UA65856C2 - Method for hydrogen and methanol obtaining - Google Patents

Abstract

The invention relates to methods for obtaining of technical hydrogen and methanol from synthesis-gas. The method for processing of synthesis-gas, which contains carbon oxides and hydrogen, comprises methanol synthesis. For methanol synthesis the synthesis-gas is used in quantity from 43 to 100 % of total flow at volume ratio of H2-CO2/CO+CO2, equal to 2.03-5.4, which is supplied to reactor system,comprising of flow reactor or cascade of flow reactors and/or reactor with gas mixture recycle. Hydrogen is obtained from non-reacted gas or from non-reacted gas mixture and synthesis-gas after purification from impurities. The use of this invention allows more efficient use of raw materials, increase the level of conversion of carbon oxides, due to which their atmospheric emission is reduced and thus ecological indices are improved.

Description

The invention relates to a method of obtaining technical hydrogen and methanol from converted gas, which contains carbon monoxide, carbon dioxide and hydrogen.

There is a known method of obtaining hydrogen from synthesis gas by converting methanol with water vapor and subsequent purification from carbon dioxide (US patent Me4869894, MKV СО181/13, dated 04.15.87, op. 09.26.89).

The process follows the following reactions: synthesis gas preparation process:

SnangOo:CoOzZNg-206 4kKJ/mol (1); carbon monoxide conversion process:

СбОовнгОо-СОооН2чаА1 OkJ/mol (2).

The disadvantage of this method is that in the process of obtaining hydrogen, almost all the carbon of the synthesis gas is lost during the washing of carbon dioxide with monoethanolamine or potash from the gas mixture.

The closest in terms of technical essence is the method of obtaining hydrogen and methanol from synthesis gas, which contains mainly carbon monoxide and hydrogen, and includes the conversion of carbon monoxide, the subsequent washing of carbon dioxide and the synthesis of methanol, which is carried out before the conversion of carbon monoxide. For methanol synthesis, recirculation gas is used next to fresh syngas, and the amount of recirculation gas does not exceed double the amount of fresh syngas. The molar ratio of hydrogen to carbon monoxide in the gas entering the synthesis is 0.8:1-1.5:1 (patent FRG Mo2904008, MKV СО1 v - 3. 02.02.79, op. 07.08.8O0, prototype).

The disadvantage of the known method is that the composition of the gas is much lower than stoichiometric; with this ratio of reacting components, the synthesis of methanol is characterized by a low speed and is accompanied by the occurrence of a large number of side reactions. Such a significant deviation of the ratio of reacting components from stoichiometry leads to a decrease in the degree of conversion of carbon oxides into methanol due to a lack of hydrogen in the source gas, and residual carbon dioxide is blown out of the system.

However, as the authors themselves note, preference is given to recycling in order to obtain the required synthesis gas composition. For this purpose, the possibility of varying the composition of the gas for the synthesis of methanol is provided, which is achieved by returning part of the product flow, which contains hydrogen, from different points of the process: after the carbon monoxide conversion stage or carbon dioxide purification, while using a compressor to equalize pressure losses in the system.

Thus, the second disadvantage of this method includes additional energy costs for compressing the flow to eliminate pressure losses inside the installation, for recirculation of the unconverted gas mixture, and the fact that the return of part of the product hydrogen leads to product loss.

The basis of the invention is the task of improving the method of obtaining hydrogen and methanol, in which, thanks to the process of obtaining methanol at a volume ratio (He-COg/СОсСо"), the so-called functional, which is equal to 2.03-5.4, and a certain organization of the technological scheme, achieve the maximum production of carbon oxides in the methanol synthesis department, and hydrogen is obtained from the unreacted gas after purification.

The problem is solved by the fact that in the method of obtaining hydrogen and methanol from converted gas, which contains carbon oxides and hydrogen, and includes the synthesis of methanol, according to the invention, converted gas with the functionality Н2е-СО2/СбО--С0О is used for the synthesis of methanol. which is equal to 2.03-5.4, which is fed into the reactor system, which consists of a flow reactor or a cascade of flow reactors and/or a reactor with a gas mixture recycle, and hydrogen is obtained from the unreacted gas after purification.

For the synthesis of methanol, a part of the converted gas is taken, and the unreacted gas is directed to the conversion of carbon monoxide, purification from carbon dioxide and production of hydrogen.

To obtain methanol, carbon dioxide released at the stage of cleaning the converted gas is dosed into the converted gas, which is fed to the synthesis.

Part of the unreacted gas is used as hydrogen-containing gas before desulfurization of the synthesis gas that enters the conversion.

A distinctive feature of the method of obtaining hydrogen and methanol is carrying out the process of methanol synthesis at a functionalization equal to 2.03-5.4, when all the converted gas is fed into the reactor system, which consists of a flow reactor or a cascade of flow reactors and/or a reactor with gas recirculation mixtures and at the same time obtain the maximum activation of the amount of carbon oxides. The degree of transformation of carbon oxides reaches at least 9395. The unreacted gas is immediately used as product hydrogen after the synthesis reactor.

At the same time, the technological scheme is simplified by excluding from it the stages of carbon monoxide conversion and carbon dioxide purification, and the emission of carbon oxides into the air in the form of carbon dioxide is completely absent, unlike the prototype, where the emission of carbon dioxide is 420nm3 per 1000nm3 of converted gas.

If only a part of the total converted gas flow is taken for the synthesis of methanol, then the second part of this flow along the hydrogen thread is directed to the conversion of carbon monoxide, while the purge gases of methanol synthesis are returned to the reactor of low-temperature conversion of carbon monoxide and are used in full for the formation of hydrogen, the combined flow after conversion of carbon monoxide is submitted to absorption purification from carbon dioxide and product hydrogen is obtained.

By returning carbon dioxide after the stage of absorption purification to the flow of fresh gas supplied to the methanol synthesis reactor, the functionality of the synthesis gas is brought to the stoichiometric - 2.03. At the same time, methanol productivity significantly increases, and carbon dioxide output decreases by 3.5 times compared to the prototype.

In addition, the unreacted gas is used as hydrogen-containing gas in the desulfurization stage of the natural gas entering the conversion, which also allows for maximum utilization of the off-gases.

Research has established that the advantages of joint production flow from the chemistry of interdependent reactions that describe the processes of obtaining hydrogen and methanol.

As mentioned above, technically pure hydrogen is obtained in the process of steam reforming of methane and other hydrocarbons with the subsequent conversion of carbon monoxide with water according to reactions (1), (2) and removal of carbon dioxide into the air from the gas mixture with solutions of potash and monoethanolamine.

In the joint production of hydrogen and methanol, carbon oxides are used as raw materials for the production of methanol in accordance with the following reactions:

СОзгЗнА:сСНзОнН-Нг2Оз49.53KJ/mol (3); bOoz2Nha-CHzOonNoO, 73 KJ/mol (4).

Thus, the carbon of natural gas is not emitted into the air, but is used to obtain a scarce and precious product - methanol, which increases the profitability of the entire production as a whole. In addition, in the process of methanol synthesis, product hydrogen is purified from carbon oxides.

For the initial converted gas, the limit of the volume ratio of H2g-COg/СОксСо», the so-called functional, is proposed, from 2.03 to 5.4. This limit is chosen based on the following considerations. A decrease in the functional below 2.03, that is, below the stoichiometric, leads to a decrease in the production of product hydrogen, as well as to a decrease in the degree of conversion of carbon oxides into methanol, and, therefore, to a deterioration in the purification of hydrogen, which is given to the consumer, from carbon oxides, which leads to additional costs to ensure the required level of cleaning.

In addition, if the functionality in the converted gas is below stoichiometric, methanol synthesis is characterized by a low speed and is accompanied by the passage of a large number of side reactions, which deteriorates the quality of raw methanol. The upper limit of the H2-СО2/СбОСО" volume ratio, which is equal to 5.4, is determined by the fact that with a higher value of the functional, due to the lack of carbon oxides in the synthesis gas, the specific productivity of the methanol catalyst decreases, which leads to an increase in the dimensions of the department's equipment synthesis of methanol.

The proposed method of obtaining hydrogen and methanol is explained by the diagram shown in the figure, where 1 is the conversion department; 2 - recovery boiler;

C - recovery heat exchanger; 4 - condensation and separation equipment; - compressor; 6 - department of methanol synthesis; 7 - methanol extraction system; 8 - thin cleaning of outgoing gas; 9 - high-temperature conversion of carbon monoxide; - low-temperature conversion of carbon monoxide; 11 - cleaning from carbon dioxide; 12 - gas desulfurization. a, b, c, d, e, i - gas flows.

The proposed method is carried out as follows. The converted gas from the conversion department 1, obtained by steam or two-stage conversion of natural gas (the latter is a combination of steam and vapor oxygen conversion), enters the recovery boiler 2, in which energy steam is obtained due to the cooling of the converted gas. After the boiler-utilizer, the converted gas, which is sent to the synthesis of methanol, enters the recovery heat exchanger C, passes through the heat utilization system, condensation and separation equipment 4 and, after separating the gas condensate, enters the suction of the compressor 5. Then the converted gas enters the methanol synthesis department 6. The reactor system of the methanol synthesis stage is a flow reactor or a cascade of flow reactors and/or a reactor with gas mixture recycling. In this case, the gas flow (flow a), which comes out of the methanol extraction system 7, is sent to fine purification 8, without using high-temperature, low-temperature conversion of carbon monoxide and purification from carbon monoxide. Part of the purge gases is advantageously supplied as gas containing hydrogen to the desulfurization unit 12, thereby saving product hydrogen. If methanol is obtained in a reactor with a recycle, then to obtain hydrogen, the purge gases of the methanol synthesis cycle (stream B) are used, which are sent to fine purification 8, without the use of high-temperature 9 and low-temperature conversion of carbon monoxide 10 and purification from carbon dioxide 11, and circulation gas (stream c or a) is returned to the methanol synthesis department 6 for mixing with fresh gas using a circulation compressor. Part of the purge gases is supplied to the desulfurization department 12.

In the case when it is necessary to change the ratio of plant capacities in the direction of increasing hydrogen capacities, the process is carried out as follows. After the conversion of natural gas 1, only a part of the converted gas is taken at the exit from the waste boiler 2 to the methanol synthesis unit 6, and the rest of the converted gas is sent along a hydrogen thread to the stage of high-temperature conversion of carbon monoxide. Blowing gases (stream e) are returned to the hydrogen thread, part of this stream after heating to a temperature of 220-2507"С0 in the recuperation heat exchanger C (its stream is returned to the low-temperature conversion of carbon monoxide 10 with subsequent cleaning of the combined stream from carbon dioxide in 11. Part of the purge gases (flow d) is fed to the desulfurization department 12.

The proposed method allows you to vary the composition of the synthesis gas, supplying part of the carbon dioxide after 11 to the suction of the compressor 5, while reducing the emission of carbon dioxide into the air. At the same time, the degree of use of the carbon component of natural gas increases accordingly.

The following examples are proof of the implementation of the proposed method.

Example 1 (comparative).

The installation for obtaining gas, which is used for the synthesis of hydrogen and methanol, is supplied with 3,000 Okg of heavy oil fraction, which is mixed with oxygen obtained at the air distribution installation, then by the method of partial oxidation, synthesis gas with a functionality of 0.85 is obtained. Synthesis-az is fed to a desulphurization plant for purification from compounds that contain sulfur. Purified synthesis gas in the amount of 91,000 m3/h is fed into the flow reactor for a single pass for methanol synthesis.

The synthesis of methanol is carried out in the presence of a copper catalyst at a gas temperature at the inlet of 230"C, at the outlet of 270"C, and the pressure of the synthesis is 10 bar. With a single passage of synthesis gas, 8994 nm/h of crude methanol is obtained as a result of the reaction. The unreacted gas, in the amount of 63846 nm/h, is directed to the conversion of carbon monoxide.

The obtained gas is washed from carbon dioxide and 6176 Onm3Z/ha are obtained. raw hydrogen The test results are shown in the table.

Example 2

Converted gas under a pressure of 2.0-2.5 MPa with a functionality of Н2-СО»/СбОСО» equal to 5.4, obtained at the stage of gas preparation by steam or two-stage steam-oxygen conversion, is fed for cooling to the utilization boiler to obtain energy steam . The temperature of the converted gas after cooling is 360-380"C. After the boiler-utilizer, all the converted gas is sent to the recovery heat exchanger 3, then it is passed through a system that uses the heat of the condensation and separation equipment, separated from the gas condensate and fed to the suction of the compressor. Then the converted gas enters the system from two flow reactors for the synthesis of methanol. The synthesis is carried out under a pressure of 5.0-5.5MPa and a temperature of 200-2607C on a copper-zinc-aluminum catalyst. The unreacted gas, after the separation of methanol, is given to the consumer as product hydrogen If it is necessary to reduce the content of impurities in the product water, condense crude methanol at reduced temperatures, while using recycled water with a lower temperature or another refrigerant. The test results are shown in the table.

Example C

The tests are carried out as in example 2, but for the synthesis of methanol, converted gas with a functional of 2.97 is supplied and the process is carried out in a reactor with a gas mixture recycle. To ensure the desired ratio of capacities for hydrogen and methanol, the consumption of converted gas fed to the synthesis reactor is equal to approximately 43905 of the total flow of converted gas supplied to the plant.

The remainder of the flow (5795), bypassing the synthesis of methanol, is fed to the high-temperature conversion of carbon monoxide.

The unreacted gas from the methanol synthesis unit, heated in the recovery heat exchanger to 2502С, is combined with the stream (5790) selected for the production of hydrogen before the low-temperature conversion of carbon monoxide, after which the gas is submitted to absorption purification from carbon dioxide and obtain product hydrogen.

The test results are shown in the table.

Example 4

The tests are carried out as in example C, but return 90 Onm/h of carbon dioxide after the stage of absorption purification from carbon dioxide into the fresh gas stream, which is fed into the methanol synthesis reactor.

Synthesis gas functionality is brought to the stoichiometric value of 2.03. At the same time, the capacity for methanol increases significantly, and the emission of carbon monoxide and carbon dioxide decreases. The test results are shown in the table.

Example 5

The tests are carried out as in example 2, but the synthesis of methanol is supplied with converted gas with a functional of 2.05, and the synthesis of methanol is carried out in a reactor with a recycle. At the same time, all converted gas supplied to the plant is sent to the methanol synthesis department. The purge gases of the methanol synthesis cycle are directed to fine purification from impurities and receive 10095th hydrogen. The test results are shown in the table.

Example 6

The tests are carried out as in example 2, but for the synthesis of methanol, a converted gas with a functional of 2.43 is supplied, and the synthesis of methanol is carried out sequentially in a flow reactor and in a reactor with a recycle.

At the same time, all converted gas supplied to the plant is sent to the methanol synthesis department. The unreacted gas after the recycle reactor with a hydrogen content of 86.43956 is either given to the consumer as product hydrogen or sent to fine purification from impurities. The test results are shown in the table.

As can be seen from the examples, the operation of the unit on converted gas with a functionality of 2.03-5.4 allows to increase the degree of conversion of the amount of carbon oxides from 18.63905, achieved in the prototype, to 93.68-96.2390 in the proposed method. At the same time, the emission of carbon dioxide into the air is either completely eliminated or significantly reduced: from 420nm3/1000nm3 of converted gas in the prototype to 124nm3/1000nm3 of converted gas in the proposed method. When varying the hydrogen to methanol productivity ratio from 0.578 to 0.010 even under comparative conditions (0.577tNg2/tCH3OH in the prototype and 0.578tNg/tCH3OH in the proposed method), the emission of carbon oxides is 3.4 times less.

Based on the above, it can be concluded that the proposed method of obtaining hydrogen and methanol allows you to flexibly vary the ratio of capacities for hydrogen and methanol, based on the demand situation, to use raw materials more efficiently, to significantly reduce the loss of its carbon component, and to improve the environmental performance of the process by reducing emissions of carbon oxides into the air.

Table

Me Name of units of measurement indicators: Example 1 Example 2 | Example C | Example 4 Example 5 | Example 6 17711127 13 | 4 1 5 1 6 | 7 | 8 | 8

Converted gas for the installation of hydrogen and methanol production: consumption nmU/h 91000 150000 30857 30857 70000 112192

Composition Uvob. 4 No 46.48 84.0 75.94 75.94 67.39 71.73 (;o) 50.99 12.0 10.29 10.29 25.54 20.57

So" 1.63 3.0 11.4 11.4 4.95 6.32

Me 018 0.5 0.37 0.37 1.16 0.48

Ag 0.48 - - - - - sn, 0.24 0.5 2.00 2.00 0.96 0.90

Amount of CO-CO" nmZ/h 47884 22500 6692.88 6692.88 21343 30168 only 0111111 stages (Tysksintez.i | Mpa | - | 80 | 50 | 50 | 53 | 60

Type of reactors Flow | Flowing - - - Flowing - - with recylomi! | with recycling! | with recycling! With the recycling of converted gas for the synthesis of methanol: in the 1st year | in 1 and 1 | flow rate Fo 100 100 43 43 100 100

Dosing CO" from the cleaning department

Consumption nmU/h

Converted gas

SE and lie same | the same | what | same energy consumption nm/h 91000 150000 13250 14150 70000 112192

Composition: Uvob.

No 46.48 84.0 75.94 71.11 67.39 71.73 (;o) 50.99 12.0 10.29 9.64 25.54 20.57 so; 1.63 3.0 11.40 17.03 4.95 6.32

Me 018 0.5 0.37 0.35 1.16 0.48

Ag 0.48 - - - - - sn. 0.24 0.5 2.00 1.87 0.96 0.9 sousoso, | 00006 0vya0lvyi 02oz 0 govo omz n-сОоУСОоСо» 0.85 5.4 2.97 2.03 2.05 2.A3 ol (flow reactors 01101111 flow reactors 2.1.|Volume of the catalyst | m' | - | zanv-48| -:-/( | 9 (| 77777777777717|r;o2by5 mia | thistle 11111111 goth 7 in/out. What; 230/270 230/270

Gas at the exit from

Eszsa MN NSH NOW NOW NOV NO MON consumption nm/h 87805 89730

Composition: СО» Absorption 0.68 7.23

No 90.58 64.00 21. But 2.20 0.67

Me 0.85 0.60 sn, 0.85 113 (;o) 0.35 13.87 snOoNn 4.49 12.50

Crude methanol: nM/h 8994 o 1.4 consumption t/h 15.66 710095 SNZON nmU/h 8920 21077 10579 t/h 12.74 30.11 15.113

The degree is the same | I am | še |.) 31. zv

SOS; in methanol Fo 18.63 93.68 35.06 go 2 51 2 251 5 2 5 52 1 yur 5 "7 | reactor with recycle 2.2.1 Volume of the catalyst | m | (HER 7 //// | 7155 | 7155 | 61 | 61 vysheen 175.11 what | tov so | zok 7773 in/out. What; 210/246 235/2659 240/261 (Svizhiysgaz: expenses | nm'/od | | 77777/7r/ryuryuIYUN|71 13250 | 14150 | 70000 | 77470

Composition: CO» Total 11.40 17.03 7.95 8.23

No 75.94 71.11 67.39 73.27 yes no - - - 0.01

TM 0.37 0.35 1.16 0.69 sn, 2.00 1.87 0.96 127 (;o) 10.29 9.64 25.54 15.77 snOoNn - - - 0.77

Gas at the entrance/exit in| | nmU/h 130000 139423 600000 600000 reactor: expenses Uvob 124485 132154 559535 563915

Composition: CO» 2.08/1.03 7.18/5.84 4.30/4.10 2.62/1.73

Not 85.92/84.15 | 58.68/54.68 | 61.74/58.44 | 84.64/82.59 2.2.4 NO 0.14/1.29 0.21/1.95 0.07/0.60 0.11/11.18

Me 2.12/2.22 7.47/7.90 12.18/13.06 | 2.89/3.08 sn, 7.21/7.53 | 22.70/23.94 | 9.69/10.40 5.08/5.40 (00) 1.90/0.92 2.91/2.05 11.24/8.96 3.93/2.08 snOoNn 0.64/ 2.87 0.84/3.64 0.77/4.44 0.74/3.95 lush 1 0 17 1 6 6 1 o 777 10095 methanol t/h 3.891 5.185 28.847 26.203

Total amount of 777 crude methanol 5,044 7,147 31,684 46,87 100th SNUON 12,74 30,11 3,891 5,185 28,847 41,32

Total degree 7-7 6bo-sSo; into methanol in the Fo synthesis department 18.63 93.68 96.23 95.97 94.61 95.86

Non-synthesis gas of methanol for hydrogen production: consumption nmZ/h 63846 81670 3643 873 5976 17261

Composition": CO; total. 2.28 0.72 1710 6.07 4.22 1.78 2.2.8 No 37.76 96.67 87.49 57.28 61.00 86.32 sho) - 0, 05 020 0.23 0.08 013

Me 0.24 0.51 2.710 8.28 13.63 321 sm, 0.34 0.89 7.40 25.06 10.85 5.64 (;о) 58.43 0.87 1.00 2, 15 9.35 217 veneer 0.25 0.39 0.71 0.94 0.87 0.73

Ag 0.69

With |Vodnevanita./// | Eat! HER HER HER HER

ZlL|ConvervyaSO. WITH! 7777 ГГ Г111111171С1111171Г1111г111111ег

Selection of the initial con. gas for oxide conversion 3.1.4! carbon for the synthesis of 777 methanol: costs

Water code 17607 17607 wet 33109 33109

ZlYatisk 7 | Mpa | 7 |! | 215 | 24

Temperature at the inlet/outlet in stages: 3.1.3) high-temperature CO conversion 345/390 345/390 low-temperature CO conversion 208/224 220/233

Return of gas from the synthesis department to CO conversion after selection for desulfurization: consumption nm/h 63846 3178 573

Composition: СО» bob. 2.28 110 6.07 3.1.2 n. 37.76 87.49 57.28 sho) - 020 0.23

Me 0.24 2.710 8.28

Ag 0.69 - - sn, 0.34 7.40 25.06 (;o) 58.43 1.00 2.15 snOoNn - 0.71 0.94

Gas at the exit from the carbon monoxide conversion department after separation of gas condensate: consumption nmMU/h 100651 22342 19720

Composition: СО» bob. 38.02 17.08 18.97 3.1.3) No 60.52 79.59 77.74 but - - -

Me 0.15 0.71 0.76

Ag 0.43 - - sn, 0.21 2.46 2.38 (0:06) 0.45 0.16 0.15 snOHn - - -

EVA NIMY PON KON HORSE OF LOVE KN KI carbon 3.3|Removal of CO»| Adsorption! - |AdsorptionAdsorption! /-/-- | 7 nielod | zvo 0000000 zmo 111 77 | released into the air nm3/h 38260 3816 3740 o (vddvshyu 00101001 from impurities 4.1 | Type of fine purification Separation of KCA

WINNY THEM ARE NOW AVAILABLE ON NBN raw material with us

IN PO PO PO Best NOV MON

Product hydrogen after purification: consumption nmU/h 61760 81238 18526 15980 3280 17261

Composition: SOz oo ob. 50 rrm 0.70 sl. sl. 1.78

No 97.06 97.08 95.5 95.10 100 86.32 with No - - - - 013

Me 0.25 0.91 0.9 0.91 321 sn, 0.34 0.89 3.4 3.82 5.64 (0:06) 0.74 0.37 02 0.91 2.17 snOoNn - 0.06 0.73

Ag 0.70

Output convertible gas: 6.1 | total number of nmU/h 91000 150000 30857 30857 70000 112192

Functional НосОУСОСо» 0.85 5.4 2.97 2.03 2.05 2.A3 7 |hydrogen 7 110090 methanol t/h 12.74 30.11 3.891 5.185 28.847 41.32

Ratio 7 |Mass ti 0.557 0.335 0.578 0.355 0.010 0.097 volumetric nmZ/nmU 6.924 3.854 6.801 4.402 0.162 0.596

Emission of dioxide nm for 6.5 carbon in the air 100 nm" of carbon in the gas con. gas 420 124 121

Baths SHY ny PI nn t t vodevu r t

I and Ж on the sum" and tuvani x ge z, I !

In | paths

SO -7 sho and yar td I and GENES in u» ' | hl NE meudiyul i 2 -- ( - - 0 kN and sec, shi shi and I y

Claims (2)

1. The method of processing synthesis gas containing carbon and hydrogen oxides and includes the synthesis of methanol, which is distinguished by the fact that synthesis gas is used for the synthesis of methanol in an amount from 43 to 100 95 of the entire stream at the volume ratio of H»- СОг/СОжСо", which is equal to 2.03-5.4, which is fed into the reactor system, which consists of a flow reactor or a cascade of flow reactors, and/or a reactor with a gas mixture recycle, and from gas that did not react, or from a mixture of unreacted gas and synthesis gas, after purification from impurities, hydrogen is obtained. 2. The method according to claim 1, which differs in that, in the case when the entire synthesis gas is used for the synthesis of methanol, the commercial product - hydrogen - is obtained from the unreacted gas after fine purification. Q. The method according to claim 1, which differs in that the synthesis gas, which is supplied for the synthesis of methanol, is additionally dosed with carbon dioxide, which is released at the stage of purification of gas that has not reacted.