Method of controlling cyclohexanol or cyclohexanone production processes

FIELD: industrial organic synthesis.

SUBSTANCE: invention relates to production of cyclohexanol or cyclohexanone via hydrogenation of phenol or benzene with hydrogen in presence of catalyst and diluent followed by hydration in case of using benzene as starting material. Process is characterized by that hydrogen and benzene or hydrogen and phenol preheated in heat exchanger, provided with condensate intake control circuit, and circulation gas are supplied to vaporizer and preheater, provided with heating steam consumption control circuits, through supply lines provided with shutoff valves. Phenol or benzene and circulation gas, as well as heating steam and condensate consumptions are specified and adjusted. Preheated mix is then fed into separator to separate gas from liquid phase, which is removed, while remaining gas mixture is sent to hydrogenation reactors comprising temperature control zones and heat-extracting tube-type condensers and provided with phenol or benzene, hydrogen and condensate control circuits, temperature sensors connected to controllers to adjust consumptions of phenol or benzene, hydrogen and condensate, and wherein diluent volume level compared to that of catalyst is controlled and hydration temperature is measured. Resulting product enters cooler and then separation column provided with cyclohexanol or cyclohexanone recovery level control and adjusting, wherefrom it is directed to gas circulation line comprising cooler, separator, and compressor equipped with pipelines with circulation gas consumption control circuits.

EFFECT: increased productivity with regard to cyclohexanol or cyclohexanone.

2 dwg

 

The invention relates to methods of producing and management in the contact apparatus in the presence of a catalyst of cyclohexanol or cyclohexanone and may find application in the chemical industry, for example, in the manufacture of caprolactam.

There is a method of automatic control of the catalytic process by filing the original of the mixture in the reactor depending on the flow rate, pressure drop along the length of the reactor. To improve the quality of the product flow of the mixture to adjust the activity of the catalyst, determined by the average differential pressure along the length of the reactor. (Ed. mon. No. 480439, 01 j 9/04, G 05 D 27/00, 1975). The disadvantage of this method is the low accuracy of determination of the activity of the catalyst and the deterioration of the quality of the product.

The known method for producing cyclohexanol/cyclohexanone mixed with cyclohexane and benzene, followed by separation of the products of the reaction of cyclohexanol/cyclohexanone and recirculation fraction allocated to stage regeneration at elevated temperature and pressure. To simplify the fuel mixture with benzene and then oxidize or hydratious, using the hydrogen supplied to the hydrogenation reactor (U.S. Pat. SU # 1833359, C 07 C 45/32, 35/05, 1993). The disadvantage is the low yield of cyclohexanol/cyclohexanone.

The known method p is produce cyclohexanol elektrokhimicheskim way. The method includes the recovery of phenol in sulfate environment to cyclohexanol at a hydrogen pressure of 1.5 MPa (U.S. Pat. Of the Russian Federation No. 2236395, IPC C 07 C 35/08, 29/20, With 25 In 3/04, 2003).

The disadvantage of this method is the low yield of cyclohexanol, in addition, the output depends on the hydrogen pressure, and to implement in an industrial environment requires additional equipment with appropriate control and management.

A known method of separation of cyclohexane in an industrial environment by rectification in two devices with capacitors, in which gases, water and part of the unreacted cyclohexane return to the column, and a concentrated fraction is used in the production of caprolactam (U.S. Pat. Of the Russian Federation No. 2226185, IPC C 07 C 13/18, 27/28, 45/82, 29/18, 2000).

The disadvantage of this method is the limited scope of application, and failure of gas emissions during the processing of raw materials (phenol, benzene).

The closest is the way of cyclohexanol by hydrogenation of phenol in the presence of a catalyst in a solvent environment, using a specific catalyst and the hydrogenation is conducted in aqueous-alcoholic medium (SU # 1051056, C 07 C 35/08, 1983). The disadvantage of this method is limited scope.

The task of the invention is to extend the scope of application of the method and p is increasing the performance cyclohexanol or cyclohexanone.

The problem is solved in that in the known process control method of cyclohexanol or cyclohexanone by hydrogenation of phenol or benzene with hydrogen in the presence of catalyst and diluent with subsequent hydration in the case of the use of benzene as the original product, with the supply line with shut-off valve, hydrogen and benzene or hydrogen and phenol, preheated in a heat exchanger with flow control condensate and circulating the gas is fed into the evaporator and the heater with the control circuits of the heating steam consumption, with set and adjust the costs of phenol or benzene and the circulating gas, and heating steam, and condensate then heated the mixture enters the separator for separating gas from the liquid phase discharged, with the subsequent receipt of ostavsheisya gas mixture in the hydrogenation reactor containing zones of temperature regulation and capacitors with pipes to remove heat and equipped with circuits for controlling the flow of phenol or benzene, hydrogen, and condensate temperature sensors connected to the controller with correction costs benzene or phenol, hydrogen and condensate level control volume of diluent with respect to the catalyst, to determine the temperature of hydration, when ethanologenic the product flows into the refrigerator, and then in separtion column with the control loop and the correction level selection of cyclohexanol or cyclohexanone, and in the line of circulation of the gases, consisting of a refrigerator, the separator and the compressor is equipped with a pipeline loops flow rate of the circulating gases. The study of the production of cyclohexanol/cyclohexanone showed that it is possible to produce a joint production by upgrading existing equipment. It is shown that for processing coal benzene and oil hydrogenation of benzene using the specifics of these processes. For processing coal benzene using elevated temperature and for processing the initial reagents (benzene or phenol) use temperature to avoid side reactions. In addition, use the methods of dilution of the upper and middle layers of the catalyst according to the height of the hydrogenation reactor at the appropriate temperature control, which increases the selectivity and speed of carrying out processes in the conversion of phenol or benzene in the cyclohexanol or cyclohexanone. To eliminate hazardous situations use the automatic cut off, which stops the supply of the raw materials for the process. For the effectiveness of the processes used otdelochnye and circulating gases. When the UE is the making use controllers, using standard P, PI-regulation to control costs of raw materials and products.

The essence of the invention is illustrated in the drawing, (without limitation of the scope of the invention) which depicts a schematic diagram of a control in the production of cyclohexanol/cyclohexanone obtained from phenol or benzene. The control circuit (1) includes units 1-13.

1 - heat exchanger for heating phenol;

2 - evaporator for heating the phenol/benzene, hydrogen, circulation and Obvodnogo gas;

3 - heater for phenol/benzene;

4 is a separator for separating gas from the liquid phase;

5 is a hydrogenation reactor;

6 - condenser for removing heat in the hydrogenation of phenol/benzene;

7 is a hydrogenation reactor;

8 - condenser for removing heat in the hydrogenation of phenol/benzene;

9 - the refrigerator to remove heat after hydrogenation;

10 - separation column for separation of cyclohexanol/cyclohexanone.

For the circulation of gases are used

11 - refrigerator; 12 - separator; 13 - compressors, which form a circulation system "column 10 - refrigerator 11 and the separator 12 to the compressor 13" to return the gas circulation process (in line otdelochnih gases). The control system is based on the controllers 14, which is connected with the sensors and valves 15-43, clicks the Zuya the loops. Electric communication line sensors and valves with controllers 14 in the drawings are arbitrarily shown with a gap (1, 2). The system includes

- flow control phenol 15, 16(the sensor 15, the valve 16), shut-off valve 17 and the controller 14 (which is not mentioned);

- flow control benzene 18, 19 and the valve 20;

- flow control of hydrogen 21, 22 and the valve 23;

- flow control circulating gas 15A, 15B;

- flow control pair (1,6 MPa) 24, 25 (the sensor 24 and the valve 25) for heating the phenol in the heat exchanger 1;

- loop control of the heating steam consumption (1.6 MPa or 4 MPa) 26, 27 for heating the phenol/benzene in the evaporator 2;

- flow control heating steam 28, 29 for heating the phenol/benzene in the heater 3;

- flow control condensate 30, 31 and 32, 33 in the capacitors 6, 8 for removing heat in the hydrogenation of phenol/benzene hydrogenation reactors 5 and 7;

- temperature sensors 34, 35, 36 in the hydrogenation reactor 5;

- temperature sensors 37, 38, 39 in the hydrogenation reactor 7;

- flow control of cyclohexanol/cyclohexanone 40, 41 in the separating column 10; valves 42, 43 on the supply line of phenol and benzene into the separator 4.

Way to get in contact apparatus of cyclohexanol or cyclohexanone OS is p, as follows.

Ask expenditures load:

phenol to 7,000 t/h (including at the start is not more than 0.2 t/h);

the benzene to 7,000 t/h (including at the start is not more than 0.5 t/h);

hydrogen up to 65 t/t;

the costs of the circulation path column 10-refrigerator 11 and the separator 12 to the compressor 13" - 3000 - 4000 nm3/h;

the level of volume of diluent relative to the catalyst of 0.44 (determined at the start of the reactor),

zone control temperature in the reactor 7, 5:

phenol is not more than 210°With alarm 210°and a lock 230°in the reactor 7 and 160-200°in the reactor 5 with alarm, 200°and locking 220°; (1A)

the benzene is not more than 240°With alarm 240°and a lock 250°in the reactor 7 and 170-230°in the reactor 5 with alarm 230°and a lock 240°C. (1B)

Injected into the controllers 14 information about current processes. When working on the phenol heated phenol enters the tube of the heat exchanger 1, which is heated by the condensate supplied to the annular space, and further flows into the evaporator 2, which is added to the circulating gas and the fresh hydrogen, where the components are heated, and then the mixture is fed to the steam heater 3, where it is heated to a temperature by supplying heating steam. Then the initial mixture enters the separator 4 (valve 42 is opened and the valve 43 is closed) the La branch of the gas from the liquid phase, then, if necessary, is discharged into the drain tank. Next the mixture goes into the tube space of the reactor 5, 7, provided with a capacitor 6, 8 for removing heat in the hydrogenation of phenol mixture.

After conducting hydrogenation reactions cyclohexanol raw goes in the fridge 9 and the separation column 10 for separation of cyclohexanol. From the top of column 10 otdelochnye gases go into the refrigerator 11, the separator 12 and a compressor 13, where it is compressed and recycled to the process, forming a circulation system "column 10 - refrigerator 11 and the separator 12 to the compressor 13". Then the circulating gases are in line otdelochnih gases to the feed with hydrogen in the process.

When working on the benzene heated benzene enters the tube space of the evaporator 2, where added otdelochnye and circulating gases and hydrogen. The components are heated due to the heat of condensation is supplied to the evaporator 2, and then the mixture is fed to the steam heater 3, where it is heated. Then the heated mixture is sent to the heat exchanger 1,which is heated to 155°when using petroleum benzene, and the use of coal benzene, the mixture is heated to a temperature of 230°With the supply of heating steam (3.9 MPa) and then sent to the separator 4 and then in the scheme through the reactor 5, 7, fridge 9 and the separator 10.

Considering the Rome examples of cyclohexanol and cyclohexanone.

Example 1

Phenol according to the sensor 15 with a pressure of 0.8 MPa and a flow rate of 2.3 t/h (at start-up of not more than 0.2 t/h) served in the pipe of the heat exchanger 1, which is heated to a temperature of 130-150°due to the heat of condensation of the vapor pressure of 1.6 MPa, supplied through valve 25 (control loop 15, 16,) in the annulus of the heat exchanger 1. Steam flow is calculated according to the temperature (conventionally not shown) and the pressure sensor 24 (the control loop 24, 25). Heated to 150°With phenol enters through the nozzle into the evaporator 2, which enters the circulation gas and Obvodny gas in the number of 3300 nm3(regulation circuit 15A, 15B) and fresh hydrogen according to the sensor 21 with a pressure of 2.1-2.4 MPa at a flow rate of 62 t/t (regulation circuit 21, 22). Evaporation of phenol in the mixture gas and hydrogen occurs due to the heat of condensation of the vapor pressure of 1.6 MPa, supplied through the valve 27 in the annular space of the evaporator 2. Steam flow is calculated according to the temperature (conventionally not shown) and the pressure sensor 26 (the control loop 26, 27). Then the initial mixture supplied to the heater 3 where it is heated to 175-180°by supplying heating steam pressure of 1.6 MPa, supplied through the valve 29 in the annular space heater 3. Steam flow is calculated according to the temperature (conventionally not shown) and the pressure sensor 28 (circuit maintains the cation 28, 29). Out of the heater 3, the reaction mixture enters the separator 4 (valve 42 is open and the valve 43 is closed), which is sent to the hydrogenation reactor 5, which is filled with catalyst. Process temperature significantly affects the selectivity and reaction rate of hydrogenation. The process of hydrogenation of phenol proceeds with evolution of heat. Optimal is the limit 170-180°the higher the ratio of phenol and hydrogen, the lower you must have the temperature in the reactor 5 and 7. In addition, by increasing the temperature increases the proportion of adverse reactions the formation of cyclohexane, methane, water and other organic compounds that must be considered when managing the process temperature with phenol. For a stable reaction is the dilution of the catalyst (before start-up of reactors) negotium material, which can be adjusted depending on the activity of the catalyst. When used to control the temperature sensors 34, 35, 36, as the average of measured sensors((175+176+180)/3=177° (C)located at the height of the catalyst. To maintain the temperature of 177°in the reaction zone is used, the capacitor 6. The condensate level is supported by the level sensor 30 and valve 31 (regulation circuit 30, 31). Then the reaction mixture is sent to a hydrogenation reactor 7, the cat is who so filled with catalyst and negotium material, as the reactor 5. For temperature control (the activity of the catalyst used, the sensors 37, 38, 39, as an average, measured by sensors, for example 179°C. the Heat is removed by the capacitor 8 with a level sensor 32 and valve 33 (regulation circuit 32, 33). From the reactor 7, the reaction mixture enters the refrigerator 9 (which cools the circulating water) and is directed into the separation column 10 (level supported by the regulation circuit 40, 41), where the liquid cyclohexanol raw is separated from the circulating gas and the amount of 2.1 t/h is sent to obtain caprolactam. The circulation gas (3000-4000 nm3/h) is sent on a path column 10 - refrigerator 11 and the separator 12 to the compressor 13" compression to a pressure of 1 MPa, and is returned to the process line circulation of gases (regulation circuit 15A, 15B) and together with hydrogen is used to retrieve the next batch of cyclohexanol. If the violation process operator command from the controller 14 acts on the shut-off valve 17 on the feed phenol (for example, when applying 0.1 t/h) and shut-off valve 23 to supply hydrogen. In addition, the control limits for alarm and locks in temperature (1A) upon receipt of cyclohexanol in the reactor 5, 7, which in this case do not go beyond the prescribed limits (177° 179°).

Example 2

Benzene according to the sensor 18 in the amount of 2.8 t/h compression 0.75 MPa (at start of installation of not more than 0.5 t/h) served in the tube space of the evaporator 2, where are heated to a temperature of 125-145°due to the heat of condensation of the vapor pressure of 1.6 MPa or 0.8 MPa, supplied through valve 27 (control loop 18, 19) in the annular space of the evaporator 2. Steam flow is calculated according to the temperature (conventionally not shown) and pressure 26 (regulation circuit 26, 27), there also comes the circulation and Obvodny gas 3700 nm3(regulation circuit 15A, 15B) and fresh hydrogen 64 t/g according to the sensor 21 (the control loop 21, 22). Then a mixture of benzene enters the heater 3 where it is heated to a temperature of 150°With due submission to the annulus of steam pressure 1.6 MPa (or 0.8 MPa)supplied through the valve 29. Steam is produced at a temperature and pressure sensor 28. Further, the heated mixture enters the heat exchanger 1 (valve 42 is closed and valve 43 is opened), where it is heated to 160°when using oil benzene pressure of 1.6 MPa, and when cleaning coal benzene to a temperature of 230°by supplying heating steam 3.9 MPa, supplied through valve 25 (control loop 24, 25).

From the heat exchanger 1 mixture enters the separator 4 and later in the hydrogenation reactor 5, which is filled with a catalyst with a solvent (reaction of benzene with hydrogen exothermic). Purification process of benzene from thiophene and the other is connected to the th is reduced to the absorption of sulfur compounds and hydrogenation with hydrogen at a temperature of 200-230° C. For a stable reaction can be measured in the temperature sensors 34, 35 and 36 (and as an average, measured by sensors, for example 215°). To maintain the temperature 215°in the reaction zone is used, the capacitor 6. The condensate level is supported by the level sensor 30 and valve 31 (regulation circuit 30, 31)item the reaction mixture is sent to a hydrogenation reactor 7. For temperature control are the temperature sensors 37, 38 and 39 (mean, measured by sensors, for example 220°). Temperature 220°supported by the capacitor 8 with level sensors 32 and valve 33 (regulation circuit 32, 33). From the reactor 7 cyclohexanone enters the refrigerator 9 in the amount of 2.6 t/h and is directed into the separation column 10, which supports a level of 40%, using the sensor 40 and valve 41 (the regulation circuit 40, 41) and next to the finished goods warehouse. In violation of the command of the controller 14 uses the shutoff valve 20 for supplying benzene (for example, 0.3 t/h) and the valve 23 to prevent the supply of hydrogen to the process. In addition, the control limits for alarm and locks (1B) temperature upon receipt of the cyclohexanone in the reactor 5, 7,which in this case went beyond the limits 215° 220°C.

Thus, modernization, with appropriate re-piping equipment the control loops allows the use of oil and coal benzene upon receipt of cyclohexanone to obtain caprolactam compared with other industries. To avoid side reactions control the temperature along the height of the catalyst's activity and, if necessary, use the methods of dilution of the catalyst, which increases the selectivity and speed of carrying out reactions of phenol and benzene to produce cyclohexanol or cyclohexanone. To eliminate hazardous situations use the selectors and to improve the efficiency of processes using the circulating gases, which ultimately increases the production efficiency.

The implementation of the method of controlling the production of cyclohexanol and cyclohexanone is scheduled for the 4th quarter of 2005 in Togliatti, "KuibyshevAzot".

The process control method of cyclohexanol or cyclohexanone by hydrogenation of phenol or benzene with hydrogen in the presence of catalyst and diluent with subsequent hydration in the case of the use of benzene as the original product, characterized in that the supply lines with shut-off valve, hydrogen and benzene or hydrogen and phenol, preheated in a heat exchanger with flow control condensate and circulating the gas is fed into the evaporator and the heater with the control circuits of the heating steam consumption, with set and adjust the costs of phenol or benzene and the circulating gas, and heating steam, and condensate, then the Greta mixture enters the separator for separating gas from the liquid phase, discharged, followed by the receipt of the remaining gas mixture in the hydrogenation reactor containing zones of temperature regulation and capacitors with pipes to remove heat and equipped with circuits for controlling the flow of phenol or benzene, hydrogen, and condensate temperature sensors connected to the controller with correction costs benzene or phenol, hydrogen and condensate regulation of the volume of diluent with respect to the catalyst temperature determination of hydration, with the resulting product arrives in the fridge, and then into the separation column with the control loop and the correction level selection of cyclohexanol or cyclohexanone, and in the line of circulation of the gases, consisting of a refrigerator, separator and the compressor is equipped with a pipeline loops flow rate of the circulating gas.



 

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10 cl, 14 ex

FIELD: chemical industry; new method of production of 2,4,4,6-tetrabromine-2,5-cyclohexadienon.

SUBSTANCE: the invention is pertaining to the new method of production of 2,4,4,6-tetrabromine-2,5-cyclohexadienon, which one has the wide application as the semi-finished product in chemistry of organic synthesis, for example at production of the linear poly(phenylene oxides). The method consists in production of 2,4,4,6-tetrabromine-2,5-cyclohexadienon in one container and provides for interaction of phenol with the brominating substance consisting of the mixture of the alkaline metal /alkaline earth metal bromide and the alkaline metal /alkaline earth metal bromate soluted in the deionized water at presence of the acid, extraction, washing and drying of the deposit with production of 2,4,4,6-tetrabromine-2,5-cyclohexadienon. The technical result of the invention is simplification of the production process due to usage of phenol as the original substance and the combination of the alkaline metal /alkaline earth metal bromides and the alkaline metal /alkaline earth metal bromates.

EFFECT: the invention ensures simplification of the production process due to usage of phenol as the original substance and the combination of the alkaline metal /alkaline earth metal bromides and the alkaline metal /alkaline earth metal bromates.

15 cl, 4 ex

FIELD: chemical industry; methods of production of the diene compounds.

SUBSTANCE: the invention is pertaining to the field of chemical industry, in particular, to the method of production of the diene compound of the formula CR1R2=CR3CFR4CR5R6OCR7=CR8R9 (1), which includes the initiation of the reaction of Claisen rearrangement for the compound of the formula CFR1R2CR3=CR4CR5R6OCR7=CR8R9 (2) in the mixture containing the diene compound of the formula (1) and compound of the formula (2), with production the product containing the reaction product of Claisen rearrangement of the formula CR5R6=CR4CR3 (CFR1R2) CR8R9CR7=O (3) and the diene compound of the formula (1), and separation of the diene compound of the formula (1) from the reaction product of Claisen rearrangement. At that R1-R9 in the above-stated formulas may be similar or different, and represent the atom of halogen, the atom of hydrogen, the trifluoromethyl group or the trifluoromethoxy group. The method allows to produce the diene compound of the formula (1) with the high degree of purity.

EFFECT: the invention ensures production of the diene compound of the formula (1) with the high degree of purity.

8 cl, 9 ex

FIELD: chemical industry; methods of production of phenol and acetone.

SUBSTANCE: the invention is pertaining to the field of chemical industry, in particular, to the industrial process of production of phenol and acetone by the cumene method. The method is realized by decomposition of the technological cumene hydroperoxide in the in series connected reactors in two stages with formation on the first stage of the dicumylperoxide at the temperature of 40-65°С at presence as the catalytic agent of 0.003-0.015 mass % of the sulfuric acid with its subsequent decomposition on the second stage in the reaction medium at the temperature of 90-140°С. The process is conducted at the excess of phenol in the reaction mixture at the molar ratio of phenol : acetone exceeding 1, preferentially - from 1.01 up to 5. Excess of phenol is formed either by distillation (blowing) of acetone or addition of phenol in the reaction medium. The technical result of the invention is reduction of formation of hydroxyacetone, which one worsens the quality of the commercial phenol.

EFFECT: the invention ensures reduction of formation of hydroxyacetone, which one worsens the quality of the commercial phenol.

5 cl, 4 ex, 8 tbl

FIELD: organic chemistry, chemical technology, catalysts.

SUBSTANCE: invention relates to catalytic decomposition of organic hydroperoxides representing important compounds on organic synthesis. Decomposition of cycloalkyl hydroperoxides comprising from 6 to 12 carbon atoms results to formation a mixture of corresponding alcohols and ketones. Process is carried out in the presence of a solvent (alkane, halogen-containing hydrocarbon) at temperature from 20°C to 200°C. Catalyst comprises ruthenium as a catalytically active metal added to a solid carrier chosen from the following group: carbon prepared by pyrolysis of acetylene and metal oxides chosen from the group comprising zirconium, aluminum, lanthanum and manganese. The amount of catalyst expressed as the mole percents of ruthenium to the amount of moles of hydroperoxide to be decomposed is from 0.0001% to 20%. Preferably, the catalyst comprises one additional rare-earth element as a component of alloy. The carrier represents, as a rule, metal oxide with high specific surface above 10 m2/g but preferably, above 100 m2/g that is resistant against oxidation. The hydroperoxide concentration is in the range from 1 to 80 wt.-% with respect to the solution mass. Preferably, hydroperoxide represents cyclohexyl, cyclododecyl, tetraline, ethyl benzene or pinane hydroperoxide and hydrocarbon used in preparing the parent hydroperoxide is used as a solvent. Invention provides the development of the modified catalyst enhancing conversion and selectivity in decomposition of hydroperoxides.

EFFECT: improved method for decomposition.

8 cl, 24 ex

FIELD: industrial organic synthesis.

SUBSTANCE: process comprises providing alcohol-water-gas mixture via evaporation of water-methanol mixture, combining the latter with air and emission gas, catalytic dehydrogenation of methanol on silver catalyst at elevated temperature followed either absorption of formaldehyde from reaction gases or chemisorption thereof from indicated gases with urea solution in column to produce and recover formalin in case of absorption or urea-formaldehyde solution in case of chemisorption. Into absorption/chemisorption stage, preheated emission gas is supplied in weight proportion to methanol (0.25-6,8):1. Generally, emission gas is preheated to 50-130°C.

EFFECT: increased concentration of produced formalin or urea-formaldehyde solution, widened concentration control range, simplified equipment, and reduced fire risk.

2 cl, 1 dwg, 4 ex

FIELD: organic chemistry, chemical technology.

SUBSTANCE: 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.

EFFECT: improved method of synthesis.

12 cl, 7 dwg, 1 ex

FIELD: organic chemistry, chemical technology.

SUBSTANCE: 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.

EFFECT: improved method of synthesis.

12 cl, 7 dwg, 1 ex

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