A method of producing methanol

 

(57) Abstract:

Usage: in the chemical industry for preparation of methanol. The inventive product is methanol. B. F. CH4O, the performance of methanol 732-1170 kg/h of the Reagent 1: metadatabase gas. Reagent 2: oxygen or air. Reaction conditions: temperature 325-500oWith the pressure of 30-100 ATM, the oxygen concentration of 2-8%, moreover, the time of contact of the reacting gases of 0.2-10, and it should not exceed the time of diffusion of the reacting particles to the walls of the reactor, the flow of gases in the reactor are separated, and the reagent 1 is heated to 380-450oWith and served under the pressure of 10-100 ATM, and reagent 2 served under the pressure of 10-100 ATM and 40-50oWith, and at first served part of reagent 2, better not more than 1.5 vol.%, and the rest served in the already developed reaction without pre-cooling flow, the mixing time of the gases in the reactor is not more than 0.1 from the reaction time. 3 C.p. f-crystals, 2 Il.

The invention relates to organic chemistry, and in particular to methods for the production of methanol by direct oxidation of natural gas (methane), and can be used in chemical and gas industry.

Natural gas reserves are large, it is ecologicalinspires, uncomfortable. The problem solves turning natural gas into a more universal liquid fuel, in particular in methanol, which besides the original product of many chemical plants.

There are a number of ways to convert methane to methanol. The wide industrial application has a steam conversion of methane into synthesis gas (mixture of CO and H2with its subsequent catalytic conversion to methanol, but this process has some significant drawbacks: complexity of the equipment, very large energy consumption for the production of synthesis gas, a multi-stage process, high demands on the purity of gas, the lack of profitability of small and medium enterprises (less than 2000 t/day) (1).

Currently, the greatest interest is direct, bypassing the stage of synthesis gas production, gas-phase oxidation of methane to methanol at high pressures. Despite numerous research still does not have enough technology suitable for commercial production mode for carrying out the process of direct oxidation of methane to methanol at high pressures (2).

Known protective patents methods of producing methanol by direct oxidation of methane at elevated temperature is s for industrial development, as inferior in efficiency to the traditional way via synthesis gas.

Closest to the proposed method and the best known was the method of direct conversion of natural gas to methanol by oxidation of oxygen-containing gas (oxygen or air), including a thorough mixing of the reacting gases to achieve the fullest possible homogeneity) and carrying out the process in an inert reactor with an inner wall of the quartz or Teflon, to reduce the negative impact of the internal surface of the reactor to the process at a temperature of 300-500aboutC, a pressure of 10-100 ATM, the oxygen concentration in the reacting gas mixture 2-20% and the time of contact of the reacting gases 2-1000, followed by the separation of the target product by cooling the reaction mixture and condensation of methanol (6).

The known method (6) is carried out in a reactor with a diameter of 0.5-2.5 cm and a length of 40-45 see

The known method (6) differs from the other known processes, for example (3-5), high yield of methanol: up to 80-90% of the reacted methane, the methane conversion in the best experiments reaches 15-18% but like other known methods, is also not suitable strategy of industrial development of the W-velocity gas stream, the performance-limiting process. Thus, when the diameter of the reactor 25 mm, the length L of 45 cm, the reaction time t 10 C, a pressure of 100 ATM and the temperature in the reactor T 700 (400aboutC) gas volume v under normal conditions (Taboutand Rabout) passing through the reactor, is

V 9,510-3nm3/c

Because 90% selectivity and conversion 10% yield of methanol will be about 120 kg/1000 nm3hour performance installation methanol will not exceed

[Me] 4 kg/HR

It should also be noted that the implementation of the high performance of this method (6) strongly depends on the requirements of a high degree of uniformity of mixing of the reacting gases and the inertia of the inner surface of the reactor. The known method is also accompanied by the emergence of experimentally observed unstable, in particular, vibrational modes (7), which is unacceptable in commercial operation.

The objective of the invention is to develop a simple, workable and sustainable method for direct oxidation of methane to methanol, which would be effective enough for use in industry instead of the traditional and suitable for use directly in usloviia a method of producing methanol by oxidation metadatareader gas, including natural gas, oxygen or air at a temperature of 325-500aboutWith the pressure of 30-100 ATM, and oxygen concentration of about 2-8. followed by the separation of the target product by cooling and condensation, in which the time of contact of the reacting gases (reaction time) is maintained within the range of 0.2 to 1.0 sec, and the reaction time should not exceed the time of diffusion of the reaction products to the inner surface of the reactor, the flow mechanostrider and oxygen-containing gases in the reactor is carried out separately, with metanosoderzhashchie gas is pre-heated to 300-500aboutWith and fed into the reactor under a pressure of 10-100 ATM, and oxygen or air is fed into the reactor under a pressure of 10-100 atmospheres and at a temperature of 40-50aboutWith, and at first served only part of the oxygen needed to start the reaction, preferably not more than 1.5. while the main part of the oxygen is supplied in an already thriving and stable response without pre-cooling the gas stream and mixing time each supplied portions of oxygen or air with the main stream in the reactor does not exceed 0.1 of the duration of time spent in this portion of the oxygen.

The process is carried out at 325-500aboutWith predpochtitel is about 4,5. and unreacted metadatabase gas recycle.

The proposed method was developed on the basis of a detailed experimental study of the mechanism of the process of direct oxidation of natural gas to methanol using the methods of mathematical modeling. Studies have shown that the oxidation reaction proceeds by a chain mechanism with degenerate branching (in the mathematical model included 69 elementary stages). Identified three main stages of the process.

The initial stage of the process is razvetvlenno-chain reaction, in which there is a rapid increase in the concentration of active radicals. At this stage the important role played by the reaction of nucleation, branching and destruction of free radicals.

The second stage is stationary razvetvlenno-chain reaction, characterized by the equality of the velocities of the branching and quadratic recombination of active radicals. In the second stage of the process is the accumulation of intermediate products (peroxides and aldehydes), leading to the recent rapid warming. The first and most part of the second stage correspond to the experimentally observed induction period of the process. At the end of the second article is e process accompanied by a rise in temperature. When this happens the main discrepancy oxidant (oxygen).

On the third and final stage of the process, after using up one of the reagents oxygen recombination of radicals and relatively slow thermal noncorrosive transformation of volatile reaction products.

The principal result of this study is the finding that the decrease of oxygen concentration not only increases the response time, but on the contrary, reduce it by reducing the induction period, which is the most time consuming process. Therefore, the decrease of the ratio of reaction time to the speed of diffusion of the reactants can be achieved by reducing the oxygen concentration at the initial stage of the process. Another important result is the finding that the likelihood of an unstable oscillatory and holographing modes of the process increases with increasing concentration of oxygen in the initial stages of the reaction, especially at concentrations exceeding 4-5% So the flow at the initial stage the minimum required to start the reaction quantities is all right known from the literature (2), lowering the oxygen concentration reduces the selectivity of the formation of products of deep oxidation of methane, primarily oxides of carbon and, consequently, increases the yield of the target products of methanol and formaldehyde.

The data obtained about the mechanism of the reaction was allowed to offer a way fundamentally different from known (6).

In the known method (6) plays a big role as mixing gases and the inertia of the internal walls of the reactor, because the interaction of free-radical particles with materials commonly used for gas-phase reactor (stainless steel and other metal alloys), leads to their quick demise. As in the known method (6) the gas flow is very slow, the desired degree of mixing is achieved by applying before the reactor an additional mixing chamber, filled Teflon shavings, and the inertness of the surface is achieved through the use of inserts of "chemically inert" materials, such as glass or Teflon, and eliminate the possibility of contact of the reacting gases with chemically active materials such as metals, which creates significant difficulties in the implementation process.

In the proposed method, the negative impact of the internal surface of the reactor for the process is reduced to a minimum, but a fundamentally different way, namely the process carried out at the time of contact of the reacting gases not exceeding the time of diffusion of free-radical particles to the walls of the reactor while free radicals have time to react in the gas phase before reaching the walls. The necessary rapid mixing of gases is carried out in the turbulent regime through the use of multiple mixing blocks, the design of which is shown in Fig.1.

The process is carried out in a two-reactor made of stainless steel (see Fig. 1). The diameter of the sections d 20 cm, the length of each section having its own block mixing gases BS, 400 see If the diameters of nozzles supply of oxidizer d10.5 cm and nozzles natural gas d21.5 cm (see Fig.1) required for complete mixing of the reagents, the length of the channel mixing I 18 cm, and the number of nozzles in each block mixing is N 49. The velocity of the gas flow in the nozzle V 56 m/s, and in the reactor of 11.7 m/s capacity of the plant 120 is:

D UL

where = 0.01 turbulence; v is the linear velocity of the gas flow; L 0,15 d2the scale of turbulence for our conditions defined by the diameter of the channel mixing d2.

Because the turbulence scale L and the degree of turbulence , defined mixing nozzles, almost saved when the passage of the gases of the main part of the reactor, the same values can be used to calculate the time of diffusion in the reactor tdiffR< / BR>
tpdeff1,37

i.e., tdiff>p= 0,2-1, while the node mixture above structure, in addition to the main function performs the role of the device, reducing the turbulence scale (increasing time of turbulent diffusion) in the main part of the reactor.

In the first stage reactor serves natural gas and part of the oxidizer so that the oxygen concentration in the reactor did not exceed 1.5 about. The second similar section serves the rest of the oxidant. At the same time this design provides a low turbulence scale and the second section of the reactor. If necessary, obtain a higher degree of conversion of natural gas can be used more La more reliable low scale turbulence in the sections of the reactor can be equipped with additional partitions with holes with a diameter of 1-2 cm and a length of 15-20 cm Coming out of the reactor the gas after separation of the liquid products contain only small amounts of oxides of carbon, hydrogen, and in the case of oxidation by air, nitrogen, and may be again submitted to the reactor inlet (recycled).

The process is as follows.

Natural gas from pipeline under pressure of 10-75 bar. served either directly on the cleaned and heated, and then into the reactor, or in a gas compressor, where he komprimerede to the desired pressure (up to 100 ATM). Natural gas prior to feeding into the reactor is cleaned on a PTFE filter from residual moisture and gas condensate and heated first regenerative heat exchanger "gas-gas" 350aboutWith, then the heater (due to the heat of combustion of the fuel gas) to 380-450aboutC. Oxygen or air is compressed by the compressor to a pressure of 90 to 100 ATM, and sent to the reactor (temperature of the oxygen stream 40-50aboutC). In the reactor at a temperature of 325-500aboutWith (preferably at 380-450aboutC) pressure 30-100 ATM, and the oxygen flow about 2-8. (preferably 2,5-4,5%) flows through the oxidation process metadatareader (natural) gas to methanol product.

From the reactor the reaction mixture with the temperature of the natural gas from the highway and cooled to 120-140aboutC. Then the reaction mixture is fed to the cooler-condenser, the liquid reaction products (methanol, mixed with ethanol, formaldehyde, acetic acid and others ) are condensed. The obtained gas-liquid reaction mixture is fed into the machine neutralize acids, and then into the separator, in which a methanol product is separated from unreacted metadatareader gas, which is directed either in the backbone or on re-oxidation in the reactor.

P R I m e R 1 process: Pressure, MPa 10 Temperature,aboutWith 410 natural gas Consumption, nm3/h 58573 Flow of oxygen, nm3/h: section 1 889 section 2 889

The degree of conversion of oxygen, 95 reaction Time, with 0.3

Yield, kg/1000 m3missed gas: the methanol product raw 40 methanol 20

The performance of methanol, kg/h 1170

The average composition of the methanol product raw wt. methanol 49,8 ethanol 2.0 propanol 0.30 acetone 0.50 formaldehyde 8,0 formic acid and 0.50 water 38,2 other 0,70

P R I m e R s 2-4.

Thus, a relatively simple technology and equipment the method of producing methanol from natural gas capacity 1200 kg/h, suitable for use in hee is 2">

1. A METHOD of producing METHANOL by oxidation metadatareader gas, including natural gas, oxygen or air at 325 500oC 30 100 ATM and the oxygen concentration 2 8 about. followed by the separation of the target product by cooling and condensation, characterized in that the time of contact of the reacting gases is maintained within the range of 0.2 to 10.0 sec, and the reaction time should not exceed the time of diffusion of the reacting particles to the walls of the reactor, the supply of methane and oxygen-containing gases in the reactor is carried out separately, with metadatabase gas is pre-heated to 380 450oWith and fed into the reactor under a pressure of 10 to 100 ATM, and the oxygen-containing gas is fed under a pressure of 10 to 100 atmospheres and at 40 50oWith, and at first served only part of the oxygen is preferably not more than 1.5. and the rest served in the already developed reaction without pre-cooling flow and the mixing time of the gases in the reactor is not more than 0.1 reaction time.

2. The method according to p. 1, wherein the process is carried out at 370 - 470oC, preferably at 380 450oC.

3. The method according to p. 1, wherein the process is carried out at oxygen concentrations of 2.5 to 4.5.

4. The method according to p. 1, otlichayuschuyusya).

 

Same patents:

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

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FIELD: oxidation catalysts.

SUBSTANCE: invention relates to catalytic oxidation of saturated hydrocarbons with oxygen-containing gas. Process according to invention comprises contacting alkane with oxygen source in presence of catalyst including compound of general formula: , where R1 and R2 independently represent hydrogen atom, halogen atom, alkyl, aryl, cycloalkyl, hydroxy, alkoxy, carboxyl, alkoxycarbonyl, or acyl, or R1 and R2 can together form double bond or aromatic or non-aromatic ring; Y represents oxygen atom; X oxygen atom to hydroxyl group; m is integer 1 or 2; and n = 1. Process is conducted at 20 to 100°C. Advantageously, catalyst includes cocatalyst.

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FIELD: chemistry.

SUBSTANCE: invention pertains to the method of oxidation of hydrocarbons using oxygen in trifluoroacetic acid and can be used particularly for oxidation of alkanes, cycloalkanes, alkylaromatic hydrocarbons, alkenes, cycloalkenes. The method involves saturation of trifluoroacetic acid with oxygen, after which, the initial hydrocarbon is added to the obtained reaction medium and is kept until depletion of bound oxygen with obtaining the corresponding oxygen containing compound.

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1 tbl, 5 ex

FIELD: chemistry.

SUBSTANCE: present invention relates to a method of continuous oxidation of saturated cyclic hydrocarbons using oxygen, into a mixture of hydroperoxide, alcohol and ketones. The method involves feeding into the lower part of a column and in parallel flow, a stream of oxidisable liquid hydrocarbon and a gas stream containing oxygen, and degassing the liquid phase in the upper part of the column by forming a gas dome and extraction of the degassed liquid phase. The gas containing oxygen is let into different compartments of the column, and into the dome and/or liquid phase at the level of the degassing zone, or directly above. A stream of non-oxidising gas with output sufficient for maintaining concentration of oxygen in the gas layer at the level of volume concentration, less than or equal to the upper limiting concentration of oxygen is supplied.

EFFECT: possibility of implementing a method with high selectivity on an explosion safe level.

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FIELD: chemistry.

SUBSTANCE: method involves partial oxidation of an alkane contained in a gaseous crude stream, which contains an alkane, with oxygen contained in an oxygen-containing crude stream. Said method involves: forming a reactor system, having a back-mixing reaction chamber with injection mixing, which is connected to a tubular flow reactor, wherein said back-mixing reaction chamber with injection mixing ensures dwell time from about 0.05 s to about 1.5 s; feeding said crude stream containing alkanes and said oxygen-containing crude stream into said back-mixing reaction chamber with injection mixing; initiating formation of alkyl free radicals in said back-mixing reaction chamber with injection mixing to obtain a product stream from the back-mixing reaction chamber with injection mixing, containing oxygen, said alkane and at least a portio of said alkyl free radicals; feeding the product stream obtained in the back-mixing reaction chamber with injection mixing into the tubular flow reactor; and converting said product stream obtained in the back-mixing reaction chamber with injection mixing into said alkyl oxygenate in said tubular flow reactor; where said alkane is selected from group consisting of methane, ethane, propane and butane.

EFFECT: invention enables to obtain the end product using an efficient and cheap method without using a catalyst.

34 cl, 2 ex, 36 dwg

FIELD: chemistry.

SUBSTANCE: Invention relates to methanol production plant and to method of methanol production by oxidising methane-containing gas at said plant. Proposed plant comprises plant for integrated gas treatment, reactor gas-phase methane-containing gas oxidation consisting of gas-to-gas heat exchanger of reaction zone and gas-to-water heat exchanger of cooling zone, refrigerator-condenser, rectification unit, ecological system and gas burner. Note here that reaction mix maximum heat zone accommodates extra reactor made up of cylindrical tube with feeder of extra portion of cold methane-containing gas including natural gas, refrigerator-condenser communicated via injector with one of gas burner inlets.

EFFECT: higher yield of methanol per 1 m3 of methane in single cycle.

1 ex, 1 dwg

FIELD: chemistry.

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EFFECT: method enables to achieve high degree of conversion of starting reactants and high selectivity of formation of alcohols.

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FIELD: chemistry.

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EFFECT: method enables to obtain an end product with high output using readily available material using a simple method.

13 ex

FIELD: oil and gas industry.

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EFFECT: method is the simplest and the most economically feasible for processing of associated oil gas and natural gas with high content of methane homologs with production of dry gas and a range of valuable liquid products.

3 ex

FIELD: oil and gas industry.

SUBSTANCE: invention refers to oil and gas industry, namely to utilisation and processing methods for associated and natural gas with high methane homologue content to obtain oil products. Processing method for natural and associated gas with high content of heavy methane homologues by selective oxidation of hydrocarbon gas and further carbonylation of products obtained involves mixing of hydrocarbon gas with oxygen or oxygen-containing gas at molar ratio of heavy carbon components to oxygen 50.2:1, and selective oxidation of heavy components at air or near-air pressure and temperature of 500-800C, and products obtained are processed in the presence of carbonylation catalysts containing compounds of VIII group metals and phosphine (arsinic) ligands, at 80-120C and air pressure to obtain liquid products such as aldehydes, carbonic acids, diethyl ketone, polyketones, and dry fuel gas saturated with methane and purified from heavy components.

EFFECT: solution to the problem of associated oil gas utilisation, common to all oil companies.

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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