, ethylene glycol ester, or 1,2-alkanolamine, which includes using ethylene oxide obtained by described above method and its conversion to ethylene glycol, ethylene glycol ester or 1,2-alaknolamine.
Catalyst and method of its application / 2342190
Catalyst contains carrier and silver, applied on carrier, in amount of at least, 10 g/kg with respect to catalyst weight, where carrier has specific surface area of at least 1.4 m2/g and such pore distribution by size, that pores with diameter in interval from 0.2 to 10 mcm constitute more than 85% of general pore volume, and such pores together form pore volume of at least 0.27 ml/g with respect to carrier weight; method of catalyst obtaining and method of olefin epoxidation, which includes interaction of olefin with oxygen in presence of said catalyst.
Novel water hydrogen peroxide solutions / 2336225
Claimed is water solution of hydrogen peroxide, suitable for olefine epoxidation, which includes: I) in total less than 50 wt fraction/mln of alkaline metals, alkaline-earth metals or their combinations irrespective of whether said alkaline or alkaline-earth metals are in catione-active or complex form; II) in total at least 50 wt fraction/mln of amines, which have pkb value less than 4.5, or respective protonated compounds; and III) in total at least 100 wt fraction/mln anions or compounds, which are able to dissociate with anion formation, according to which values in wt fraction/mln are given in terms of hydrogen peroxide weight. Claimed is method of obtaining hydrogen peroxide solution. Claimed is application of water solution of hydrogen peroxide.
Method of molecular ethylene oxidation / 2335498
According to the present invention, ethylene is oxidised in contact with mix of heterogeneous catalyst in particles and solid inert substance in particles, treated with alkali metal, in oxidation conditions.
Oxidation catalyst of ethylene / 2331474
Oxidation catalyst of ethylene in ethylene oxide is described, free from rhenium and transition metal, which is solid silver and containing the combination of promoters consisting of (1) alkaline metals in quantity 400-1500 ppm by weight of the catalyst, (2) barium in the quantity 5-500 ppm by the weight of the catalyst and (3) sulfur in the quantity 5-300 ppm by the weight of the catalyst. Also described is the method of obtaining ethylene oxide, including the interaction of ethylene and molecular oxygen in the presence of the above described catalyst.
 Method of perfecting process of producing ethylene oxide / 2329259
Invention pertains to ethylene oxide and to the method of obtaining 1,2-ethanediol or a simple ether of 1,2-ethanediol, from ethylene oxide, obtained using the proposed method. The process of producing ethylene oxide involves an epoxidation reactor system, containing a volume of a high octane epoxidation catalyst. The method involves replacing part of the volume of the high octane epoxidation catalyst with a volume of highly selective catalyst and modification of the process system so as to provide for initial raw materials of the reactor of the epoxidation system, with low concentration of carbon dioxide.
Method for olefines epoxidation and applied catalyst / 2328491
Method for olefine epoxidation is invented which includes the reaction of the raw material containing olefine, oxygen and organic halogenide, in presence of the catalyst containing silver and rhenium precipitated on the carrier where the catalyst contains rhenium at 1.5 mol/kg of the catalyst mass, at maximum, and 0.0015 mmol/m3 of the carrier surface, at maximum, and where the reaction temperature is increased so as to partially reduce the effect of catalyst loss, and the halogenide is presented in relative Q amount which is maintained constant and where the relative amount of Q is the ratio of the effective molar amount of the active halogen compound in the raw material, to the effective molar amount of hydrocarbon, in the raw material. The invention also implies the method for producing the 1,2-diol, the simple ether of the 1,2-diol and/or alkanolamine and the catalyst to be applied in the said method.
 Method of producing olefin oxide, method of application of olefie oxide and catalytic composition / 2325948
Principle refers to the method of producing olefin oxide, method of application of the produced olefin oxide and the production of 1,2-diol or simple ether 1-,2-diol and catalytic composition. The mentioned catalytic composition for the production of olefin oxide contains silver and activating agent, that consists of an alkaline metal on a bearer where the activating alkaline metal contains potassium whose quantity is not less than 5 mcmol/g of metal relative to the mass of the catalytic composition and not less than 1 mcmol/g alkaline metal from the group that contains lithium, sodium and there mixtures in which the mentioned bearer contains calcium carbonate joined with silver. The relative mass of silver: calcium carbonate is 1:5 to 1:100, and the unit surface area of the bearer is from 1 m/g to 20 m/g, and the apparent porosity of the bearer is 0.05 ml/g to 2 ml/g. The explained method of producing olefin oxide, include interaction of olefin, that has 3 or more carbon atoms, with oxygen in the presence of the above mentioned catalytic system, and the method of producing 1,2-diol or simple ether 1,2-diol, in which the olefin oxide is produced from the explained method.
 Propene/propane separation process / 2296736
Invention relates to separation of saturated and unsaturated hydrogenation-hydrocarbon, in particular propane and propene contained in starting hydrocarbon blend. Process is carried out in vertical countercurrent contact zone, wherein stream with elevated concentration of propene is withdrawn from concentration section and stream with elevated concentration of propane is withdrawn from exhausting section connected to boiler. Separation is effected in presence of hydrocarbon diluent containing mainly one or several saturated C4-C10-hydrocarbons having boiling point at least by 30°C above that of propane. Preferred content of the diluent in liquid phase ranges from 20 to 90 wt %. Separation is accomplished through rectification and/or selective absorption with partial stripping of stream in boiler, stripped fraction being recycled into rectification or absorption zone. C2-Hydrocarbon impurities and diluent are separated in additional rectification zones.
 The method of chemical cleaning managersdynamic (c7-c9)- fractions / 2189965
The invention relates to chemical treatment managersdynamic fractions WITH7-C9that use in the process of getting a film-forming agents for the preparation of drying oils and varnishes cationic cooligomerization unsaturated hydrocarbons
 The way the joint production of pyrocatechin and hydroquinone / 2028287
The invention relates to chemical technology and can be used in the production of pyrocatechin and hydroquinone, which are widely used as intermediates for the production of antioxidants, medicinal substances, dyes and so on
 Method of extraction of phenol, pyrocatechin and hydrochinone, mixtures thereof with water and a resinous products / 2028286
The invention relates to chemical technology and can be used in the production of pyrocatechin and hydroquinone, which are widely used as intermediates for the production of antioxidants, pharmaceuticals, dyes, etc
 A way of separating aromatic hydrocarbons, c8 / 2021242
The invention relates to an improved method of extraction of aromatic hydrocarbons FROM8from catalization reforming of straight-run gasoline fractions containing as impurities paraffin Uglevodorody9and higher olefins, cycloparaffins and cycloolefins hydrocarbons WITH8and above
 Method of catalytic oxidation in vapour phase implemented in multiple-tubular reactor / 2331628
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.
 Process for production of acrylic acid via heterogeneously catalyzed partial oxidation of propane / 2308446
Invention relates to improved process to produce acrylic acid via heterogeneously catalyzed gas-phase partial oxidation of propane wherein starting reactive gas mixture containing propane, molecular oxygen, and at least one gas diluent is passed at elevated temperature over a multimetal oxide bulk depicted by total stoichiometry as Mo1VbM1 сM2 вOn (I), in which M1 = Te and/or Sb and M2 is at least one element from group comprising Nb, Ta, W, Ti, Al, Zr, Cr, Mn, Ga, Fe, Ru, Co, Rh, Ni, Pd, Pt, La, Bi, B, Ce, Zn, Si, and In; b = 0.01 to 1, c = >0 to 1, d = >0 to 1, and n = number, which is determined by valence and number of non-oxygen elements in (I). Propane is partially oxidized to produce acrylic acid in a process wherein composition of starting reaction mixture is at least two times varied in the course of process such that molar percentage of gas diluent (water steam) in starting reaction gas mixture decreases relative to molar percentage of propane contained in starting gas mixture.
 Method for production of (meth)acrolein and (meth)acrlic acid compounds / 2279424
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.
 Method for preparing acrylic acid / 2258061
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: AaBbCcCadFeeBifMo12Ox 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.
Method for preparing acrylic acid / 2258061
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: AaBbCcCadFeeBifMo12Ox 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.
 The method of obtaining acrylic acid / 2119908
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FIELD: chemistry. SUBSTANCE: present invention pertains to perfection of the method of obtaining at least, one product of partial oxidation and/or ammoxidising of propylene, chosen from a group, comprising propylene oxide, acrolein, acrylic acid and acrylonitrile. The starting material is raw propane. a) At the first stage, raw propane, in the presence and/or absence of oxygen, is subjected to homogenous and/or heterogeneous catalysed dehydrogenation and/or oxydehydrogenation. Gas mixture 1, containing propane and propylene is obtained. b) If necessary, a certain quantity of the other components in gas mixture 1, obtained in the first stage, besides propane and propylene, such as hydrogen and carbon monoxide is separated and/or converted to other compounds, such as water and carbon dioxide. From gas mixture 1, gas mixture 1' is obtained, containing propane and propylene, as well as other compounds, besides oxygen, propane and propylene. c) At the third stage, gas mixture 1 and/or gas mixture 1' as a component, containing molecular oxygen, of gas mixture 2, is subjected to heterogeneous catalysed partial gas-phase oxidation and/or propylene, contained in gas mixture 1 and/or gas mixture 1', undergoes partial gas-phase ammoxidising. Content of butane-1 in gas mixture 2 is ≤1 vol.%. The method increases output of desired products and efficiency of the process. EFFECT: increased output of desired products and efficiency of the process. 72 cl, 10 ex
The text descriptions are given in facsimile form. 1. The method of obtaining at least one product of partial oxidation and/or amoxiline propylene selected from the group comprising propylene oxide, acrolein, acrylic acid and Acrylonitrile, the original substance of which is crude propane, in which a) at the first stage, the crude propane in the presence and/or absence of oxygen is subjected to a homogeneous and/or heterogeneous-catalyzed dehydration and/or oxidisation, and get containing propane and propylene gas mixture 1, and b) from those obtained in the first stage of the gas mixture 1, contained therein, other than propane and propylene components, such as hydrogen, carbon monoxide, if necessary, to separate a certain amount and/or convert it into other compounds such as water, carbon dioxide, and the gas mixture 1 receive the gas mixture 1'containing propane and propylene, and other than oxygen, propane and propylene compounds, and at least one stage C) the gas mixture 1 and/or gas mixture 1' as a component containing molecular oxygen, the gas mixture 2 is subjected to a heterogeneously-catalyzed gas-phase partial oxidation and/or partial gas-phase Immokalee contained in the gas mixture 1 and/or in the gas mixture 1' propylene, characterized in that the content of butene-1 in the gas mixture 2 is ≤1%vol. 2. The method according to claim 1, characterized in that the content of butene-1 in the gas mixture 2 is ≤0,75%vol. 3. The method according to claim 1, characterized in that the content of butene-1 in the gas mixture 2 is ≤0,5%vol. 4. The method according to claim 1, characterized in that the content of butene-1 in the gas mixture 2 is ≤0,3%vol. 5. The method according to claim 1, characterized in that the content of butene-1 in the gas mixture 2 is ≤0,1%vol. 6. The method according to claim 1, characterized in that the content of butene-1 in the gas mixture 2 is >0,003%vol. 7. The method according to claim 1, characterized in that the content of butene-1 in the gas mixture 2 is >0,001%vol. 8. The method according to claim 1, characterized in that the content of TRANS-butene-2 in the gas mixture 2 is ≤1%vol. 9. The method according to claim 1, characterized in that the content of TRANS-butene-2 in the gas mixture 2 is ≤0,5%vol. 10. The method according to claim 1, characterized in that the content of TRANS-butene-2 in the gas mixture 2 is ≤0,05%vol. 11. The method according to claim 1, characterized in that the content of CIS-butene-2 in the gas mixture 2 is ≤1%vol. 12. The method according to claim 1, characterized in that the content of CIS-butene-2 in the gas mixture 2 is ≤0,5%vol. 13. The method according to claim 1, characterized in that the content of CIS-butene-2 in the gas mixture 2 is ࣘ 0,05%vol. 14. The method according to claim 1, characterized in that the content of ISO-butene in the gas mixture 2 is ≤1%vol. 15. The method according to claim 1, characterized in that the content of ISO-butene in the gas mixture 2 is ≤0,5%vol. 16. The method according to claim 1, characterized in that the content of ISO-butene in the gas mixture 2 is ≤0,05%vol. 17. The method according to claim 1, characterized in that the total content of butenes in the gas mixture 2 is ≤1%vol. 18. The method according to claim 1, characterized in that the total content of butenes in the gas mixture 2 is ≤0,5%vol. 19. The method according to claim 1, characterized in that the total content of butenes in the gas mixture 2 is ≤0,05%vol. 20. The method according to claim 1, characterized in that the total content of C4-hydrocarbons in the gas mixture 2 is ≤3%vol. 21. The method according to claim 1, characterized in that the total content of C4-hydrocarbons in the gas mixture 2 is ≤2 vol.%. 22. The method according to claim 1, characterized in that the total content of C4-hydrocarbons in the gas mixture 2 is ≤1%vol. 23. The method according to claim 1, characterized in that the total content of C4-hydrocarbons in the gas mixture 2 is >0.05 and <3%vol. 24. The method according to claim 1, characterized in that the gas mixture 1' contains ≥0,1% vol. other than propane and propylene, and oxygen components. 25. The method according to claim 1, characterized in that the gas mixture 1' contains ≥ 0,2% vol. other than propane and propylene, and oxygen components. 26. The method according to claim 1, characterized in that the gas mixture 1' contains ≥0,3% vol. other than propane and propylene, and oxygen components. 27. The method according to claim 1, characterized in that the gas mixture 1' contains ≥0,5% vol. other than propane and propylene, and oxygen components. 28. The method according to claim 1, characterized in that the gas mixture 1' contains ≥1% vol. other than propane and propylene, and oxygen components. 29. The method according to claim 1, characterized in that the gas mixture 1' contains ≥3% vol. other than propane and propylene, and oxygen components. 30. The method according to claim 1, characterized in that the gas mixture 1' contains ≥5 vol.% other than propane and propylene, and oxygen components. 31. The method according to claim 1, characterized in that the gas mixture 1' contains ≥10 vol.% other than propane and propylene, and oxygen components. 32. The method according to claim 1, characterized in that the gas mixture 1' contains ≥30% vol. other than propane and propylene, and oxygen components. 33. The method according to one of claims 1 to 32, characterized in that the gas mixture 2 contains up to 60% vol. propane. 34. The method according to one of claims 1 to 32, characterized in that the gas mixture 2 contains up to 50% vol. propane. 35. The method according to one of claims 1 to 32, otlichuy is the, what gas mixture 2 contains from 20 to 40 vol.% propane. 36. The method according to one of claims 1 to 32, characterized in that the gas mixture 2 contains from 7 to 15% vol. About2, from 5 to 10 vol.% propylene, from 15 to 40 vol.% propane, from 25 to 60 vol.% nitrogen, from 1 to 5 vol.% the amount of CO, CO2and H2And from 0 to 5% vol. other components, and contained, if necessary, ammonia is not considered. 37. The method according to one of claims 1 to 32, characterized in that the gas mixture 2 contains H2O≤60 vol.%, N2≤80 vol.%, O2>0, ≤20 vol.%, CO≤2 vol.%, CO2≤5 vol.%, Ethan ≤10 vol.%, ethylene ≤5 vol.%, methane ≤5 vol.%, propane >0, ≤50 vol.%, cyclopropane ≤0,1%vol., propyne ≤0,1%vol., PROPADIENE ≤0,1%vol., propylene >0, ≤30 vol.%, H2≤30 vol.%, ISO-butane ≤3.% n-butane ≤3.% TRANS-butene-2 ≤1 vol.%, CIS-butene-2 ≤1 vol.%, butene-1 ≤1 vol.%, ISO-butene ≤1 vol.%, butadiene-1,3 ≤1 vol.%, butadiene-1,2 ≤1 vol.%, 1-buten ≤0,5% vol. and 2-Butin ≤0,5%vol., and contained, if necessary, ammonia is not considered. 38. The method according to one of claims 1 to 32, otlichalis the same time, that crude propane contains ≥0,25% vol. other than propane and propylene components. 39. The method according to one of claims 1 to 32, wherein the crude propane contains ≥1% vol. other than propane and propylene components. 40. The method according to one of claims 1 to 32, wherein the crude propane contains ≥2 vol.% other than propane and propylene components. 41. The method according to one of claims 1 to 32, wherein the crude propane contains ≥3% vol. other than propane and propylene components. 42. The method according to one of claims 1 to 32, wherein the crude propane contains up to 6% vol. With4-hydrocarbons. 43. The method according to one of claims 1 to 32, wherein the crude propane contains from 0.1 to 6% vol. With4-hydrocarbons. 44. The method according to one of claims 1 to 32, wherein the crude propane contains up to 0.5% vol. butene-1. 45. The method according to one of claims 1 to 32, wherein the crude propane contains about 5. ppm to 0.5% vol. butene-1. 46. The method according to one of claims 1 to 32, wherein the crude propane contains up to 0.5% vol. of butenes. 47. The method according to one of claims 1 to 32, wherein the crude propane contains 5 ABC/m to 0,5% vol. of butenes. 48. The method according to one of claims 1 to 32, wherein the crude propane has the following characteristics: the content of propane ≥90 vol.%, the total content of propane and propylene ≤99%, < num="93"> the total content of C4-hydrocarbons<6%,the content of butene-1 ≤0,5%vol., the total content of butenes ≤0,5%vol., the content of ethane ≤10 vol.%, the ethylene content ≤5 vol.%, methane ≤5 vol.%, the content of cyclopropane ≤0,1%vol., the content of propylene ≤10 vol.%, the total content other than propane and propylene With3-hydrocarbons ≤0,3 vol.%, the total content of C5-hydrocarbons ≤0,3% vol. and the total content of C6to C8-hydrocarbons ≤600 OBC/million 49. The method according to one of claims 1 to 32, characterized in that the conversion of propane in the first stage ranges from ≥5 mol.% to ≤30 mol.%. 50. The method according to one of claims 1 to 32, characterized in that the gas mixture of the product of gas-phase partial oxidation and/or partial gas-phase Immokalee separating at least one product of partial oxidation and/or amoxiline propylene and at least contained in this gas mixture, unreacted propane recycle to the first stage and/or gas-phase partial oxidation and/or gas-phase amoxilina. 51. The method according to one of claims 1 to 32, characterized in that it is carried out in at least one reaction zone to the catalyst layer, the active mass of which is ENISA least represents the mass of metal oxides, which comprises in combination at least the elements Mo, V, at least one of the two elements Te and Sb, and at least one element selected from the group including Nb, TA, W, Ti, Al, Zr, Cr, Mn, Ga, Fe, Ru, Co, Rh, Ni, Pd, Pt, La, Bi, B, Ce, Sn, Zn, Si, Na, Li, K, Mg, Ag, Au and In. 52. The method according to § 51, characterized in that the active mass is, at least, a lot of metal oxides, which has a stoichiometry of elements I
where M1=Te and/or Sb, M2= at least one element selected from the group including Nb, TA, W, Ti, Al, Zr, Cr, Mn, Ga, Fe, Ru, Co, Rh, Ni, Pd, Pt, La, Bi, CE, Sn, Zn, Si, Na, Li, K, Mg, Ag, Au and In, b=0.01 to 1, with=>0 to 1 and d=>0 to 1. 53. The method of paragraph 52, wherein M1=Te and M2=Nb, TA, W and/or Ti. 54. The method according to paragraph 52 or 53, characterized in that M2=Nb. 55. The method according to § 51, wherein the at least one active mass of the metal oxide has an x-ray diffraction pattern, the diffraction reflexes h and i which have peaks (highs) with the angles of diffraction of 22.2±0,5° (h) and 27.3±0,5° (i). 56. The method according to § 55, characterized in that the x-ray diffraction pattern has additionally diffraction reflex k, the peak of which is the diffraction angle of 28.2±0,5°. 57. The method according to § 55 or 56, the tives such as those that diffraction reflex h inside the x-ray diffraction is the most intense and the half-width of the peak is a maximum of 0.5°. 58. The method according to § 57, characterized in that the width of the diffraction peak of reflex i and diffraction reflex k advanced at the same time makes each ≤1° and the intensity of the Pkdiffraction reflex k and the intensity of the Pidiffraction reflex i perform ratio of 0.20≤R≤to 0.85, where R is expressed by the formula R=Pi/(Pi+Pk) the ratio of intensities. 59. The method according to § 51, characterized in that the x-ray diffraction pattern, at least one active mass of metal oxides has no diffraction reflex, the maximum of which is 2Θ=50±0,3°. 60. The method according to one of claims 1 to 32, characterized in that the first stage is carried out in a separate reaction zone. 61. The method according to p, characterized in that the first stage is a heterogeneously-catalyzed dehydrogenation. 62. The method according to p, characterized in that the gas mixture 1 contained therein, other than propane and propylene component is separated by a certain amount, which includes at least one4the hydrocarbon. 63. The method according to p, characterized in that the gas mixture 1 contained in n the th, other than propane and propylene component is separated by a certain amount, which includes at least one butene. 64. The method according to p, characterized in that the gas mixture 1 contained therein, other than propane and propylene component is separated by a certain amount, which includes, at least, butene-1. 65. The method according to p, characterized in that when heterogeneous catalyzed gas-phase partial oxidation and/or partial gas-phase amoxiline used catalyst, the active mass which contains the elements Mo, Bi and Fe. 66. The method according to p, characterized in that when heterogeneous catalyzed gas-phase partial oxidation and/or partial gas-phase amoxiline used catalyst, the active mass of which contains a metal oxide of General formula IV
in which the variables have the following meanings: X1= means the Nickel and/or cobalt, X2= means thallium, an alkali metal and/or alkaline earth metal, X3= means zinc, phosphorus, arsenic, boron, antimony, tin, cerium, lead and/or tungsten, X4= means silicon, aluminum, titanium and/or zirconium, a = is the number from 0 to 5, b = is the number of from 0.01 to 5 C = is the number from 0 to 10, d = is the number from 0 up to 2, e = equal to the number of from 0 to 8, f = is equal to the number from 0 to 10 and n = is the number that is determined by the valence and amount of non-oxygen elements in the formula (IV). 67. The method according to p, characterized in that when heterogeneous catalyzed gas-phase partial oxidation is used, the catalyst, the active mass which contains the elements Mo and V. 68. The method according to p, characterized in that when heterogeneous catalyzed gas-phase partial oxidation is used, the catalyst, the active mass of which is a metal oxide of General formula VII Mo12VaXb 1Xc 2Xd 3Xe 4Xf 5Xg 6On in which the variables have the following meanings: X1= W, Nb, TA, Cr and/or CE, X2= Cu, Ni, Co, Fe, Mn and/or Zn, X3= Sb and/or Bi, X4= one or more alkali metals, X5= one or more alkaline earth metals X6= Si, Al, Ti and/or Zr, a = 1 to 6, b = from 0.2 to 4, from = from 0.5 to 18, d = from 0 to 40, e = from 0 to 2, f = from 0 to 4, g = from 0 to 40, n = is the number that is determined by the valence and amount of non-oxygen elements in the form of the OLE VII. 69. The method according to one of claims 1 to 32, characterized in that in the first stage, the crude propane in the presence and/or absence of oxygen is subjected to a heterogeneously-catalyzed dehydration and gas mixture 1 is subjected to a heterogeneously-catalyzed gas-phase Immokalee contained in the gas mixture 1 propylene. 70. The method according to one of claims 1 to 32, characterized in that in the first stage, the crude propane in the presence and/or absence of oxygen and in the presence of water vapor is subjected to a heterogeneously-catalyzed dehydration and formed in the first stage of the gas mixture 1 is completely or partially separate the water vapor condensation and resulting gas mixture 1' is subjected to a heterogeneously-catalyzed gas-phase partial oxidation and/or partial gas-phase Immokalee contained in the gas mixture 1' propylene. 71. The method according to one of claims 1 to 32, characterized in that in the first stage, the crude propane is subjected autothermal heterogeneously-catalyzed dehydration. 72. The method according to one of claims 1 to 32, characterized in that the gas mixture 1 and/or gas mixture 1' as a component of the gas mixture 2 is subjected to a heterogeneously-catalyzed partial gas-phase Immokalee contained in the gas mixture 1 and/or in the gas mixture 1' propylene.
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