Method for production of (meth)acrolein and (meth)acrlic acid compounds |
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IPC classes for russian patent Method for production of (meth)acrolein and (meth)acrlic acid compounds (RU 2279424):
  
 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
 Method for oxidation for preparing alkenes and carboxylic acids / 2276127
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.
 Oxidation process resulting in production of alkenes and carboxylic acids / 2275351
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.
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.
Catalysts for the oxidation of ethane to acetic acid and methods of their production and use / 2234368
 The method of obtaining acetic acid / 2233832
The invention relates to the production of acetic acid
 Method for selective derivation of 2-hydroxybenzoic acid and 4-hydroxybenzaldehyde and derivatives / 2220948
The invention relates to a new method of obtaining a mixture of 2-hydroxybenzoic acid and 4-hydroxybenzaldehyde or derivatives thereof, in particular to a method for the preparation of 3-methoxy-4-hydroxybenzaldehyde-vanilla, and 3 ethoxy-4-hydroxybenzaldehyde-ethylaniline, in which the mixture of phenolic compounds, one compound (A) contains a formyl or hydroxymethylene group in position 2, and the other compound (B) contains a formyl or hydroxymethylene group in position 4, which meets the General formula (IIA) and (IIB) in which Y1and I2identical or different, denote one of the following groups: group - SNO; group - CH2HE; Z1, Z2and Z3identical or different, denote a hydrogen atom, a radical alkyls1-C4alkenyl2-C4or alkoxyl1-C4linear or branched, phenyl radical, a hydroxyl, a halogen atom; is subjected to selective oxidation, in which the formyl or hydroxymethylene in position 2 of the compound (A) is oxidized to a carboxyl group and possibly hydroxymethylene connection group (C) at position 4 is oxidized to formyl group, and the oxidation is carried out in the presence of a base in an amount of from 2 to 10 moles per mole of the dryer is Noah acid and 4-hydroxybenzaldehyde or their derivatives
 Catalyst for oxidation of ethane and/or ethylene to acetic acid (options), the method of obtaining acetic acid / 2208480
The invention relates to catalytic compositions for the selective oxidation of ethane and/or ethylene to acetic acid, which in combination with oxygen includes items: MoandWbAgcIrdXeYf(I) where X denotes the elements Nb and V; Y represents one or more elements selected from the group including Cr, Mn, Ta, Ti, B, Al, Ga, In, Pt, Zn, Cd, Bi, Ce, Co, Rh, Cu, Au, Fe, Ru, Os, K, Rb, Cs, Mg, Ca, Sr, Ba, Zr, Hf, Ni, P, Pb, Sb, Si, Sn, Tl, U, Re and Pd; a, b, c, d, e and f indicate such gram-atom ratios of the elements, in which 0<a
 1,0b<1 and (a+b)=1; 0<(C+d)0,1; 0<e2 and 0f2
 Method for selective receipt of acetic acid and the catalyst / 2198869
The invention relates to a new method for selective receipt of acetic acid and used in the catalyst
 The method of obtaining 4-hydroxybenzaldehyde and its derivatives / 2194032
The invention relates to a new method of obtaining 4-hydroxybenzaldehyde and its derivatives, in particular for the preparation of 3-methoxy-4-hydroxybenzaldehyde (vanilla) and 3-ethoxy-4-hydroxybenzaldehyde (ethylvanillin)
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 producing acrolein / 2031096
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.
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 -unsaturated aldehydes, method thereof and method of producing acrolein" target="_blank"> ,-unsaturated aldehydes, method thereof and method of producing acrolein" align="left" vspace="30" hspace="30" /> Catalyst to obtain ,-unsaturated aldehydes, method thereof and method of producing acrolein / 2135280
The invention relates to catalysts containing media, which caused the active phase on the basis of, in particular, molybdenum, Nickel, cobalt, bismuth, iron promoted with phosphorus and at least one alkali metal
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 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 acrolein and/or acrylic acid / 2285690
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.
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FIELD: improved method for production of (meth)acrolein and (meth)acrylic acid. SUBSTANCE: 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. EFFECT: stable and effective method for production of (meth)acrolein and (meth)acrylic acid without alteration of raw mixture composition, abrupt temperature elevation and reducing of catalyst activity and durability. 5 cl, 1 dwg, 2 ex
The technical field to which the invention relates. The present invention relates to a method for producing compounds of (meth)acrylic acid, in particular to a method for producing (meth)acrolein or (meth)acrylic acid, which includes membership in the reaction of propylene, propane or isobutylene by catalytic oxidation in the vapor phase in the oxidation reactor, when the weakening of the catalytic activity or the reduction of the useful life of the catalyst is prevented, which allows to obtain compounds of (meth)acrylic acid is continuously and efficiently. According to the present invention, the term "compounds of (meth)acrylic acid" means (meth)acrolein or (meth)acrylic acid, the term "(meth)acrolein" means acrolein or methacrolein and the term "(meth)acrylic acid" means acrylic acid or methacrylic acid. Description of the prior art As a reaction to produce (meth)acrylic acid using the method of catalytic oxidation in the vapor phase propylene, propane or isobutylene. According to the method of obtaining a (meth)acrylic acid by catalytic oxidation in the vapor phase propylene, propane or isobutylene conditions for oxidation to obtain a (meth)acrolein and for oxidation to obtain a (meth)acrylic acid during the next stage differ the Rog from each other. Accordingly, there is a two-step oxidation process, in which the corresponding oxidation reaction is carried out in the presence of different catalysts or in a separate reactor, and a process in which many types of catalysts are concentrated in a single reactor for the implementation of the oxidative reactions in the same reactor. At this stage, obtaining (meth)acrolein by catalytic oxidation in the vapor phase propylene, propane or isobutylene with molecular oxygen and/or the stage of obtaining the (meth)acrylic acid by catalytic oxidation in the vapor phase (meth)acrolein using molecular oxygen (hereinafter sometimes called the "method of obtaining compounds of (meth)acrylic acid"), for the regulation of catalytic activity and to prevent the formation of explosive gas in the gas containing a combustible gas, such as propylene and molecular oxygen, add gaseous water (steam) to obtain the raw material mixed gas. The drawing shows an example of the arrangement of the sequence of operations for obtaining acrylic acid by two-stage oxidation, when propylene with steam and air is oxidized in two stages in the first reactor and second reactor, containing a catalyst of molybdenum or similar type, for forming a gas containing acrylic to the slot. Such a gas containing acrylic acid comes in contact with water in the condensation column (cooling column) to obtain an aqueous solution of acrylic acid which is removed by adding a suitable extraction solvent in the extraction column, after which the extraction solvent is separated in the separation column for separating the solvent. Then separate the acetic acid separation column for separating acetic acid and get the crude acrylic acid, and then from the crude acrylic acid produce by-products in a distillation column and obtain purified acrylic acid. In addition, in recent years, instead of the above method, solvent extraction, whereby removing acrylic acid from an aqueous solution of acrylic acid is carried out with the aid of the extraction solvent, also use the method of azeotropic extraction, according to which are distilled with water and the azeotropic solvent so that from the top of the azeotropic separation column distilling the azeotropic mixture containing water and the azeotropic solvent, and from the lower part of the distilling acrylic acid. When methacrylic acid is produced by the method of catalytic oxidation in the vapor phase, isobutylene is subjected to oxidation in the vapor phase. In the case of the two-way oxidation of isobutylene oxidized to obtain methacrylic acid via obtaining methacrolein. In the course of obtaining compounds of (meth)acrylic acid composition of the raw gas mixture containing a fuel gas, such as propylene, molecular oxygen and gaseous water may change, which causes a reduction of the yield of the required product, or can dramatically increase the temperature of the catalyst, which causes the formation of sites of local overheating and thus leads to the deterioration of the catalyst or damage to production equipment. The document JP-A-5-229984 describes a method of obtaining acrylic acid by oxidation of acrolein, according to which the raw acrolein is preheated to increase the selectivity upon receipt of acrylic acid. In addition, the document JP-A-2000-53610 describes the proportions in the raw gas mixture and the temperature of the raw gas mixture at the inlet of the reactor to enhance the yield of acrylic acid. However, such methods create the problem of deterioration of the catalytic activity or the useful life of the catalyst. The present invention is to provide a method of obtaining a (meth)acrolein or (meth)acrylic acid, soda is people joining in the reaction of propylene, propane or isobutylene by catalytic oxidation in the vapor phase in the oxidation reactor, the change of the composition of the raw gas mixture, a sharp increase in temperature in the oxidation reactor and the deterioration of the catalyst activity or reduce the useful life of the catalyst is prevented and a constant and effective connection is obtained (meth)acrylic acid. Description of the invention The method of obtaining compounds of (meth)acrylic acid corresponding to the present invention, includes obtaining compounds of (meth)acrylic acid, which includes entry into the reaction raw material gas mixture by catalytic oxidation in the vapor phase in the oxidation reactor for the production of (meth)acrolein or (meth)acrylic acid, characterized in that the temperature of the raw gas mixture supplied into the oxidation reactor is maintained at least at the level of the condensation temperature of the raw gas mixture. Still water in a liquid state, formed by the condensation of gaseous water contained in the raw material gas mixture was in contact with the catalyst, resulting in the activity or the useful life of the catalyst decreased. In addition, due to the formation of such water in the liquid state composition of the supplied raw material gas mixture is smenyaetsya, resulting in the formation sites of local overheating, leading to problems such as decreased production of the required product, deterioration of the catalyst and damage to production equipment due to abnormal temperature increase. According to the present invention by maintaining the temperature of the raw gas mixture supplied into the oxidation reactor, at least at the level of the condensing temperature in the oxidation reactor is fed a raw gas mixture does not contain water in liquid state, resulting solved the above problems caused by the presence in the raw material gas of a mixture of water in the liquid state. According to the present invention it is preferable that the pipeline for the supply of raw gas mixture from the mixer raw substances in the oxidation reactor was heated and/or maintained in a heated condition to control the temperature of the raw gas mixture. In addition, the temperature of the raw gas mixture supplied into the oxidation reactor, preferably should not exceed 260°C. Brief description of drawing Fig. 1 is a process flow Diagram showing an example of the method of producing acrylic acid. Option of carrying out the invention Now will be described in detail option to implement the Oia method of obtaining compounds of (meth)acrylic acid, relevant to the present invention. The method corresponding to the present invention may be particularly suitable for the production of (meth)acrolein or compounds of (meth)acrylic acid by oxidation of propylene, propane or isobutylene gas containing molecular oxygen, using mnogotranshevogo reactor, or to obtain a (meth)acrylic acid by oxidation of (meth)acrolein gas containing molecular oxygen, using mnogotranshevogo reactor. As noted above, propylene, propane or isobutylene oxidized in two stages, during which the (meth)acrylic acid is obtained by obtaining (meth)acrolein. Accordingly, obtaining (meth)acrylic acid from propylene, propane or isobutylene carried out using two Novotrubny reactors, as shown in the drawing. The reaction may be carried out by bookmarks of different catalysts in the respective reactors or can be used a method of obtaining a (meth)acrylic acid, whereby the shell of one of the reactor is divided in at least two reaction compartment plate, located in the middle part of the pipe, and in corresponding with different compartments provide different catalysts. Thus, the present invention can be applied for the implementation of both processes. The catalyst used is used to obtain the (meth)acrylic acid, not limited to a specific type, but preferred widely used multi-component composite oxide catalyst with molybdenum type. In the oxidation reactor, such as Novotrubny reactor, served raw gas mixture containing propylene, propane or isobutylene, vapor and molecular oxygen and which regulate inert component, such as nitrogen or carbon dioxide. This raw gas mixture generated by mixing raw materials such as propylene, water, air, etc. in the mixer raw substances at the stage preceding the filing in the oxidation reactor. According to the present invention, for example, the pipeline for the supply of raw gas mixture from this faucet raw substances in the oxidation reactor is covered with insulating material or support in a heated state by means of lines with high temperature fluid medium such as steam or hot water, or raw gas mixture supplied into the oxidation reactor can be heated by a heater located between the mixer raw substances and oxidizing reactor. Thus, the temperature of the raw gas mixture supplied into the oxidation reactor support, at least at the level of the condensation temperature of the raw gas mixture. To maintain the temperature resource is the gas mixture, fed into the oxidation reactor, at least at the level of the condensing temperature by maintaining its heated condition and/or heating in this way, it is possible to use, for example, the following method. Before entering the oxidation reactor establish a thermometer and a pressure gauge and a condensation temperature of the raw gas mixture is determined by calculation, taking into account the composition and pressure of the raw gas mixture. Temperature corresponding components in the raw gas mixture and/or the heating temperature by the heater (the temperature at the outlet of the heater) can be adjusted so that the value measured by thermometer located at the inlet of the oxidation reactor, consistent with at least the condensing temperature calculated as described above. Thanks to this maintain the temperature of the raw gas mixture supplied into the oxidation reactor, at least at the level of the condensing temperature, the composition of the raw gas mixture will not deviate from the specified values in the catalyst layers of the oxidation reactor will be supplied raw material gas mixture of a given composition. In addition, it also prevents the growth temperature and the formation of sites of local overheating so that it becomes possible to obtain a high level of production it is possible to product. Now will be described an example of a method of calculating the condensation temperature of the raw gas mixture. For example, if mixed 10% vol. propylene having a temperature of 45°C, 75% vol. air having a temperature of 100°C, 10% vol. heated water vapor having a temperature of 132°and 5 vol.% nitrogen having a temperature of 20°C, to produce raw gas mixture pressure P=170 kPa, the temperature t of condensation will be 56,6°according to the formula Antoine: log10P[kPa]=7,074-1657/(227,0+t(°C)). According to the present invention the temperature of the raw gas mixture supplied into the oxidation reactor, which is maintained by maintaining the heated state and/or heating the raw material gas mixture coming from the mixer raw substances in the oxidation reactor can be modified depending on the condensation temperature of the raw gas mixture, namely depending on its composition or pressure. However, in the normal case, the lower limit of this temperature is preferably 60°and more preferably 80°C. additionally, the upper limit temperature of the raw gas mixture is preferably 260°S, more preferably 240°and most preferably 220°C. In particular, the temperature of the raw gas mixture supplied into the oxidation reactor, preferred is entrusted to exceed 5-25° With a condensation temperature of the raw gas mixture. By selecting the above preferred range of temperatures is possible to prevent an abnormal decrease in the activity of the catalyst in the oxidation reactor and an abnormal temperature rise, resulting in continuously and efficiently producing the compound (meth)acrylic acid. In addition, according to the present invention can be obtained compound (meth)acrylic acid in accordance with the conventional method under the condition that the temperature of the raw gas mixture supplied into the oxidation reactor is maintained at least at the level of the condensation temperature of the raw gas mixture by maintaining its heated condition and/or heating the raw material gas mixture supplied from the mixer raw substances into the oxidation reactor. For example, in the composition of the raw gas mixture or the reaction conditions in the oxidation reactor can be used the usual parameters. In General, the composition of the raw gas mixture can be set appropriately in such a range that substances such as propylene, propane or isobutylene, ranged from 5 to 13 vol.%, the air - from 37 to 87 vol.%, pairs from 3 to 26% vol. and nitrogen from 0 to 55 vol.%. Examples Now the present invention will be described in more detail with reference to examples and compare the global examples. Example 1 For the implementation of the oxidation reaction of propylene as the catalyst for the first stage was made of powder catalyst consisting of Mo12Bi5Ni3Co2Fefor 0.4Naof 0.2Bfor 0.4Ka 0.1Si24Ox(the content x of oxygen is the value determined by oxidation of the corresponding metals). Made of powder catalyst formed annular catalyst having an external diameter of 5 mm, an inner diameter of 2 mm and a height of 4 mm, as the reactor was used Novotrubny reactor having a reaction tube length of 3.5 m with an inner diameter of 24 mm and an outer diameter of 28 mm, the inner diameter of the shell of the reactor was 100 mm as a carrier was used molten salt nitrate, consisting of a mixture of nitrates, and it was served in the upper part of the reactor. As the reaction temperature was adopted temperature nitrate as the coolant fed to the reactor. In the respective reaction tubes laid 1.5 liters of annular catalyst of the first stage and in the upper part of the reactor was fed raw gas mixture under pressure of 170 kPa (kilopascals). As the raw gas mixture used a mixture obtained by mixing propylene, air, steam and nitrogen in proportions of 10%, 75 vol.%, 10% vol. and 5% vol. sootvetstvenno is. The condensing temperature of this raw gas mixture was 56.6°C. The pipeline between the mixer to produce raw gas mixture and the reactor was equipped with a line steam heating low pressure and is covered with insulating material to maintain the heated condition. In addition, the input section of the reactor was equipped with a thermocouple and pressure gauge and using the computer were constantly calculating and tracking the condensation temperature of the raw gas mixture. At the same time using a heater located between the mixer and the reactor, and the temperature controller was implemented to regulate the temperature of the raw gas mixture at the inlet of the reactor to maintain it at least at the level of the condensing temperature and the work was carried out so that the temperature of the raw gas mixture, as measured by thermocouple located at the entrance of the reactor remained constant at 80°C. In addition, we measured the temperature distribution by placing the reaction tube of the reactor thermometer, providing measurement at ten points along the axial direction of the pipe. The temperature was set to 330°and the work was carried out within one week, while the conversion of propylene was 97%, the development of acrolein SOS is Avila 92% and the maximum temperature in the catalyst amounted to 400° C. Work continued within one month from its beginning, while the temperature was maintained at 330°With the result that after one month the conversion of propylene was 96.8%, the development of acrolein increased by 91.9% and the maximum temperature of the catalyst amounted to 385°C. During this period, the temperature displayed by thermocouple located at the entrance of the reactor remained constant at 80°C. in Addition, by gas chromatography was carried out the analysis of the composition of the raw gas mixture at the reactor inlet and the measured values were equal to specified values. Comparative example 1 The work was carried out as according to example 1, except that the supply of steam for heating was discontinued, the insulating material was removed and the temperature control heater was stopped. The temperature was set to 330°and the work was carried out during the week, and the conversion of propylene was 97%, the development of acrolein was 91% and the temperature plots of local overheating of the catalyst layers 410°C. maintaining the temperature of the coolant at level 330°the work was carried out within one month from the beginning, resulting in the conversion of propylene composition is La 95,8%, develop acrolein amounted to 89.5% and temperature plots of local overheating of the catalyst amounted to 400°C. During this period, the temperature displayed by thermocouple located at the entrance of the reactor ranged from 40 to 42°C. in Addition, by gas chromatography was carried out the analysis of the composition of the raw gas mixture at the inlet of the reactor, propylene was 10.6%, the air was 74.4%, water was 4.4% vol. and nitrogen amounted to 10.6%. Work was stopped and the device was removed for study, while the pipeline was detected residual water. Industrial application According to the present invention in the process of obtaining a (meth)acrolein or (meth)acrylic acid through the implementation of catalytic oxidation in the vapor phase propylene, propane or isobutylene in the oxidation reactor can be continuously and efficiently to get the connection (meth)acrylic acid by preventing changes in the composition of the raw gas mixture, the abnormal temperature increase in the oxidation reactor and reducing the catalytic activity or the useful life of the catalyst. 1. The method of obtaining compounds of (meth)acrolein or (meth)acrylic acid, comprising feeding the raw material gas mixture through a pipeline from the mixer sirev the x substances in the oxidation reactor and the entry into the reaction raw material gas mixture by catalytic oxidation in the vapor phase to obtain a (meth)acrolein or (meth)acrylic acid, characterized in that the pipeline for the supply of raw gas mixture from the mixer raw substances in the oxidation reactor is heated and/or support when heated and the temperature of the raw gas mixture supplied into the oxidation reactor is maintained at a level above 5-25°With a condensation temperature of the raw gas mixture. 2. The method according to claim 1, in which the temperature of the raw gas mixture supplied into the oxidation reactor does not exceed 260°C. 3. The method according to claim 1, in which the composition of the raw gas mixture includes from 5 to 13% vol. propylene, propane or isobutylene, from 37 to 87% air, from 3 to 26% vol. steam and from 0 to 55 vol.% of nitrogen. 4. The method according to claim 1, in which the temperature of the raw gas mixture support with the help of thermometer and pressure gauge before entering the oxidation reactor and the temperature of condensation of the raw material gas mixture is determined by calculation, taking into account the composition and pressure of the raw gas mixture. 5. The method according to claim 4, in which the temperature of corresponding components in the raw gas mixture and/or the heating temperature of the heater is adjusted so that the measured values indicated by thermometer, corresponded, at least, the condensing temperature calculated by the above method.
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