A method of producing methanol

 

(57) Abstract:

The invention relates to the chemical industry, in particular for the production of methanol from carbon-based feedstocks. The invention consists in the method of producing methanol, comprising a steam-oxygen conversion of hydrocarbons, the allocation of carbon dioxide from the reformed gas and the synthesis of methanol from carbon oxides and hydrogen, in which the feedstock is pre-storeroom to volume ratio of steam : gas 0.4 to 0.7, the conversion is carried out at a temperature steam-gas mixture at the inlet to the Converter, equal 260-300oWith volumetric steam : gas ratio, equal to 2.2-2.8 and pressure of 2.0 MPa, the carbon dioxide removal is carried out by a single stage of leaching solution of monoethanolamine to obtain the factorial f = 2,05-2,2 followed by drying and compression of the reaction mixture to a pressure of 8.5 to 9.5 MPa feed to the stage of synthesis. 1 table, 1 Il.

The invention relates to the chemical industry, in particular for the production of methanol from hydrocarbon raw materials.

A known method of producing methanol according to which the source gas mixture for the synthesis of methanol is produced by conversion of hydrocarbons with won input to the Converter when the pressure which has received the gas, i.e. without additional compression. In the reaction zone all the raw materials are subjected to partial oxidation with oxygen, the primary conversion, resulting receive the gas mixture for the synthesis of methanol with a ratio of reagents that are close to stoichiometric. Primary conversion is carried out at an absolute pressure of > 55 bar over the catalyst in tubes heated externally by the gas leaving the secondary zone conversion, moving countercurrent to the reaction mixture of the primary conversion.

In a preferred embodiment, water vapor is introduced into the flow of hydrocarbons fed to the Converter, up to saturation, and the excess steam is removed from the converted gas by direct contact with cold water. This method provides no need to use steam under high pressure to remove it from the composition of the reformed gas. Cm. for example, Europatent N A, class C 07 C 29/15, 1989).

The main disadvantage of this method is the high energy consumption of the process.

There is also known a method of producing methanol, comprising obtaining a gas containing hydrogen and carbon monoxide by partial combustion of carbonaceous substances is dorod their interaction with water vapor, the allocation of part of the carbon dioxide from the gas obtained in the second stage, the interaction of the remaining gaseous carbon dioxide and hydrogen with the formation of methanol, drying the obtained product (see, for example, application France N 2288722, CL 31/04 C 07 C, 1976 prototype).

The main disadvantage of this method is not sufficiently high degree of purity of the target product and high energy costs.

A known method of producing methanol, comprising the conversion of natural gas or oil steam at 600-1000oWith pressure 8-53 ATM. in the presence of Nickel catalyst, the recovery of oxides of carbon with hydrogen to methanol at 215-450oAnd pressure 70-300 ATM in the presence of alumina-zinc-copper or aluminum-zinc-chromium catalyst, separation of the formed methanol, recycling unreacted mixture in the form of gases blowing partially or fully on the stage of conversion of the mixture hydronaut at 180-200oWith speed and feed 100-300103h-1in the presence of a catalyst composition, wt. Nickel oxide 32-40; aluminum oxide 47-57; calcium oxide 3-21, with subsequent dehydroretinal at a temperature of 250-450oWith and feed rate of the raw material 10 50103h-1in the presence of the -1,2, and allocation of about 40-70. of hydrogen through palladium membranes (see, for example, USSR author's certificate N 829609, CL 31/04 C 07 C, 1981 similar).

The main disadvantage of this method is the high energy intensity of the process, and the need to use expensive catalysts and palladium membranes for purification of a gas mixture of methanol synthesis.

Objective behind the creation of the invention is to develop a method of producing methanol with low energy consumption, ensure the absence of harmful emissions and methanol obtaining the highest quality grade "AA".

The problem is solved by a method of producing methanol, comprising a steam-oxygen conversion of natural gas, the allocation of carbon dioxide converted their gas and synthesis of methanol from carbon oxides and hydrogen, in which the feedstock is pre-storeroom to volume ratio of steam:gas, equal to 0.4-0.7 by spraying heated to 150-170oWith gas condensate, the conversion is carried out at a temperature steam-gas mixture at the inlet to the Converter, equal 260-300oWith volumetric steam:gas ratio, equal to 2.2-2.8 and pressure of 2.0 MPa, the carbon dioxide removal is carried out by impressia the reaction mixture to a pressure of 8.5 to 9.5 MPa feed gas mixture at the stage of synthesis, which is carried out in shelving columns with stepped vipasyana gas at a temperature of 220-270oWith the pressure of 8.5 to 9.5 MPa for low-temperature copper-containing catalyst.

The essence of the invention lies in the fact that the developed technology provides significant energy savings for natural gas and oxygen, as well as the additional getting in the schema pair, having a pressure of 27 atmospheres.

In addition, generated during methanol has the highest quality and meet the AA brand through methanol synthesis at a pressure of 90 ATM.

According to the invention the source of hydrocarbon raw materials pre-storeroot heated gas condensate, circulating in the system. This allows the use of low-grade heat is converted gas and to reduce the consumption of process steam.

Steam-oxygen conversion of hydrocarbons is carried out in a shaft furnace, where the conversion takes place at low volume steam:gas ratio and the temperature of the gas mixture at the inlet to the Converter. This saves process steam for the process and saving of heat, i.e. the optimal thermal conditions of the conversion process and n is estlat 8-12% aqueous solution of monoethanolamine (MEA) to obtain the factorial of f is 2.05 and 2.1. This saves heat regeneration IEA solution.

Regeneration of the saturated solution of monoethanolamine is carried out by contact with the hot gas condensate, circulating in the system.

After removing part of the carbon dioxide gas mixture is subjected to drying by freezing the main remaining moisture and further or gas and contacting with Almagell.

This allows the supply to the compression of dry gas of the desired condensation.

The methanol synthesis is carried out in shelving columns using speed vipasyana gas in equal installments on each shelf of the column.

This allows the process at the optimum temperature for maximum yield of crude methanol and receiving from him methanol-rectified high quality, relevant brand "AA", with a mass fraction of methanol is not less than 99.9%

Then the gas mixture komprimiert to a pressure of 8.5 to 9.5 MPa, which is necessary for carrying out the process of methanol synthesis on copper-containing catalyst and produces a crude methanol of high quality and obtaining methanol-rectified mark "AA".

On centerperiphery, MON saturated steam, VPN water nutrient MediaElement, VPD water nutrient deaerated, the IEA monoethanolamine, IN the circulating water.

The method according to the schema as follows.

Source natural gas from the network under pressure of 2.0 MPa in the saturator 1, where the saturated water vapor contained in the gas condensate to volume ratio of steam:natural gas equal to 0.4:0,7, due to the heat circulating gas condensate from the scrubber 6.

Next, the gas-vapor mixture is heated in the heat exchanger 2 of the converted gas from the recovery boiler 5, is mixed with superheated steam and fed to the mixer 3 Converter methane.

The original oxygen from the network compremised in the compressor 16 to a pressure of 2.0 MPa, mixed with superheated steam, performing the protective function of steam and fed to the mixer 3 Converter methane. The total volume ratio of steam: natural gas in the mixer 3 is 2.2 to 2.8. After the mixer 3 steam-gas mixture enters the Converter methane 4, wherein the Nickel catalyst is provisionality conversion of natural gas to a residual methane content of 0,6-1,1 about. on dry gas. Temperature converterdownload in the boiler 5, where due to the heat get saturated vapour pressure of 2.7-3.0 MPa. After the recovery boiler 5 converted gas is cooled in the heat exchanger 2 gas-vapor mixture, then in the scrubber-cooler 6 circulating gas condensate in the heat exchanger 7 circulating water to a temperature of 40oC.

Chilled converted gas after the heat exchanger 7 is included in the separator 8 for cooling the condensed moisture and arrives in the Department of monoethanolamine treating gas 9, where at one step remove part of the carbon dioxide to obtain the factorial f [(H2-CO2)/(CO2+CO)] equal 2,05 - 2,2 necessary for carrying out the methanol synthesis.

Then cleaned the converted gas is fed to the drying in the adsorber 10, where it is removed from the residual moisture, after which the gas compremised in the compressor 11 to the pressure of 9.0 MPa and enters the synthesis of methanol shelf type with stepped vipasyana. In column 12 on the copper-zinc-chromium catalyst at a temperature of 230-250oC and a pressure of 9.0 MPa is the synthesis of methanol from methanol obtaining raw.

Next, methanol raw enters the rectification 13 to obtain commercial methanol-rectifier 5, heated in the heat exchanger 14 circulating gas condensate leaving the saturator 1, deaeribed in the deaerator 15, degraves in the heat exchanger 17 and enters the boiler 5.

The circuit of the gas condensate is as follows. In the scrubber-cooler 6, the flow of the cooled gas condensate for irrigation, heated converted gas leaving the scrubber 6 is connected with a gas condensate separated in the scrubber from the converted gas. Output stream with a temperature of 165-170oWith is divided into two streams. One stream, comprising 1/3 of the total goes to the saturation of natural gas in the saturator 1 and heating nutritional necesariamente water in the heat exchanger 14.

The second stream, comprising 2/3 parts of the total served to heat the nutrient deaerated water in the heat exchanger 14 and the regeneration monoethanolamine solution in office cleaning 9. Then both chilled stream are mixed and fed to the irrigation scrubber-cooler 6.

Example. Natural gas of the following composition, about. CO20,04; N20,8; Ar 0,75; CH495,5; C2H61,81; C3H80,74; C4H100,29; C5Hrochade through the nozzle, irrigated hot condensate with a temperature of 170oWith saturated water vapor to steam:gas 0,65.

After saturation vapour-gas mixture is heated in the heat exchanger to 290oWith, mixed with technological superheated steam to steam:gas 2.48 and is served in the annulus parovozoremontnom mixer. In the tube space of the mixer is fed steam-oxygen mixture with a ratio of steam: oxygen 0,47.

The amount of oxygen is 5297 nm3/PM

The total value pairs: natural gas output from the mixer is 2.8.

In mine Converter is steam-oxygen conversion of methane on Nickel catalyst GIAP-8. The number of converted gas at the outlet of the Converter 4563,5 nm3/h, a temperature of 870oC.

The warmth of the hot reformed gas is utilized to obtain the saturated vapor pressure of 2.7 MPa, for heating the gas mixture after saturation. The final disposal of heat takes place in the scrubber-cooler, where it is heated while the gas condensate used for the process of carbonation and regeneration of monoethanolamine.

The converted gas is supplied to onestops factorial gas is (N2CO2)/(CO2+ CO) 2,11.

Next, the converted gas is drained from moisture and quantity 24000 nm3/h at a pressure of 1.6 MPa compremised to the pressure of 9.0 MPa and enters the separation of methanol synthesis.

The methanol synthesis is carried out on a copper-containing catalyst in shelving columns with stepped vipasyana gas.

Methanol obtained raw comes at the Department of rectification, where it turns out the methanol-rectified mark "AA" in the amount of 8,44 t/h and THE corresponding 113-05-494-85. Comparative with the known method the data on the effectiveness of the inventive method for production of methanol are presented in the table.

A method of producing methanol, comprising a steam-oxygen conversion of natural gas, the allocation of carbon dioxide from the reformed gas and the synthesis of methanol from carbon oxides and hydrogen, characterized in that the feedstock is pre-storeroom to extensional relations vapor/gas 0,4 0,7, by spraying heated to 150 170oWith gas condensate, the conversion is carried out at a temperature steam-gas mixture at the inlet to the Converter 260 - 300oWith, the volume ratio of steam/gas of 2.2 to 2.8, and a pressure of 2 MPa, the carbon dioxide removal is carried out by what impressia the reaction mixture to a pressure of 8.5 to 9.5 MPa feed gas mixture at the stage of synthesis, which is carried out in shelving columns with stepped vipasyana gas at 220 270oWith the pressure of 8.5 to 9.5 MPa for low-temperature copper-containing catalyst.

 

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FIELD: chemical industry; production of synthesis gas, methanol and acetic acid on its base.

SUBSTANCE: the invention is dealt with the methods of production of synthesis gas, production of methanol and acetic acid on its base. The method of upgrading of the existing installation for production of methanol or methanol/ ammonia provides for simultaneous use of the installation also for production of acetic acid or its derivatives. The existing installation contains a reformer, to which a natural gas or other hydrocarbon and a steam (water), from which a synthesis gas is formed. All the volume of the synthesis gas or its part is processed for separation of carbon dioxide, carbon monoxide and hydrogen. The separated carbon dioxide is fed into an existing circuit of synthesis of methanol for production of methanol or is returned to the inlet of the reformer to increase the share of carbon monoxide in the synthesis gas. The whole volume of the remained synthesis gas and carbon, which has not been fed into the separator of dioxide, may be transformed into methanol in the existing circuit of a synthesis of methanol together with carbon dioxide from the separator and-or carbon dioxide delivered from an external source, and hydrogen from the separator. Then the separated carbon monoxide is subjected to reactions with methanol for production of acetic acid or an intermediate compound of acetic acid according to the routine technology. A part of the acetic acid comes into reaction with oxygen and ethylene with formation of monomer of vinyl acetate. With the help of the new installation for air separation nitrogen is produced for production of additional amount of ammonia by the upgraded initial installation for production of ammonia, where the separated hydrogen interacts with nitrogen with the help of the routine technology. As the finished product contains acetic acid then they in addition install the device for production of a monomer of vinyl acetate using reaction of a part of the acetic acid with ethylene and oxygen. With the purpose of production of the oxygen necessary for production of a monomer of vinyl acetate they additionally install a device for separation of air. At that the amount of nitrogen produced by the device of separation of air corresponds to nitrogen demand for production of additional amount of ammonia. The upgraded installation ensures increased production of additional amount of ammonia as compared with the initial installation for production of methanol. The invention also provides for a method of production of hydrogen and a product chosen from a group consisting of acetic acid, acetic anhydride, methyl formate, methyl acetate and their combinations, from hydrocarbon through methanol and carbon monoxide. For this purpose execute catalytic reforming of hydrocarbon with steam in presence of a relatively small amount of carbon dioxide with formation of the synthesis gas containing hydrogen, carbon monoxide and carbon dioxide, in which synthesis gas is characterized by magnitude of the molar ratio R = ((H2-CO2)/(CO+CO2)) from 2.0 up to 2.9. The reaction mixture contains carbon monoxide, water -up to 20 mass %, a dissolvent and a catalytic system containing at least one halogenated promoter and at least one rhodium compound, iridium compound or their combination. The technical result provides, that reconstruction of operating installations increases their productivity and expands assortment of produced industrial products.

EFFECT: the invention ensures, that reconstruction of operating installations increases their productivity and expands assortment of produced industrial products.

44 cl, 3 ex, 6 dwg

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.

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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.

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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

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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

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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

FIELD: chemical industry; installations and the methods of production of the synthesis-gas from the natural gas.

SUBSTANCE: the invention is pertaining to the field of chemical industry, in particular, to the installation and the method for simultaneous production from the natural gas of the methanol synthesis-gas, the ammoniac synthesis-gas, carbon monoxide and carbon dioxide. The installation consists of the in-series connected to each other assembly units and includes: the first reactor (A), in which at feeding of oxygen realize the transformation of the natural gas into the synthesis gas consisting of carbon monoxide, carbon dioxide, hydrogen and the steam; the second reactor (B), in which exercise the regular transformation of carbon monoxide into carbon dioxide; if necessary the compressor (C) using which the formed gases may be contracted; absorbing apparatus D, which serves for absorption of carbon dioxide and production of he mixture of monoxide with hydrogen used for synthesizing methanol; the refrigerating separator E, in which at feeding of the liquid nitrogen receive the ammoniac synthesis gas and simultaneously produces carbon monoxide, argon and methane. The invention allows to increase profitability of the installation due to production at one installation of several products.

EFFECT: the invention ensures the increased profitability of the installation due to production at one installation of several products.

15 cl, 1 dwg, 1 tbl

FIELD: industrial organic synthesis.

SUBSTANCE: invention relates to improved process of producing methanol from synthesis gas and can be used at methanol production plants. Process comprises mixing synthesis gas with circulation gas, heating obtained gas mixture to starting synthesis temperature, passing heated gas mixture through additionally installed preliminary adiabatic reactor, wherein partial methanol synthesis takes place and temperature rises. Stream is then passes additionally installed recuperating heat exchanger, wherein resulting reaction mixture is cooled to starting reaction temperature in first catalyst bed of the principal methanol synthesis reactor comprising several adiabatic catalyst bed. Reacted gas is cooled to isolate condensed crude methanol, while non-condensed gas stream is divided into two streams: return stream and purging stream. Return while non-condensed gas stream is compressed in circulation compressor and then is sent to be mixed with synthesis gas. Volume ratio of preliminary adiabatic reactor bed to the first bed of principal reactor lies within a range of 35 to 150%.

EFFECT: increased yield of methanol and reduced power consumption.

2 cl, 1 dwg, 1 tbl, 7 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

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