A method of producing methanol

 

(57) Abstract:

The invention relates to a method for producing methanol, which finds application in the field of organic synthesis. The method comprises contacting a gas mixture containing carbon oxides and hydrogen, with a copper-containing catalyst at a temperature of 190-290oC, a pressure of 5.0-10.0 MPa and flow rate 4500-100000 h-1. The source gas mixture containing 1.0 to 33,7% vol. oxide of carbon, 0.3 to 22,5% vol. carbon dioxide, when the volume ratio of hydrogen to the sum of the oxides of carbon, equal 1,91-the ceiling of 5.60 and 0.5-50,0% vol. nitrogen, sequentially passed through a cascade of two reactors at one stage. Typically, the methanol and water emit after each reactor. 1 C.p. f-crystals, 1 table.

The invention relates to the field of organic synthesis, in particular, to the production of methanol from carbon oxides and hydrogen.

A known method of producing methanol, which involves the reaction of oxide and carbon dioxide with hydrogen under a pressure of 1.0-15.0 MPa (preferably from 4.0 to 8.0 MPa), the temperature of 160-300oWith (preferably from 190 to 270oC), flow rate 7000-25000 h-1in the presence of a catalyst containing the oxides of copper and sincemy, the allocation of methanol from the reaction mixture and recycling the unreacted in the synthesis of methanol substances. As a raw material using a mixture of carbon oxides and hydrogen, and carbon dioxide is contained in an amount of 1-20 vol.% (preferably about 3-12. %). In the reaction gas in contact with the catalyst, the volume ratio of hydrogen to the sum of the oxides of carbon 1.3 to 3.0 times the stoichiometric (patent England 1159095, MKI 07 With 32/00, Z. 18.08.65 g, op. 23.07.69 year).

The disadvantages of this method are the low specific capacity of a copper-containing catalyst (0,191-0,425 kg/LCAS), as well as significant energy costs of recycling the gas mixture.

There is also known a method of producing methanol from synthesis gas containing hydrogen and oxides of carbon, in which fresh gas is fed into the reactor operated without circulation of the gas mixture and the unreacted gas after condensation of methanol served as the fresh gas into the reactor with circulating synthesis gas. The flow reactor operates izotermiczne. (Application Germany 3518362 MCI 31/04 C 07 C, Z. 22.05.85 g, op. 27.11.86 year).

The disadvantage of this method is the use of compressors more power for circulating the gas mixture in the second stage, and hence the finding is a method of producing methanol by contacting the gas mixture, containing carbon monoxide, carbon dioxide and hydrogen, with a copper-containing catalyst at a temperature of 190-290oC and a pressure of 5-10 MPa in two stages. In the first stage copper-containing catalyst is brought into contact with a gas mixture containing 5-30 vol.% of carbon monoxide and 0.3 to 20.0 vol.% carbon dioxide, when the volume ratio of carbon monoxide to carbon dioxide of 0.25-87 and the volume ratio of hydrogen to the amount of carbon oxides 2-3,65. This stage is carried out in a flow reactor or a cascade type flow rate of the source gas mixture 4500-100000 h-1thus the gas mixture containing carbon monoxide, carbon dioxide, hydrogen, methanol vapor and 0.02-1,38% vol. water vapors, these vapors of methanol and water are removed from the gas mixture. The remaining gas mixture containing carbon monoxide, carbon dioxide and hydrogen is fed to the second stage, which is carried into the reactor by circulation of the gas mixture with a bulk velocity 7000-15000 h-1getting after the second stage of the gas mixture containing carbon monoxide, carbon dioxide and hydrogen, methanol vapor and water, which are removed from the gas mixture (WO 88/00580, MKI 07 With 29/15, Z. 23.07.87, op. 28.01.88, prototype).

The disadvantages of this method include low udevil synthesis of 0.40-0.68 t/m3hour, a minor contribution of methanol obtained in the first stage, a total amount from 5.42 to 78,33%, high circulation rate of the gas mixture. This involves the use of a compressor of a large capacity and a significant expenditure of energy for circulating the gas mixture that significantly impairs the technical-economic indicators of the process. Another disadvantage of the proposed method is the limited range of concentrations of the components included in the source gas mixtures. Existing methods for the conversion of hydrocarbons allow you to receive gases with a high content of carbon monoxide and nitrogen than those declared in the prototype, for conversion to methanol. So high temperature conversion of hydrocarbons receive a gas mixture containing carbon monoxide more than 33%, and vapor conversion - gases with a nitrogen content of more than 40 vol.%. Proposed in the prototype method uneconomical to recycle methanol gases with a high content of carbon monoxide (greater than 30 vol.%), and high nitrogen content, although on industrial sites such necessity exists. In the first case, the ratio of reactants below the stoichiometric and reduced step the Institute of gas with a high nitrogen content decreases sharply specific productivity of the catalyst in the low content of reactive components of carbon monoxide, carbon dioxide and hydrogen gas in direct contact with the catalyst. While it is impossible to reach the accepted economic indicators of the process due to the high cost of energy for circulation of the gas, which consists mainly of nitrogen - inert component in the synthesis of methanol.

The basis of the invention the task is improving the method of producing methanol, which through the process in a cascade of two reactors at one stage, the cost of energy for circulation of the gas mixture and simplified flow chart of the process while maintaining a high specific productivity of the catalyst and a high degree of conversion of carbon oxides to methanol.

The problem is solved in that in the present method, the methanol is produced by contacting a gas mixture containing carbon oxides and hydrogen, with a copper-containing catalyst at a temperature of 190-290oWith the pressure of 5-10 MPa and flow rate 4500-100000 h-1while according to the invention, the source gas mixture containing 1.0 to 33,7% vol. oxide of carbon, 0.3 to 22,5% vol. carbon dioxide, when the volume ratio of hydrogen to the sum of the oxides of carbon 1,91-the ceiling of 5.60 and 0.5-50,0 about. % nitrogen consistently pada,

Salient features of the proposed method of production of methanol are as follows:

- methanol receive in two or more reactors operating without circulation of the gas mixture, sequentially connected in cascade, with the separation of methanol and water after each reactor,

- the source gas mixture is supplied to the first flow reactor, contains 1.0 to 33,7 about. % carbon monoxide, from 0.3 to 22.5% vol. carbon dioxide, when the volume ratio of hydrogen to the sum of the oxides of carbon 1,91-the ceiling of 5.60 and 0.5-50,0% vol. of nitrogen.

As raw material for methanol synthesis can be applied to the gas mixture obtained from a variety of materials, using various manufacturing processes, also waste gases other industries. Studies show, for the production of methanol in a cascade of two reactors can be recycled gases in a wide range of variation in the concentration of reactive components, achieving high performance of the catalyst of 0.45-2,85 t CH3HE/m3hour with a high degree of conversion of carbon oxides from 69,50 to 93,85%. The proposed limit of the ratio H2/CO+CO2equal 1,91-the ceiling of 5.60 for the source gas mixture selected from the following considerations. SN is glared in methanol due to the lack of hydrogen in the source gas, in subsequent reactors the ratio of reactants abruptly removed from stoichiometric. The upper limit of the volume ratio of N2/CO+CO2equal to the ceiling of 5.60, is determined by the fact that at higher relations decreases the specific productivity of the catalyst due to the low content of carbon oxides in the feed gas. The lower limit of the content of carbon monoxide in the source gas mixture of 1% vol. due to the fact that at low concentrations of carbon monoxide water dramatically inhibits the synthesis of methanol as it is formed by two reactions, both reaction 1 and reaction 2, which is due to a defect occurs in the direction of the hydrogenation of carbon dioxide:

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In case of using a gas with a low ratio of CO/CO2as seen from the table, reduces the specific performance of the catalyst, increasing the number of flow reactors in a cascade that leads to increased capital and operating costs.

The upper limit of the content of carbon monoxide 33,7% vol. due to the fact that at higher CO content ratio of the reactants is significantly below stoichiometric, which leads to the decrease of the degree Pravda carbon source gas mixture of 0.3% vol. due to the fact, upon the further reduction of CO2in Gaza, the rate of synthesis of methanol is sharply reduced, and in the absence of CO2the reaction of methanol synthesis in General is not (Kagan Y. B., A. Rozovsky I., Lin, I., and others, Kinetics and catalysis, 1975, I. 16, 3, page 809). Limitation upper limit for carbon dioxide to 22.5% vol. due to the same reasons as the upper limit of the area for carbon monoxide. In addition, at higher content of carbon dioxide in the feed gas by reducing the speed of the process increases the number of reactors in the cascade, if you are concerned about the depletion of carbon oxides. The upper area by nitrogen up to 50% due to the fact that nitrogen is an inert component and the increase of its concentration in the feed gas leads to a reduction in the content of the reactive components of carbon dioxide, carbon monoxide and hydrogen. This reduces the specific productivity of the catalyst and becomes uneconomic to process in a cascade of reactors gases with a higher nitrogen content. These negative phenomena are more evident (at high nitrogen content up to 50%) in the known circulation circuits, which require large particularly the am scientific-technical and patent information revealed the combination of all the essential features of the claimed technical solution is not known. So we can assume that the proposed method of producing methanol meets the requirements of novelty, because it is not known from the prior art.

Comparative analysis of the essential distinctive features of the proposed method and the known characteristics shows that these signs are used for the first time. And the whole set of essential features of the proposed technical solution allows to obtain a new result is to simplify the process flow and improve technical and economic performance of the process with a high degree of conversion of carbon oxides to methanol. Thus, we can conclude that the claimed method meets the requirements of inventive step.

The essence of the method consists in the following. The source gas mixture containing 1.0 to 33,7 about. % of carbon monoxide. 0.3 to 22,5% vol. of carbon dioxide at a volume ratio of H2/CO+CO2= 1,91-the ceiling of 5.60, under the pressure of 5-10 MPa fed into the heat exchanger where it is heated to a temperature of 200aboutC. the Heated gas mixture is fed to the first as the gas flow reactor with intensive heat sink, for example in a tubular re the cases (53.2 wt. % SiO, 27,1 wt.% Zn, 5.5 wt.% Al2ABOUT3) or copper copper-zinc-chromium (56,0 wt. % CuO, 25 2 wt.% Zn, 17 2 wt.% Cr2ABOUT3). In the process of reaction is methanol and water. The heat of reaction is used, for example, to produce steam, which can be used for technological purposes. The temperature of the gas mixture at the outlet of the reactor is slightly higher than the temperature of the source gas mixture at the inlet to the reactor. Emerging from the flow reactor a gas mixture containing carbon oxides, hydrogen, methanol vapor and water enters the heat exchanger for heat dissipation, and then emit from it in the separator methanol and water. Coming out of the separator gas mixture containing carbon oxides and hydrogen, is heated in the heat exchanger and serves in the second flow reactor. Depending on the process conditions (amount and composition of the source gas flow rate, temperature, pressure) cascade may include a different number of reactors - two or more. The parameters in all the reactors of the cascade, it is advisable to keep the same as in the first along the gas flow reactor.

The proof of the proposed method are the following examples.

Example 1 (crantzii in the reactor recycle gas mixture. In the first flow reactor serves the original gas mixture, where she at a temperature 251-265oC, a pressure of 8 MPa and a flow rate 28000 h-1contact with 10 m3a copper-containing catalyst. This forms a 24 t/h of methanol. Coming out of the first flow reactor, the gas mixture after the separation of methanol and water is directed to the second flow reactor, where it is at a temperature 255-264oWith the pressure of 8.0 MPa and flow rate 22602 h-1contact with 10 m3a copper-containing catalyst. This forms 22 t/h of methanol. After the second reactor, the gas mixture is sent to the third flow reactor. Here at the temperature 258-264oC, a pressure of 8 MPa and a flow rate 17847 h-1get 18 t/h of methanol. Just in the first stage receive 64 t/h of methanol, reaching the degree of conversion of carbon oxides 56,74%. Unreacted in the first stage, the gas mixture after separation of the methanol and water are served on the second stage in the shaft reactor, working with recycling where at a temperature 200-278oC, a pressure of 8 MPa and a flow rate 12250 h-1get 34 t/h of methanol. The total number of methanol obtained in the first and second stages is 98 t/h, the specific productive mixtures and process conditions shown in the table.

Examples 2-11.

Methanol receive in a cascade of two (examples 2, 9), three (examples 3, 4, 8, 10, 11), four (examples 5, 6) and six (example 7) flow-through reactors. The source gas mixture is fed under pressure to the recuperative heat exchanger. The heated gas mixture flows in a flow tube reactor with intensive heat sink where it is in contact with the copper-zinc-aluminum catalyst (examples 2, 4-10), containing a 53.2 wt.% CiO, 27 wt.% ZnO, 5.5 wt.% Al2ABOUT3or copper-zinc-chromium catalyst (example 3) containing 56 wt.% CiO, 26 2 wt.% ZnO, 17 2 wt.% Cr2ABOUT3. After cooling gas flow and condensation of methanol and water gas mixture in a quantity of heated and served in the second flow reactor, where it is again in contact with the catalyst, etc. Conditions for processes, expense ratios and unit performance given in the table.

In the table examples show that the inventive method opens the possibility to recycle the methanol gas mixture obtained by any known means conversion of hydrocarbons or waste gases, this expands the range of concentrations of both reactants to 33.7% vol. of carbon monoxide in the gas mixtures. Example also shows that the specific productivity of the catalyst in methanol is 0.45-2,84 t/m3hour, that is equal to or exceeds the same indicator of the prototype (0,52-1,09 t/m3hour) and is several times the value of specific performance of the catalyst, which is achieved in modern technology. In a modern industrial plant production of methanol specific productivity of the catalyst is relatively small from 0.1 to 0.3 t/m3h under a pressure of 5 MPa and up to 0.4 t/m3hour under a pressure of 8 MPa. In addition, in the proposed method, in the absence of recirculation of the gas mixture is achieved a high degree of processing of raw materials in methanol (70-94%) due to the fact that the removal of the reaction products (methanol and water) between the stages of the cascade eliminates thermodynamic inhibition of their process. For the traditional scheme to reduce the braking process, the reaction products and to reach almost full (85-95%) processing of carbon oxides to methanol synthesis it is necessary to conduct at high velocity gas circulation and intense conclusion of the cycle of liquid products, which requires a considerable amount of energy. The number of reactors in the cascade and the volume of a single reactor to savagelove power installation, given the market demand for methanol.

Implementation of the proposed method in a cascade of two reactors distinguishes it from other known methods, as it allows to completely eliminate the energy consumption for the circulation of gas, to simplify the process.

1. A method of producing methanol by contacting the gas mixture containing carbon oxides and hydrogen, with a copper-containing catalyst at a temperature of 190-290oC, a pressure of 5.0-10.0 MPa and flow rate 4500-100000 h-1, characterized in that the source gas mixture containing 1.0 to 33,7% vol. oxide of carbon, 0.3 to 22,5% vol. carbon dioxide, when the volume ratio of hydrogen to the sum of the oxides of carbon, equal 1,91-the ceiling of 5.60 and 0.5-50,0% vol. nitrogen, sequentially passed through a cascade of two reactors at one stage.

2. The method according to p. 1, characterized in that the methanol and water emit after each reactor.

 

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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

FIELD: chemistry.

SUBSTANCE: method includes contact of gas mixture containing carbon oxides and hydrogen ballasted down with nitrogen with copper-containing catalyst under heating, pressure and definite rate velocity of feeding into reactor. Reactor unit consists of two adiabatic-type reactors connected with a pipeline; the original gas mixture containing CO - 10-15 % v/v, CO2 - 0.3-5.0 % v/v, H2 - 15-40 % v/v, N2 -40.0-74.7 % v/v and volumetric ratio H2/(CO+CO2) equal to 1.00-2.91, at 200-260°C and pressure 3.5-5.0 MPa with rate velocity 2000-5000 h-1 is fed into the first reactor with larger main part of unconverted gas fed to circulation and produced at the outlet of the second reactor cooled to 15-20°C and further purified to remove methanol in tower washer and compressed; then the reaction mixture from the first reactor is fed into the second reactor along with the rest minor part of circulating gas indicated above as quench - cold circulation gas fed into the pipeline between the two rectors.

EFFECT: method allows increasing methanol yield, efficiency of the process and reducing energy consumption.

4 cl, 3 tbl, 1 dwg, 1 exsid1190496

FIELD: chemistry.

SUBSTANCE: invention pertains to the method of methanol obtaining from a concentrated mixture of hydrogen and carbon oxides with the following components in vol %: H2 - 62.0-78.5; Ar - 0.02-0.07; N2 - 0.05-2.2; CH4 - 1.0-3.5; CO - 10.4-29.5; CO2 - 3.2-10.7. The methanol is obtained by concentrating it in a copper containing catalyst at high temperature and pressure in two stages. The gas mixture from the reformer is divided into two streams in volume ratios of 100 : (1-50), one of which is in direct contact with the catalyst in the flow reactor at the first stage, at temperature of 200-285°C, pressure of 5-15 MPa and volume rate of 800-2000 h-1. The other stream is mixed with a cycled gas in volume ratio of 10 : (10-100) and with volume rate of 2500-10000 h-1. This stream is then channelled to the second stage, with separation of methanol and water on each stage in corresponding devices.

EFFECT: increased production of methanol and increased efficiency of the process.

1 tbl, 1 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing Cu/Zn/Al catalysts, to a catalyst produced using this method, as well as to its use in methanol synthesis, methanol reforming and for low-temperature conversion of carbon monoxide. A method is described for preparing Cu/Zn/Al catalysts, involving preparation of a first aqueous solution which contains at least copper formate and zinc formate, preparation of a second solution which contains a precipitation agent, wherein the first and/or second solution contains an aluminium hydroxide sol/gel mixture, combining both solutions, separating the obtained precipitate from the aqueous phase which forms waste water, washing the precipitate until an alkali content, based on a catalyst which calcined at 600°C, of not less than 500 parts per million is attained, and drying. A catalyst prepared using this method is described, and its use in methanol synthesis, methanol reforming and conversion of carbon monoxide.

EFFECT: simpler technology of producing catalyst and increased activity of the catalyst.

32 cl, 5 tbl, 8 ex

FIELD: chemistry.

SUBSTANCE: invention relates to catalyst, suitable to application in reactions of conversion of carbon oxides, in form of granules, formed by pressing reduced and passivated catalyst powder, and claimed powder contains copper in the interval 10-80 wt %, zinc oxide in the interval 20-90 wt %, aluminium oxide in the interval 5-60 wt % and, optionally, one or several oxide promoter compounds, selected from compounds of Mg, Cr, Mn, V, Ti, Zr, Ta, Mo, W, Si and rare-earth elements, in quantity in the interval 0.01-10 wt %. Said granules have average crush strength in horizontal direction after production ≥6.5 kg, ratio of values of average crush strength in horizontal direction after reduction and after production ≥0.5:1 and area of copper surface over 60 m2/g Cu. Invention also relates to method of claimed catalyst production and to method of conversion of carbon oxides in presence of claimed catalyst.

EFFECT: catalyst has high strength of granules and high activity as a result of increased area of copper surface, which makes it possible to apply reactors of smaller size and increase process productivity.

15 cl, 9 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a methanol synthesis method, which includes the following steps: (i) conducting a reaction, in a reaction loop, of a process gas containing hydrogen, carbon dioxide and carbon monoxide over a catalyst to obtain a product gas, (ii) condensing methanol, water and secondary oxygenates from the product gas, (iii) returning unreacted gases into the reaction loop, where the catalyst includes pellets obtained by pressing from a reclaimed and passivated powdered catalyst, where said powder contains copper in the range of 15-70 wt %, zinc oxide, wherein the weight ratio Cu:Zn with respect to the oxide is in the range of 2:1 to 3.5:1, aluminium oxide in the range of 5-60 wt %, and optionally one or more oxide promoting compounds selected from Mg, Cr, Mn, V, Ti, Zr, Ta, Mo, W, Si and rare-earth elements, in the range of 0.01-10 wt %, wherein the catalyst is obtained by carrying out steps which include: (i) preparing, in an aqueous medium, a composition containing a homogeneous mixture of separate particles of copper, zinc, aluminium and optionally one or more promoting compounds of metals selected from Mg, Cr, Mn, V, Ti, Zr, Ta, Mo, W, Si and rare-earth elements, (ii) separating and drying the composition to form a catalyst precursor, (iii) exposing the dried catalyst precursor composition to reducing conditions so that copper compounds contained therein are reduced to copper, (iv) passivating the surface of the reduced copper, and (v) forming a reduced and passivated composition, where, before reducing the copper compounds, the homogeneous mixture is treated at the drying step at temperature in the range of 180-240°C.

EFFECT: when carrying out the disclosed method, total content of secondary oxygenates in the condensate is not more than 500 ppm.

12 cl, 7 tbl, 5 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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