A method of producing methanol

 

(57) Abstract:

Usage: mainly organic synthesis. The inventive product - methanol BF CH4O. Specific productivity of the catalyst from 0.50 to 0.62 tonnes of methanol/m3catalyst including Reagent 1: gas mixture with a volume ratio of CO/CO2= 0,004-1,25 previously restored in the presence of aluminoborosilicate catalyst at 400-600oWith, 20-70 MPa, flow rate 5029-40236 h-1to the degree of conversion of CO to CO2equal of 24.90-80,58%. Reagent 2: hydrogen. Reaction conditions: at elevated temperature and pressure in two stages in the presence of a copper-containing catalyst. table 2.

The invention relates to the field of organic synthesis, in particular to the synthesis of methanol on copper-containing catalysts at elevated temperature and pressure of a mixture of carbon oxides and hydrogen, mainly from a mixture of carbon dioxide and hydrogen.

A known method of producing methanol [1] from carbon dioxide and hydrogen in the presence of highly active and selective catalyst at a temperature of 280aboutC and a pressure of 120 atmospheres under adiabatic conditions. The raw material used flue gases: diox the RA. To produce 1 t of methanol by this method requires 760 nm399% CO2and 2400 nm3H2while the flow of hydrogen is higher than in a conventional process for the synthesis of methanol from hydrogen and carbon oxides.

Closest to the invention is a method of producing methanol [2] by contacting a mixture of carbon oxides and hydrogen with copper-containing catalyst at a temperature of 190-270aboutC and a pressure of 50-100 ATM in two stages. In the first stage, the gas mixture containing FROM 0.7 to about 30. and CO20,3-23,6 about. when the ratio of CO: CO2(0,03-87):1, in contact with the catalyst in reactor consisting of one or a cascade of two reactors. In the second stage the process is conducted at a concentration of CO2in the incoming gas mixture 0.4 to about 20. and the ratio of CO:CO2equal to (0.25 to 55):1, preferably from 0.25 to 3.6):1, followed by separation of the methanol and water known techniques in multiple devices or a single for both stages of the device.

The disadvantage of this method is the low specific productivity of the catalyst upon receipt of methanol from gas mixtures with a high content of carbon dioxide, as well as the high water content in methanol raw, more than 30 wt.

The purpose and the OLE raw.

This goal is achieved by the fact that methanol is produced by contacting a mixture of carbon oxides and hydrogen with copper-containing catalyst at elevated temperature and pressure in two stages with separation of methanol by known techniques, and the source gas with a volume ratio of CO/CO2equal 0,004-1,25, previously reduced to the degree of conversion of carbon dioxide to carbon monoxide, equal of 24.90-80,58% water formed is separated, and the resulting gas mixture is sent to the methanol synthesis.

The essence of the proposed method of producing methanol is as follows.

The source gas containing carbon dioxide and hydrogen or carbon monoxide and hydrogen at a volume ratio of CO/CO2equal 0,004-1,25, heated in the heat exchanger to a temperature of 400-600aboutWith using an additional source of heat, for example heat converted gas and fed into the reactor with a bulk velocity 5029-40236 h-1under pressure from 20-70 ATM. The reactor may be a tubular flow type or recycle gas mixture. In the reactor of carbon dioxide reduced to the degree of conversion of CO2in the carbon monoxide equal of 24.90-80,58%

As the catalyst recovery dioxide gas, the carbon monoxide conversion.

Used at the stage of recovery allocability catalyst developed by the research Institute of oil refining and according to THE 38-1-243-69 has the following composition, wt. the content of active ingredients: cobalt oxide COO 4; molybdenum trioxide of Moo312.

Aluminum oxide (Al2O3used as a carrier. This catalyst showed high selectivity in the process of recovering carbon dioxide, organic impurities in the water was either absent or contained in trace quantities (from 0.01 to 0.1 wt.). The gas discharged from the reactor with a temperature of 400-600aboutWith, send in a recuperative heat exchanger for heating the gas supplied into the reactor and then cooled in the refrigerator condenser and separating the formed water. After separation of the water mixture emerging from the reactor flow type or otdavaema of the cycle, if the recovery of carbon dioxide is carried out in the reactor recycle, heated in the heat exchanger, win the compressor and served on the first stage of the synthesis of methanol in a flow reactor with increased heat sink, for example in a tubular reactor. In the reactor, the gas mixture in contact with a copper-containing catalyst at a temperature of 250aboutC and the pressure is containing to restore 52-54 wt. CuO; 24-20 wt. ZnO; 5-6 wt. Al2O3. Heat due to the heat away from the reaction zone and is used, for example, to produce steam. The gas emerging from the reactor is sent to a regenerative heat exchanger for heating the gas supplied into the reactor and then cooled in the refrigerator condenser. After separation of the methanol in the separator gas stream is mixed with the recirculation gas to the second stage of the synthesis of methanol, compress the circulation compressor and through the recuperative heat exchanger is sent to the reactor. Formed in the second stage, the methanol condense in the cooler-condenser. After separation of the methanol in the separator of the gas (purge gas) is removed from the system, and the rest is mixed with the gas coming from the first stage, and serves on the suction side of the circulation compressor.

The process of methanol synthesis the proposed method, due to the peculiarities of the mechanism and kinetics of methanol synthesis. It is known [3] that methanol is produced directly from carbon dioxide in the course of two reversible interdependent reactions:

CO2+3H2CH3OH+H2O (1)

CO2+H2O CO2+H2(2)

The oxide of carbon is reaction (2) and taking the water from the reaction zone. In the absence of carbon monoxide or low ratio of CO/CO2in the source gas water strongly inhibits the reaction of formation of methanol. The proposed method can efficiently convert to methanol gas mixture of carbon dioxide and hydrogen or gas mixture with a low ratio of CO/CO2as at the stage of recovery of carbon dioxide can bring significant amounts of water and get gas for methanol synthesis favorable composition with the ratio of CO/CO2higher than in the feed gas.

Thus, the proposed technical solution is most effective when using a source gas containing a lot of carbon dioxide, namely, when the ratio of CO/CO2in the source gas is within 1.25 or less. At higher against the effect of introducing an additional stage of recovery of carbon dioxide is so reduced, that does not justify the cost of its implementation. The lower limit of the degree of conversion of carbon dioxide to carbon monoxide, equal of 24.90% corresponds to the case of the implementation of this method using a flow reactor for recovery of carbon dioxide at a temperature of 400aboutC. Maximum stereototal WITH/CO2and recovery is carried out at a temperature of 600aboutWith the reactor recycle. The achievement of a higher degree of conversion of carbon dioxide to carbon monoxide is possible, but will require additional costs: it is necessary to carry out the process at higher temperatures, low space velocities.

A distinctive feature of the proposed method for production of methanol is that the source gas mixture containing carbon oxides and hydrogen in the ratio of CO/CO2equal 0,004-1,25 before stage methanol synthesis to restore the degree of conversion of carbon dioxide to carbon monoxide, equal 2,90-80,58% of the resulting water is separated, and the resulting gas mixture is sent to the methanol synthesis.

P R I m e R 1 (comparative). 56068 nm3/h Converted gas containing about. CO223,60; 0,70; N272,15; CH4+ + N23,55 (ratio WITH/CO20,03), served in a tubular reactor of the first stage of synthesis of methanol containing 10 m3of the catalyst. The gas temperature at the reactor exit 260aboutWith the pressure of 50 ATM. In the first stage receive 4,88 t/h of methanol and 4.09 to t/h of water. Methanol raw contains 45,6 wt. water. After separation of the methanol gas is SUB> 5,00; 5,00; CH3HE 0,50, served on the second stage adiabatic reactor using recycle loaded with 40 m3of the catalyst. The flow rate of the circulating gas 400000 nm3/H. In the second stage gain of 13.18 t/h of methanol and 5,93 t/h of water. The water content in the methanol raw 31,03 wt. The number received at the first and second stages of the methanol is 18,06 t/h total capacity per unit volume of the catalyst of 0.36 t/m3h, the total water content in the methanol raw 35,68 wt.

In examples 2-6 preliminary restoration CO2in spend in the reactor recycle, and in example 7 in a flow reactor. Conditions and results for methanol synthesis examples 1-7 are summarized in table.1, and table.2 shows the material flows corresponding to examples 2-7.

P R I m m e R 2. The source gas in the number 41136 nm3/h, containing about. CO2TO 23.03; N274,78; N20,88; CH41,22; 0,09 (ratio WITH/CO2well 0,004), serves on the stage of restoration CO2in WITH. The reactor of this stage contains 5 m3aluminoborosilicate catalyst. The recovery process CO2to CO and H2About perform at a flow rate of recirculating the gas mixture 201180 nm3/h and the temperature and conversion of CO2in 66,99% After separation of the water-gas mixture in the amount of 33608 nm3/h composition, about. CO28,40; N269,09; N2ABOUT 0,06; N21,07; CH42,38; 19,00, served on the first stage of the synthesis of methanol. The flow type reactor contains 7 m3a copper-containing catalyst. The methanol synthesis is carried out at a temperature of 250aboutC, a pressure of 70 ATM, flow rate 4801 h-1. In the first stage receive 5,59 t/h of methanol and 0,19 t/h of water. The water content in the methanol raw 3,29 wt. After separation of the methanol gas in the number 20746 nm3/h composition, about. CO212,11; N270,23; N2ABOUT 0,10; N21,69; CH43,80; 11,66; CH3HE 0,41, served on the second stage of the synthesis of methanol. Adiabatic reactor using recycle, contains 13 m3a copper-containing catalyst. The flow rate of the circulating gas 150000 nm3/h space velocity 11538 h-1temperature at the inlet to the reactor and the reactor exit, respectively 230 and 257aboutC. In the second stage receive 6,80 t/h of methanol and 1,90 t/h of water. The water content in the methanol raw 21,82 wt. The total number of methanol obtained in the first and second stages, is KZT 12.39 t/h total capacity per unit volume of the catalyst of 0.62 t/m3h is P>3/h, containing about. CO222,41; N274,71; N20,91; CH40,64; 1,33 (the volume ratio of CO/CO2well 0,059), serves on the stage of restoration CO2in WITH. In the reactor recovery download 10 m3aluminoborosilicate catalyst. The recovery process CO2to CO and H2About perform at a flow rate of the circulating gas mixture 200506 nm3/h, a temperature of 500aboutWith the pressure of 20 ATM, flow rate 20051 h-1. You get 4,80 t/h of water. The degree of conversion of CO2in is 63,29% After separation of the water-gas mixture in the amount of 34230 nm3/h of the following composition, about. CO29,16; N269,63; N2ABOUT 0,15; N21,08; CH41,44; 18,54, served on the first stage of the synthesis of methanol. The reactor contains 7 m3of the catalyst. The methanol synthesis is carried out at a temperature of 260aboutC, a pressure of 80 ATM, flow rate 4890 h-1. In the first stage receive 5,94 t/h of methanol and 0.24 t/h of water. The water content in the methanol raw 3,83 wt. After separation of the methanol gas in the number 20395 nm3/h of the following composition, about. CO213,50; N271,36; N2ABOUT 0,01; N21,78; CH4OF 2.26; WITH A 10.74; CH3HE 0,35, served on the second stage of the synthesis of methane 11538 h-1. The temperature at the inlet of the reactor and the reactor exit, respectively, 235 and 261aboutC. In the second stage receive 6,97 t/h of methanol and 2.15 t/h of water. The water content in the methanol raw 23,57 wt. The total number of methanol obtained in the first and second stages, is 12,91 t/h total capacity per unit volume of catalyst 0.65 t/m3h, the total water content in the methanol raw is 15.62 wide wt.

P R I m e R 4. The source gas in the number 42113 nm3/h, containing about. CO223,09; N275,35; N20,85; CH40,62; 0,09 (volume ratio is 0,004), serves on the stage of restoration CO2in WITH. Charged to the reactor 20 m3aluminoborosilicate catalyst. The recovery process CO2to CO and H2About perform at a flow rate of the circulating gas 201469 nm3/h, a temperature of 600aboutC, a pressure of 50 ATM, flow rate 10073 h-1. You get 6.68 t/h of water. The degree of conversion of CO2in is 80,58% After separation of the water-gas mixture in the amount of 32096 nm3/h of the following composition, about. CO24,13; N267,66; N2ABOUT 0,06; N21,12; CH42,49; 24,54, served on the first stage of the synthesis of methanol. The reactor contains 7 m3SUP>. In the first stage receive 5,18 t/h of methanol and 0.05 t/h of water. The water content in the methanol raw 1,34 wt. After separation of the methanol gas in the number 20417 nm3/h of the following composition, about. CO26,13; N268,04; N21,76; CH4A 3.87; 19,57; CH3HE 0,63, served on the second stage of the synthesis of methanol. The reactor contains 13 m3of the catalyst. The flow rate of the circulating gas 150000 nm3/h space velocity 11538 h-1. The temperature at the inlet of the reactor and the reactor exit, respectively 230 and 263aboutC. In the second stage gain 7 t/h of methanol and of 0.85 t/h of water. The water content in the methanol raw 10,83 wt. The total number of methanol obtained in the first and second stages, is 12,18 t/h total capacity per unit volume of catalyst 0,61 t/m3h, the total water content in the methanol raw is 7,39 wt.

P R I m e R 5. The source gas in the number 40878 nm3/h, containing about. WITH 18,15; N274,56; N20,97; CH41,42; 4,90 (the volume ratio of CO/CO2well 0,270), serves on the stage of restoration CO2in WITH. In the reactor recovery download 10 m3of the catalyst. The recovery process CO2to CO and H2About performs at a flow rate of the circulating gas 200869 nm2in is 74,43% After separation of the water-gas mixture in the amount of 34432 nm3/h, containing about. CO24,81; H2 69,80; N2ABOUT 0,06; N21,16; CH42,32; 21,85, served on the first stage of the synthesis of methanol. The reactor contains 7 m3of the catalyst. The methanol synthesis is carried out at a temperature of 250aboutC, a pressure of 50 ATM, flow rate 4919 h-1. In the first stage receive 8,09 t/h of methanol and 0.12 t/h of water. The water content in the methanol raw of 1.44 wt. After separation of the methanol gas in the number 15668 nm3/h of the following composition, about. CO28,80; N273,29; N22,37; CH44,74; 10,52; CH3HE 0,28, served on the second stage of the synthesis of methanol. The reactor contains 13 m3of the catalyst. The flow rate of the circulating gas 150000 nm3/h space velocity 11538 h-1. The temperature at the inlet of the reactor and the reactor exit, respectively, 235 and 249aboutC. In the second stage receive 4,36 t/h of methanol and 1.09 t/h of water. The water content in the methanol-20 raw wt. The total number of methanol obtained in the first and second stages, is 12,45 t/h total capacity per unit volume of the catalyst of 0.62 t/m3h, the total water content in the methanol raw is 8,86 MASP20,40; CH41,67; 15,65 (the volume ratio of CO/CO2well 1,125), serves on the stage of restoration CO2in WITH. In the reactor recovery download 20 m3of the catalyst. The process is carried out at a flow rate of the circulating gas 450832 nm3h, a temperature of 400aboutC, a pressure of 50 ATM, flow rate 22542 h-1. When this receive 3.12 t/h of water. The degree of conversion of CO2in is 44,10% After water separation gas in the number 88785 nm3/h of the following composition, about. CO27,24; N267,66; N2ABOUT 0,06; N20,43; CH42,02; 22,50, served on the first stage of the synthesis of methanol. The reactor contains 18 m3of the catalyst. The methanol synthesis is carried out at a temperature of 250aboutC, a pressure of 50 ATM, flow rate 4933 h-1. In the first stage receive 12,72 t/h of methanol and 0.27 t/h of water. The water content in the methanol raw 2.15 wt. After separation of the methanol gas in the number 59843 nm3/h of the following composition, about. CO2OF 10.05; N267,79; N2ABOUT 0,01; N20,63; CH42.91 IN; TO 18.01; CH3HE 0,61, served on the second stage of the synthesis of methanol. The reactor contains 40 m3of the catalyst. The flow rate of the circulating gas 400000 nm3/h space velocity of 10,000 h-1. The temperature at the entrance to the t/h of water. The water content in the methanol raw 15,22 wt. The total number of methanol obtained in the first and second stages, is 33,89 t/h total capacity per unit volume of the catalyst of 0.58 t/m3h, the total water content in the methanol raw is of 10.72 wt.

P R I m e R 7. In contrast to examples 1-6, the stage of recovery CO2in carried out in the reactor flow type, which serves the source gas in the number 150870 nm3/h of the following composition, about. CO2FALL OF 19.88; N274,16; N20,99; CH41,80; 3,17 (the volume ratio of CO/CO2equal to the strength of 0.159). Charged to the reactor 30 m3almocabar - molybdenum catalyst. The process is carried out at a temperature of 400aboutC, a pressure of 70 ATM, flow rate 5029 h-1. You get 6,21 t/h of water. The degree of conversion of CO2WITH amounts of 24.90% After water separation gas in the number 142250 nm3/h of the following composition, about. CO215,60; N262,56; N2ABOUT 0,06; N21,05; CH42,11; 8,62, served on the first stage of the synthesis of methanol. In a reactor loaded 30 m3of the catalyst. The methanol synthesis is carried out at a temperature of 250aboutWith the pressure of 70 ATM, flow rate 4408 h-1. In the first stage receive 13,96 t/h of methanol is UP>3/h of the following composition, about. CO216,96; N273,12; N2ABOUT 0,01; N21,38; CH42,77; 5,40; CH3HE 0,36, served on the second stage of the synthesis of methanol. Charged to the reactor 60 m3of the catalyst. The flow rate of the circulating gas 600000 nm3/h space velocity of 10,000 h-1. The temperature at the inlet and outlet of the reactor, respectively, 235 and 258aboutC. In the second stage receive 30,90 t/h of methanol and 13,03 t/h of water. The water content in the methanol raw 29,66 wt. The total number of methanol obtained in the first and second stages, is 44,86 t/h total capacity per unit volume of catalyst 0,60 t/m3h, the total water content in the methanol raw is 26,41 wt.

From table. 1 it is clear that in all cases described in the examples, positive results: increased specific productivity of the methanol synthesis catalyst.

The initial recovery of carbon dioxide and separating the formed water reduces the water content in the methanol raw. In embodiments of this method the water content in the methanol raw substantially less than in the prototype. Thus obtained water does not contain salt and can be used to technologyyou.

Thus, the introduction of the pre-recovery of carbon dioxide can improve the composition of the gas entering the synthesis of methanol, to increase the specific productivity of the catalyst, and therefore, it becomes possible to reduce the download size of the catalyst and the dimensions of the methanol synthesis reactor. In addition, the process of the proposed method allows you to use as feedstock for methanol synthesis gas mixture with a high content of carbon dioxide and efficiently convert them into methanol. You get methanol raw with a low water content. The proposed solution allows you to expand the raw material base for the production of methanol. Emit significant amounts of carbon dioxide as a reaction product, and in the form of coal combustion products and hydrocarbons in all industries that consume large amounts of carbon-based fuels. Hydrogen also is often a waste product, for example, in the production of acetic acid. Using these sources of carbon dioxide and hydrogen, it is possible to organize the production of methanol considerable power, thereby to solve the problems of waste disposal, the comp is a mixture of oxides of carbon and hydrogen with copper-containing catalyst at elevated temperature and pressure in two stages, followed by separation of methanol, characterized in that, with the aim of increasing the specific productivity of the catalyst and reduction of water content in the methanol raw, original gas mixture with a volume ratio of CO/CO2equal 0,004 - 1,25 previously restored in the presence of aluminoborosilicate catalyst at a temperature of 400 - 600oC, a pressure of 20 to 70 ATM, flow rate 5029 - 40236 h-1until the degree of conversion of carbon dioxide to carbon monoxide, equal of 24.90 - 80,58%, the resulting water is separated, and the resulting gas mixture is sent to the step of methanol synthesis.

 

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EFFECT: the invention ensures the fullest usage of the catalyst activity in its last layers.

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1 tbl, 2 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to method of obtaining methanol from feeding flow enriched with hydrogen, carbon monoxide and carbon dioxide. Method includes: (a) contacting of feeding flow with methanol synthesis catalyst and obtaining technological flow which contains methanol, aldehides and ketones and unconverted hydrogen, carbon monoxide and carbon dioxide, (b) cooling of obtained technological flow to temperature between 20° and 200°C, (c) contacting of cooled technological flow with hydrogenisation catalyst active in reaction of aldehide and ketone hydrogeniosation into corresponding alcohols and obtaining technological flow enriched with methanol and depleted of aldehides and ketones, (d) cooling and condensation of technological flow enriched with methanol and depleted of aldehides and ketones, and separation of stage (d) technological flow into gas phase and liquid phase with raw methanol.

EFFECT: ensuring efficient obtaining methanol from feeding flow, enriched with hydrogen, carbon monoxide and carbon dioxide.

4 cl, 3 tbl, 3 dwg, 2 ex

FIELD: technology for production of methanol from syngas.

SUBSTANCE: claimed method includes mixing of hydrocarbon raw material with water steam to provide syngas by steam conversion of hydrocarbon raw material and subsequent methanol synthesis therefrom. Conversion of hydrocarbon raw material and methanol synthesis are carried out under the same pressure from 4.0 to 12.0 MPa. In one embodiment hydrocarbon raw material is mixed with water steam and carbon dioxide to provide syngas by steam/carbonic acid conversion of hydrocarbon raw material in radial-helical reactor followed by methanol synthesis therefrom under the same pressure (from 4.0 to 12.0 MPa). In each embodiment methanol synthesis is carried out in isothermal catalytic radial-helical reactor using fine-grained catalyst with grain size of 1-5 mm. Methanol synthesis is preferably carried out in two steps with or without syngas circulation followed by feeding gas from the first or second step into gasmain or power plant.

EFFECT: simplified method due to process optimization.

12 cl, 3 tbl, 3 dwg

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to the improved method for preparing methanol. Method involves the successive feeding hydrocarbon-containing gas, injection of chemically purified water, carrying out the preliminary steam reforming for preparing synthesis gas and carrying out the final reforming if formed gas with addition of oxygen under pressure for carrying out synthesis of methanol, heating reactor for preliminary reforming by flow of obtained synthesis gas going out from reactor for the final reforming that is fed to intertubular space of reactor for preliminary reforming followed by cooling synthesis gas obtained as result of reforming by vapor-gas mixture and carrying out synthesis of methanol in 2-step reactor. Cooling the reaction mixture for carrying out isothermal reaction for synthesis of methanol in intermediate external heat exchanger of two-step reactor is carried out with vapor-gas mixture and cooling flow going out from reactor for synthesis of methanol is carried out with vapor-gas mixture and chemically purified water. Also, invention relates to unit for preparing methanol including the source of hydrocarbon-containing gas and unit for complex preparing gas, reactor for preliminary vapor reforming heated with flow going out from reactor for final reforming, two-step reactor for synthesis of methanol, heat exchangers for cooling synthesis gas, heat exchangers for cooling flow going out from reactor for synthesis of methanol, separator for separation of reaction products and exhausting gases and crude methanol. The unit for preparing methanol is assembled with unit for complex gas preparing including block for preparing chemically purified water, block for preparing raw, additional manufacture involving torch making, cleansing constructions, sources of electric energy, air of control and measuring instruments and automatic equipment, chemical laboratory and operating block. Two-step reactor for synthesis of methanol joined with heat exchanger for cooling synthesis gas with vapor-gas mixture, intermediate external heat exchanger for cooling the reaction mixture with vapor-gas mixture is joined in-line with heat exchanger for cooling flow obtained in reactor with vapor gas mixture, heat exchanger for cooling of chemically purified water and separator for separation of reaction products. Ignition device is assembled in reactor for final reforming that promotes to carry out the start of unit without trigger furnace. Water is injected in flow hydrocarbon gas directly before heat exchanger for the reaction mixture that provides excluding boiler-utilizer and trigger boiler from schedule and to solve the problem for cooling the reaction mixture in reactor for synthesis of methanol also. Based on integration of the device for preparing methanol in technological schedule with unit for complex preparing gas and significant change of the conventional schedule for preparing methanol method provides 3-fold reducing capital investment.

EFFECT: improved method for preparing methanol.

2 cl, 1 dwg

FIELD: organic chemistry, chemical technology.

SUBSTANCE: method for synthesis of methanol involves the following stages: removing hydrocarbon gas to be processed, sulfur elimination, catalytic steam conversion to obtain converted gas, heat utilization with separation of water, synthesis of methanol and separation of condensed methanol. Hydrocarbon gas with unstable composition is removed under pressure 0.001 MPa, not less, and sulfur elimination of hydrocarbon gas with unstable composition is combined with stage of step-by-step stabilization of pressure to form steam-gaseous mixture. Methanol synthesis is carried out for at least two successive flow steps with reducing volume of catalyst under pressure 1.5 MPA, not less, and separation of methanol between successive stages. Method provides significant reducing cost of gas processing and service of devices and allows carrying out the processing in mobile traveling devices in field conditions. Invention can be used in processing gas with unstable composition, for example, casing-head petroleum gas in petroleum-extracting holes, in field conditions in small traveling devices.

EFFECT: improved preparing method.

2 cl, 2 dwg

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to a new method for preparing methanol and other aliphatic alcohols by gas-phase interaction of hydrocarbon gases with water vapor under effect of ultraviolet radiation. Methanol and other aliphatic alcohols are prepared by direct hydroxylation of hydrocarbon gas or mixture of hydrocarbon gases with water vapor. For this aim hydrocarbon gas and vapor or mixture of gases and vapor are fed into reactor wherein the reaction mass is subjected for effect of ultraviolet radiation in wavelength range 240-450 nm at temperature lower vapor formation point. The end product is isolated from vapor-gaseous mixture by condensation and unreacted gas or mixture of gases removed from the reaction zone is purified from the end product by bubbling through water layer and recovered into reactor by adding the parent gaseous component in the amount equal to consumed one. The process is carried out for a single stage and can be realized under atmosphere pressure. Invention can be used in chemical, petroleum chemical, petroleum processing and petroleum and gas extracting industry.

EFFECT: improved preparing method.

2 cl, 1 tbl, 8 ex

FIELD: industrial organic synthesis.

SUBSTANCE: invention relates to improved process of producing methanol from purge gas produced in basic methanol or ammonia synthesis. Process comprises dispensing compressed carbon dioxide into basic synthesis purge gas, heating resultant gas mixture to starting synthesis temperature, passing thus heated gas through methanol synthesis catalyst, cooling reacted gas, recovering condensed crude methanol, and separating non-condensed gas stream into return stream and purge stream, the former being designed for mixing with basic synthesis purge gas stream and passed to one or two circulation jet compressors. Circulation is effected by energy provide either by (i) pressure of basic synthesis purge gas, which is supplied to jet compressor and further dispensed into compressed carbon dioxide stream, or by (ii) pressure of compressed carbon dioxide, which is dispensed into jet compressor and then introduced into basic synthesis purge gas stream, or by (iii) pressure of basic synthesis purge gas and pressure of indicated compressed carbon dioxide, both being supplied to one or two jet compressors. Ammonia or methanol production purge gas is successfully used for production of methanol without utilizing additional hydrogen-containing streams.

EFFECT: reduced methanol production cost.

4 cl, 5 dwg, 1 tbl, 4 ex

FIELD: industrial organic synthesis catalysts.

SUBSTANCE: invention relates to copper-containing catalysts for low-temperature synthesis of methanol in fluidized bed at median pressure and provides catalyst, whose preparation involves impregnation and which contains oxides of copper, zinc, chromium, magnesium, aluminum, boron, and barium and has following molar ratio: CuO:ZnO:Cr2O3, MgO:Al2O3:B2O3:BaO = 1:0.3:(0.014-0.038):(0.047-0.119):(0.05-0.1):(0.007-0.014):(0.0292-0.054).

EFFECT: increased mechanical strength and wear resistance of catalyst.

1 tbl

FIELD: industrial organic synthesis catalysts.

SUBSTANCE: invention relates to copper-containing catalysts for low-temperature synthesis of methanol in fluidized bed at low pressure and provides a wear-resistant catalyst, whose preparation involves impregnation and which contains oxides of copper, zinc, chromium, magnesium, aluminum, and boron and has following molar ratio: CuO:ZnO:Cr2O3, MgO:Al2O3:B2O3 = 1:0.3:(0.15-0.2):(0.1-0.025):(0.25-0.3):(0.08-0.1).

EFFECT: increased mechanical strength and wear resistance of catalyst.

1 tbl

FIELD: industrial organic synthesis catalysts.

SUBSTANCE: invention relates to copper-containing catalysts for low-temperature synthesis of methanol in fluidized bed at high pressure and provides catalyst, whose preparation involves impregnation and which contains oxides of copper, zinc, chromium, magnesium, aluminum, boron, and barium and has following molar ratio: CuO:ZnO:Cr2O3, MgO:Al2O3:B2O3:BaO = 1:(0.7-1.1):(0.086-0.157):(0.05-0.15):(0.125-0.2):(0.018-0.029):(0.04-0.075).

EFFECT: increased mechanical strength and wear resistance of catalyst.

1 tbl

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