A method of producing methanol
The invention relates to a method of producing methanol from natural gas and "tail" of hydrocarbon gases in the chemical and petrochemical industries. The method includes the stage of synthesis gas, the catalytic conversion of the produced synthesis gas to methanol in multiple reactors at elevated temperatures and pressures, cooling the reaction products, separation of methanol and recycling tail gas. In the inlet zone of the reactor serves synthesis gas containing more than about 20. % nitrogen at a molar ratio of hydrogen and carbon monoxide in the range from 1.2:1 to 4:1. While periodically serves synthesis gas containing additional oxygen in a quantity not exceeding 0,9 about. %. As a rule, the process is carried out in the temperature range 160-300oWith the pressure of 4.0-10.0 MPa, volumetric flow rates 500-10000 h-1. Usually the source of the synthesis gas is divided into two streams, one of which is enriched with hydrogen mass transfer in the membrane installation type and fed to the first catalytic reactor and the second stream depleted in hydrogen, is mixed with a stream of gas leaving the last catalytic reactor after separation of methanol, and the mixture is fed to the power plant as gas fuel. The way I utilization of raw materials, to reduce the degree of deactivation of the catalyst during long-term operation of the installation to obtain the target product of high quality. 2 C.p. f-crystals, 2 Il. The invention relates to the technology of synthesis of methanol from synthesis gas obtained by partial oxidation of natural gas with air, oxygen-enriched air or the flow of oxygen-containing gas with a high content of nitrogen.More specifically, the invention relates to the field of chemical technology, energy-saving processes for the production of methanol from natural gas or "tail" of hydrocarbon gases in the chemical, petrochemical, gas processing and metallurgical industries.In the traditional industrial technologies for production of methanol is usually the first stage of the process is obtaining synthesis gas steam conversion of hydrocarbons of natural gas. At this stage is not reached full conversion of gaseous hydrocarbons into synthesis gas and therefore being further conversion at a later stage - steam-oxygen conversion. For its implementation is typically used pure oxygen, the receipt of which is associated with significant Energetica carbon and to reduce the content of carbon dioxide in it guided the processes of chemisorption of CO2in particular, solutions of ethanolamine or carbonates of potassium.The cost of the resulting synthesis gas containing a small amount of nitrogen is high enough to produce synthesis gas could be high profitability used in addition to the production of methanol in the production of olefin production, motor fuels, dimethyl ether. The latter circumstance is due to the fact that the reaction of steam reforming of light hydrocarbons is strongly indeterminacy and she, as well as the reaction of the steam-oxygen conversion of light hydrocarbons, is implemented in expensive equipment with significant energy and maintenance costs.Known techniques for producing methanol from natural gas (US 5245110), which provide for the production of synthesis gas by catalytic oxidation of natural gas with air or oxygen-enriched air. Reducing the cost of synthesis gas is achieved by reducing the cost of producing oxygen-enriched air in comparison with the costly production of pure oxygen, use the stage production of methanol synthesis gas with a high content of nitrogen converted into methanol in four or six series-connected reactors with intermediate output generated in reactors of methanol after each catalytic reactor. The tail gases of methanol production have a high heat of combustion, so you can use them as fuel for gas turbines. The nitrogen in the system catalytic reactors do not recycle and is discharged into the atmosphere with the exhaust gases of the gas turbine.Closest to the claimed method for the production of methanol, selected as a prototype, a method described in patent RU 2152378. In the method-prototype convert synthesis gas with a high content of nitrogen in the three serially connected catalytic reactors with intermediate selection generated in reactors of methanol after each catalytic reactor. Due to thermal operating modes of each catalytic reactor achieved a high overall conversion of synthesis gas at high quality target product.The disadvantages of the known methods of production of methanol on the basis of the synthesis gas with a high content of nitrogen (>20%) are: low conversion of synthesis gas when the hydrogen content in the synthesis gas is less than 15 vol.%, low volume load on raw when the content in the synthesis gas of nitrogen more than 70 vol.%, significant deactivation of the catalyst in literrature use when organizing small-tonnage production of methanol in the gas fields and medium-duty methanol chemical, petrochemical and gas processing enterprises.In the present invention are the following tasks: achieving high performance in the production of methanol on the basis of the synthesis gas with simultaneous high degree of use of raw materials, reducing the degree of deactivation of the catalysts for long-term operation of an industrial installation, obtaining the target product of methanol of high quality.The tasks are achieved by a method of producing methanol, comprising the stage of synthesis gas production, the stage of regulating the content of oxygen in it, the stage catalytic conversion of synthesis gas into methanol in multiple reactors, including heating operation and the conversion of synthesis gas, the operation of cooling the reaction products and separating methanol, operations recycling tail gas, in which the input zone of the reactor is fed with synthesis gas containing more than 20% vol. nitrogen at a molar ratio of hydrogen and carbon monoxide from 1.2:1 to 4:1 at elevated temperatures and pressures.The process of methanol synthesis carried out preferably in the temperature range 160-300oC, pressure of 4.0-10.0 MPa, volumetric flow rates 500-10000 h-1.By decreasing the activity of cat is ishushim 0,9% vol.To reduce energy consumption source synthesis gas can be divided into two streams, one of which is enriched with hydrogen mass transfer in the membrane installation type and fed to the first catalytic reactor and the second stream depleted in hydrogen, is mixed with the gas stream leaving, after separation of the methanol, the last catalytic reactor, and the mixture is fed to the power plant as gas fuel.In Fig. 1 illustrates the essence of the invention which involves the use of installation, consisting of serially connected reactors, focused, first, on the regulation of the oxygen content in the synthesis gas, and secondly, on the synthesis of methanol from synthesis gas with an intermediate conclusion of methanol after each catalytic reactor.The synthesis gas obtained in the energy machines in the reaction homogeneous partial oxidation of natural gas, contains 1.2 to 1.5 vol.% the oxygen. The latter has a concentration greater than the permissible concentration in the input flow reactors for methanol synthesis. Its reduction to values 0-0,9 about. % is achieved in the oxygen reactor 1, which is oxidized by oxygen of carbon monoxide to dioxide ua is in catalytic reactors 2, 3, 4, loaded promoted copper-zinc catalyst, each of which has an input zone 7 and root zone of the catalytic reaction 8. Zone 8 is connected with heat exchangers-condensers 9, 12, 15, and the last one with the separators 10, 13, 16. Before entering the installation of the synthesis gas passes through the compressor and flows into the heat exchanger 5.In Fig.2 schematically shows a power technological installation for production of methanol according to p. 4 claims. The installation further comprises a membrane element 17, a steam turbine 20, furnace heating combined-threads 19, the gas turbine 18.An energy-chemical method of producing methanol is implemented with the system shown in Fig.1, 2, as follows.Feedstock with synthesis gas obtained by partial oxidation of natural gas in internal combustion engines, gas turbines or catalytic reactors) served with a bulk velocity 500-10000 h-1in the compressor 5, where compremised to pressure, for example, 5.0 to 7.0 MPa. Then he goes into the reactor 1, in which the catalytic oxidation of part of the carbon monoxide synthesis gas residual oxygen output gases of the engine of internal combustion is mi flow reactor 2 to a temperature close to the onset temperature of the reaction for production of methanol. After the heat exchanger 6 synthesis gas is sent into the reactor 2, in the input zone 7 which it is heated to the reaction temperature. Then the synthesis gas is zone 8, which is the main conversion of synthesis gas to methanol. In zone 7, the original reactants are heated in boiling shirt catalytic reactor coolant, and in the zone 8 due to the heat release due to chemical reactions. From the reactor 1, the gas stream passes the heat exchanger 6, where it heats the feedstock to a temperature close to the temperature of the beginning of the reaction. Next, the gas flow through the cooler-condenser 9 is supplied to the separator 10, where the condensation of methanol and not condensable gases are directed into the heat exchanger 11 and then to the entrance area 7 of the reactor 3.The operating conditions of the reactors 3, 4 are similar to the operating conditions of the reactor 1. From reactor 4 product gas stream is fed through a cooler-condenser 15 to the separator 16, where the condensation of methanol, and non-condensable gases are fed into the recovery unit tail gas (shown in Fig.2). System gas transport communications installation organized on the 2, 3, 4.Option ways, corresponding to p. 4, as follows.Raw synthesis gas with a high nitrogen content exceeding 20% vol, served in the compressor on the suction line of the first stage which comes permeate stream from the membrane unit 17. In membrane apparatus receives a smaller portion of the flow of synthesis gas from the compressor 5. In item 17, the gas stream is divided into two streams. First - permeate stream enriched in hydrogen, the second - recently stream depleted of hydrogen and enriched with nitrogen.Enriched with raw hydrogen stream, komprimierung in the compressor 5, passes through three series-connected reactor 2, 3, 4 with the formation of methanol in each of them. In the separators 10, 13, 16 produced methanol is separated from the gas stream is collected in a common container and removed from the installation. Unreacted, non-condensable synthesis gas after the separator 16 is combined with retenti flow membrane element 17 and is directed into the gas turbine 18 to generate electricity. Flue gases of the turbine 18 are received in oven 19 for overheated steam coming from reactors 2, 3, 4. Superheated steam enters the steam turbine 20 to generate electricity.Pino, physico-chemical meaning of the present invention is that the synthesis of methanol in the synthesis gas and nitrogen (containing more than 20 vol.%) on the promoted copper-zinc catalysts is carried out in the presence of oxygen, the concentration of which in a certain way varies over time, which allows you to adjust the degree of vosstanovlenie the catalyst surface, which ensures its high performance.The invention is illustrated below with specific examples of embodiments of the method.Example 1. In the energy machine (diesel) served 1002 m3/h of methane and the oxidizer (air). The coefficient of excess oxidant 0,34. Formed 5400 m3/h of synthesis gas composition, vol.%: H227, 14, N252, CO22,5, O20,9. When receiving 1000 m3clean synthesis gas (without nitrogen) produced more than 0.35 MW of electricity.Produced synthesis gas (Fig. 2) is fed to the catalytic reactor 1 purification from oxygen. In the feedstock, the oxygen content of 0.0% at the exit of the reactor 1, the volumetric rate of the raw material 2500 h-1. After the catalytic reactor 1 raw material at a pressure of 6.0 MPa and a temperature of 195o(Raw material is heated grocery poses at the exit of the reactor 2 is cooled in the heat exchanger 9 and from the separator 10 non-condensable gases enter the reactor 3, which is formed 195 kg/h catalyzate. The product mixture at the outlet of the reactor 3 is fed into the heat exchanger 12 and the separator 13. Non-condensable gas components are served after heating the product flow reactor 4 into the reactor 4, which is formed 97 kg/hour of methanol. He after cooling the gas mixture in the heat exchanger 15 is separated in the separator 16. The tail-gas is directed to a gas turbine to generate electricity.After 300 hours of operation of the installation according to the above diagram, the reactor 1 is arranged so that in the feedstock supplied to the second reactor, the oxygen content was 0.2 vol%. The duration of operation under this part raw materials for 20 hours. Then 150 hours installing again operated in the absence of oxygen in the original synthesis gas. Then the cycle of oxygen with the specified time interval is repeated.After every 720 hours of operation switches the circuit feeding the feedstock into the reactor. The first 720 hours reactors operate in sequence 1-->2-->3, subsequent 720 hours in sequence 2-->3-->1, the following 720 hours in sequence 3-->1-->2 and, finally, after 720 hours - again according to scheme 1-->2-->3.Overall the Birmingham organization of the process according to the patent-prototype - less 747 kg/hour. The composition of the methanol produced by the new technology: the methanol is 98.8 wt.%, water - 1.2 wt.%. The content of organic compounds (ethanol, propanol, formate, dimethyl ether) in trace quantities.Example 2. In the energy machine due to partial oxidation 1005 m3/h natural gas is obtained 5400 m3/h of synthesis gas composition, vol.%: hydrogen 37,2, carbon monoxide 18,5, carbon dioxide, 2,5, methane, 1,5, the rest is nitrogen.The resulting synthesis gas with oxygen content 0,0% vol. from the reactor 1 is served after heating the product gases from reactor 2 to reactor 2, in which at a pressure of 7.0 MPa, a temperature of 210oC, flow rate 4000 h-1the synthesis of methanol. After cooling in the heat exchanger 9 and condensed in the separator 10 from the gas methanol and water non-condensable gas components are fed after pre-heating the product flow reactor 3 into the reactor 3. The pressure in the reactor 3 7.0 MPa, a temperature of 220oC. After cooling in the heat exchanger 12 and condensed in the separator 13 methanol, non-condensable gas components get hot product gases from reactor 4 and fed into the reactor 4, which at a pressure of 6.9 MPa and temperate 15 and condensation of methanol in the separator 16 non-condensable gases are directed into the gas turbine to generate electricity.When carrying out the process in the absence of oxygen in the synthesis gas and without switching the input stream of the synthesis gas at reactor 3 and 4, the average performance of each reactor at 1600 hours is: 2 - 749,4 kg/h, 3 - 336,5 kg/hour, 4 - 137,3 kg/hour. The overall average performance setup 1223,2 kg/hour.During the implementation of operation modes of operation (when the oxygen concentration of 0.4 vol.% and duration of treatment catalyst 10 hours) when intermittent oxygen average performance of the first reactor in the tri-reactor site of methanol synthesis is 810,0 kg/h, the second - 362,2 kg/h, the third - 163,3 kg/hour. The overall average performance setup 1335,5 kg/hour. After 8000 hours of operation of the reactor site, its overall average performance during intermittent oxygen was 1175,24 kg/h (88%). The average performance of the reactor 2 - 696,6 kg/h (86%), reactor 3 - 332,4 kg/h (89%), reactor 4 - 146,24 kg/hour (89,5%).Example 3. In the energy machine is the partial oxidation of 1020 m3per hour of natural gas. The composition of the produced synthesis gas, vol.%: the 29 hydrogen, carbon oxide 16, carbon dioxide 3, the rest is inert components (nitrogen and methane). Stream Sint is recently (760 m3/hour). Permeate stream enriched in hydrogen to a concentration of 33 vol.%, directed through the reactor 1 to reactor 2, in which at a pressure of 7.0 MPa, a temperature of 205oC and a flow rate of 3200 h-1when the oxygen concentration 0,0 about. % formed 489 kg/hour of methanol. In the reactor 3 at 7.0 MPa and 205oReceived 158,5 kg/hour of methanol in the reactor 4 at 7.0 MPa and 210oWith - of 83.4 kg/hour of methanol. The average plant capacity for 1500 hours 730,9 kg/hour of methanol.Recently stream is combined with the product gas stream of the reactor 4 is supplied to the gas turbine to generate electricity.If additional dosing in the synthesis gas of oxygen to a concentration of 0.6 vol. % and the duration of activation of the catalyst in each reactor 10 hours average plant capacity for 1500 hours is 752,0 kg/hour (when the process conditions defined in example 3).When metering in the synthesis gas of oxygen to a concentration of 0.8% vol. and duration of activation of the catalyst in each reactor 10 hours average plant capacity for 1500 hours is 732,0 kg/hour (when the process conditions defined in example 3). When dosing into synthesis gas KIS the partial oxidation 1234 nm3per hour of natural gas. Get 4100 nm3/h of synthesis gas composition, vol.%: hydrogen 47,2, carbon monoxide 25,1, carbon dioxide 5,0, nitrogen 22,0, the rest is methane.The resulting synthesis gas with oxygen content 0,0% vol. from the reactor 1 is served after heating the product gases from reactor 2 to reactor 2, in which at a pressure of 10.0 MPa, a temperature of 240oC, flow rate 10000 h-1the synthesis of methanol. After cooling in the heat exchanger 9 and condensation from the gas methanol and water non-condensable gas components served after pre-heating the product flow reactor 3 into the reactor 3. The pressure in the reactor 3 to 9.9 MPa, temperature 230oC. After cooling in the heat exchanger 12 and condensed in the separator 13 methanol, non-condensable gas components are heated product gases from reactor 4 and fed into the reactor 4, where the pressure to 9.9 MPa and a temperature of 220oTo carry out the synthesis of methanol. At the exit of the reactor 4 after cooling, the product mixture in the heat exchanger 15 and condensation of methanol in the separator 16 non-condensable gases are directed to the gas turbine to generate electricity.When carrying out the process in the absence of oxygen in si is/h, 4 to 92.4 kg/hour. The overall average performance setup 992,6 kg/hour.When implementing an operation mode setup (when the oxygen concentration of 0.6 vol. % and the duration of treatment catalyst 10 hours) when intermittent oxygen average performance of the first reactor in the tri-reactor site of methanol synthesis is 676,2 kg/h, the second - 301,8 kg/h, the third - 137,9 kg/hour. The overall performance of the installation 1115,9 kg/hour. When dosing into synthesis gas oxygen as the target product, methanol does not deteriorate.
Claims1. A method of producing methanol, comprising the stage of synthesis gas, the catalytic conversion of the produced synthesis gas to methanol in multiple reactors at elevated temperatures and pressures, cooling the reaction products, separation of methanol and recycling tail gas, characterized in that in the inlet zone of the reactor serves synthesis gas containing more than about 20. % nitrogen at a molar ratio of hydrogen to carbon monoxide in the range from 1.2: 1 to 4:1, with periodic feeding synthesis gas containing additional oxygen in quantities not exceeding 0,9% vol.2. A method of producing methanol by p. 1, wherein camarota flow 500-10000 h-1.3. A method of producing methanol by PP.1 and 2, characterized in that the raw synthesis gas is divided into two streams, one of which is enriched with hydrogen mass transfer in the membrane installation type and fed to the first catalytic reactor and the second stream depleted in hydrogen, is mixed with a stream of gas leaving the last catalytic reactor after separation of methanol, and the mixture is fed to the power plant as gas fuel.
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: 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: 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