DE2427330B2 - METHANOL PRODUCTION METHOD - Google Patents

Description

H ₂ - CO ₂
CO + CO ₁

<2

is working.

2. The method according to claim 1, characterized in that one is a gas mixture that also contains unsaturated hydrocarbons in an amount not exceeding 1% by volume, is used.

3. The method according to claim 1 and 2, characterized in that at a ratio of called reactive components of

H ₂ - CO ₂
CO + CO ₂

= 1.0-1.84

is working.

4. The method according to claims 1-3, characterized in that it is carried out at a temperature from 180 to 280 ⁰ C.

5. The method according to claim 1-4, characterized in that at a volume velocity of the gas mixture from 4,000 to 20,000 St! works

6. The method according to claim 1-5, characterized in that at a total content of the gas mixture of nitrogen, argon and methane works up to 50 vol .-%.

7. The method according to claim 1-6, characterized in that one in a closed Cycle works.

The present invention relates to processes for the production of synthetic methanol.

The synthetic methanol is one of the most important organic products, which for the production of Formaldehyde, dimethyl terephthalate, methyl methacrylate, Pentaerythritol, urotropine, synthetic isoprene rubber and others. is used.

In recent years, methanol has been used for the production of acetic acid and the sodium salt of nitrilotriacetic acid.

Work has also commenced on the development of methanol fuel elements and Use of methanol as a fuel.

Various hydrocarbons, gaseous (for example Natural gas), liquid (naphtha, heavy gasoline, etc.) and solid fuel.

The synthesis of methanol is carried out from the gas that is carried out in various Types of reforming processes of hydrocarbons, such as steam, steam carbonic acid, steam oxygen, high temperature reforming, is obtained.

The solid fuel is subjected to gasification with subsequent steam reforming of Carbon oxide.

In addition, exhaust gases from various chemical production processes are used for the production of methanol, containing hydrogen and carbon oxides.

Two main reactions occur in the synthesis of methanol from hydrogen and carbon oxides.

CO + 2H ₂ = CH ₃ OH (1)

CO ₂ + H ₂ = CO + H ₂ O (2)

If one expresses the concentrations of the reacting components by the ratio

H ₂ -CO ₂

CO + CO ₂

off, the latter is 2 or more in all cases.

In the gas mixtures that result from some types of reforming of hydrocarbons, as well as in the exhaust gases of some chemical production processes, the ratio mentioned is the reacting Components less than 2.

To achieve the required ratio (2 and higher) of the reacting components, the reforming gases and the exhaust gases are subjected to an additional one

ίο treatment.

This is how one leads, for example, in high-temperature reforming of natural gas two additional technological stages, the secondary (steam) reforming of Carbon oxide and the subsequent cleaning of the gas

J5 from the excess carbon dioxide, and at that Steam-oxygen reforming of natural gas an additional technological stage, the purification of the gas the excess carbon dioxide.

In the case of the use of exhaust gases from chemical production processes, for example acetylene production, for the production of methanol, additional stages of working up the gas are also carried out for methanol synthesis, the steam or steam-oxygen reforming of the residual hydrocarbons

4> through. In the latter case one purifies to achieve a ratio of

H ₂ - CO ₂
CO + CO ₂ "

the reforming gases from the excess carbon dioxide.

It is a process for the production of methanol are known (FR-PS 20 49 193, and DT-OS 19 30 702) which is that the synthesis atm of methanol at a pressure of 20 to 100, a temperature of 200 to 300 ⁰ C. on a copper-containing catalyst composed of hydrogen and carbon oxides at a ratio

from

H ₂ - CO ₂
CO + CO ₂

> 1

is carried out.

A disadvantage of this process, that the achievement and maintenance of the mentioned ratio of requires reactive components is a complication of the technological scheme of manufacture

of methanol, associated with the need for additional technological operations (stages) for Working up of gas for the synthesis of methanol both in the case of reforming of hydrocarbons as well as the use of exhaust gases from chemical plants, for example Produce acetylene by the method of thermo-oxidative pyrolysis of methane, to carry out.

If exhaust gases are also used for the production of methanol, the unsaturated residual hydrocarbons (Acetylene, ethylene and their derivatives) are used alongside the technological ones Steps that are carried out to achieve the required ratio of reacting components, an additional technological level, namely a complete removal from the whole set of Residual gases of unsaturated hydrocarbons, for example by carrying out the hydrogenation in Presence of various catalysts, e.g. B. of palladium catalyst or catalyst on the Based on iron oxide (FR-PS 12 04 673), which makes the production of methanol more expensive and complicated will.

The purpose of the present invention is to avoid the disadvantages mentioned.

The invention was based on the object, in the process for the production of methanol from carbon oxides and hydrogen, which are contained in the gas mixture in addition to nitrogen, argon, methane, at a temperature of not more than 300 ^c C under a pressure of 20 to 100 atm to change the ratio of the reacting components in the gas mixture in the presence of a copper-containing catalyst in such a way that a simpler technological scheme is created which enables the reforming gases or the exhaust gases of chemical production processes to be used directly (without additional work-up) for the synthesis of methanol.

This object is achieved according to the invention in that the synthesis of methanol at a ratio of the reacting components in the gas mixture

H ₂ - CO ₂

In addition, it is the presence of the reducing medium and that which promotes the hydrogenation Catalyst possible to carry out the synthesis of methanol when using a gas mixture, which unsaturated hydrocarbons (acetylene, ethylene and others) in an amount not more than 1 vol-o / o contains.

The acetylene is among the above

Conditions hydrogenated to ethylene and ethane, sits down

ίο partly with the carbon oxide and methanol, therefore there is no accumulation of free acetylene in the cycle gases.

The ethylene is also partially hydrogenated to ethane, and the content of the cycle gases to unsaturated compounds with double bonds is between 0.1 and 0.3% by volume.

To reduce the rate of formation of

By-products to the synthesis of methanol at a temperature of not advantageously carried out above 300 ° C, preferably at a temperature from 180 to 280 ⁰ C, by.

The content of inert additions (nitrogen, argon, methane) in the circulated The gas mixture is regulated by constantly flushing the circuit and maintained at a level of up to 50% by volume a content of carbon dioxide of 5 to 15 vol .-% and of carbon oxide of 5 to 20 vol .-% upright.

The volume velocity of the gas mixture in the circuit is expediently kept in a range from 4000 to 20,000 St- ¹ .

Thanks to the lowering of the ratio

H ₂ - CO ₂

CO + CO ₂

performed by less than 2. This is achieved in that the equilibrium of the reaction CO ₂ + H ₂ : $ CO + H ₂ O, which largely depends on the temperature of the process and the composition of the gas, when carrying out the synthesis of methanol at a temperature not exceeding 300 ° C is such that the reduction of carbon dioxide can only be carried out by 30 to 60%.

Under these conditions, the carbon dioxide is contained in the contacting gas in amounts that ensure stable operation of the catalytic converter, and the cycle with the purge gases and the in Methanol dissolved gases discharged as a result of an incomplete reduction of carbon dioxide accumulates hydrogen becomes involved in the cycle, and the synthesis of methanol is carried out at a ratio of

preferably carried out at a ratio of 1 to 1.84.

CO + CO ₂

can be used as a starting gas for the synthesis of methanol gas mixtures of various types of reforming and the Exhaust gases from other chemical production processes, for example acetylene production, are used directly will.

The process does not require removal of the residual methane and other residual hydrocarbons (Acetylene, ethylene, etc.) from the exhaust gases, which makes it possible to obtain high quality The technological scheme of gas production for the synthesis of methanol by the product Reduction of the number of stages to simplify its pretreatment or by avoiding it altogether.

so The end product, the methanol, is obtained in high yield by the process according to the invention and high quality.

The proposed procedure is carried out as follows.

The starting gas mixture, obtained for example by steam-oxygen reforming of natural gas, is compressed one with a compressor to the synthesis pressure, after which this the intake pipe of the Circulation compressor supplies and in this with the circulation (unreacted) gas of the synthesis cycle of Methanol mixed. The mixture of the starting gas and the cycle gas is passed by means of the cycle compressor in the inter-tube space of the recuperation heat exchanger, where the gas mixture on the The temperature of the start of the reaction is heated by the heat of the reaction gases. From the heat exchanger the heated gas mixture enters the reactor, where it is placed on a copper-containing catalyst

Pressure of 20 to 100 atm and a temperature of up to 300 ⁰ C, preferably 180 to 280 ⁰ C, comes for the synthesis of methanol. The hot gases, which contain methanol vapors and the unreacted components, emerge from the reactor. Tubular space of the recuperation heat exchanger, where they are cooled down by heating the gas mixture flowing through the twin tube space of the heat exchanger into the reactor.

The final cooling of the gas and the condensation of the methanol vapors occurs in the Condenser cooler, from which the gas-liquid mixture enters the separator. This is where the gas becomes the crude methanol containing up to 10-12% by weight of water is deposited, while the unreacted gases (Cycle gas) enter the intake pipe of the cycle compressor, where it is mixed with the starting gas mixture are mixed, after which the cycle is repeated.

The inert gases (nitrogen, argon, methane) that accumulate in the synthesis cycle are removed from the system blown off and used, for example, as fuel.

The liquid raw methanol is throttled in the methanol collecting tank, from where it is used for rectification got. During the throttling, the gases dissolved therein develop from the methanol, which essentially consist of carbon dioxide.

In the case of using the exhaust gases from acetylene production for the production of methanol, one passes expediently a small part of the gas used for the methanol synthesis, namely 10 to 20%, to the Total amount related to reforming carbon dioxide, after which the reforming gases with the Main stream of raw exhaust gases mixed, compressed to the synthesis pressure and further as described above moves.

This changes the relationship

H ₂ - CO ₂

CO + CO ₂

in the gas mixture which occurs for the synthesis of methanol, that is, it remains less than 2, while the ratio of H ₂ to CO increases, whereby the conditions for carrying out the synthesis of methanol are improved.

For a better understanding of the present invention, specific examples are given which represent the essence of the Illustrate the invention, but other variants of the embodiment are not excluded will.

In all of the examples below, a starting gas mixture is used for the synthesis of methanol (Fresh gas) in which the ratio of the reacting components

H ₂ - CO ₂ CO + CO ₂

<2

and the ratio of H ₂ to CO> 2.

example 1

The synthesis of methanol was carried out on a copper-containing catalyst with a volume of 1.7 m ³ . The pressure in the synthesis reactor was 50 atm, the temperature 230 to 285 ° C, the volume velocity of the gas 10,000 St- '.

The cycle gas at the inlet to the reactor had the composition 10.0% by volume CO ₂ , 19.3% by volume CO, 56.4% by volume H ₂ , 1.8% by volume CH ₄ , 12.5 Vol-% N ₂ + Ar a ratio of

H ₂
CO

= 2.92 and

H ₂ - CO ₂ CO + CO ₂

= 1.58

The efficiency of the catalyst was 8.14 ι ίο methanol / m ^{3 of} catalyst per 24 hours. The water content of the crude methanol was 12% by weight, the methanol content of the organic part of the crude product was 99.614% by weight, 0.076% by weight of dimethyl ether, 0.058% by weight of n-propanol, 0.029% of isobutanol of isobutanol Wt%. The rest was made up of additions such as aldehydes, ketones and others up to 100%.

Example 2

The synthesis of methanol was carried out under the 2 conditions of Example 1, but at a temperature of 219 to 258 ° C., a gas volume velocity of 14,365 hours, a composition of the cycle gas of 9.2% by volume of CO ₂ , 11.05% by volume CO, 31.05% by volume H ₂ , 5.4% by volume CH ₄ , 43.3% by volume N ₂ + Ar, at a ratio of

Jk.

CO

= 2.81 and

H ₂ - CO ₂ CO + CO ₂

= 1.08

su carried out. The efficiency of the catalyst was 7.161 methanol / m ^{3 of} catalyst per 24 hours.

The crude methanol obtained contained 8.1% by weight

Water. The organic part of the crude product contained 99.317% by weight of methanol, 0.294% by weight of dimethyl ether, 0.104 wt% n-propanol, 0.031 wt% isobutanol.

The rest was made up of additions such as aldehydes, ketones and others up to 100%.

Example 3

The synthesis of methanol was carried out under the conditions of Example 1, but at a temperature of 222 to 259 ° C., a volume velocity of the gas of ^{12,706 St "1} , a composition of the cycle gas of 9.75% by volume of CO ₂ , 10 , 0% by volume CO, 32.5% by volume H ₂ , 4.35% by volume CH ₄ , 43.40% by volume N ₂ + Ar, at a ratio of

Jk co

= 3.25 and

H ₂ - CO ₂
CO + CO ₂

= 1.15

carried out. The capacity of the catalyst was 8.03 t of methanol / m ^{3 of} catalyst per 24 hours.

The crude methanol obtained contained 9.2% by weight of water. The organic part of the crude product contained 99.41% by weight of methanol, 0.234% by weight of dimethyl ether, 0.078% by weight of n-propanol, 0.020% by weight of isobutanol. The rest was made up of additions such as aldehydes,

bo ketones and others up to 100%.

Example 4

The synthesis of methanol was carried out under the conditions of Example 1, but at a temperature of 222 to 260 ° C, a volume velocity of the gas of 9760 St- ', a composition of the cycle gas of 10.25 vol .-% CO ₂ , 11, 5% by volume CO. 33.5% v / v H ₂ , 3.75% v / v CH ₄ , 41.0

Vol .-% N ₂ + Ar, at a ratio of

H ₂
CO

= 2.91 and

H ₂ - CO ₂
CO + CO ₂

= 1.06

carried out. The capacity of the catalyst was 8.04 t of methanol / m ^{J of} catalyst per 24 hours.

The crude methanol obtained contained 8.9% by weight of water. The organic part of the crude methanol contained 99.46% by weight of methanol, 0.183% by weight of dimethyl ether, 0.086% by weight of n-propanol, 0.023% by weight of isobutanol. The rest was made up of additions such as aldehydes, ketones and others up to 100%.

Example 5

The synthesis of methanol was carried out under the conditions of Example 1, but at a temperature of 185 to 256 ° C, a volume velocity of the gas of 11,918 St- ', a composition of the cycle gas of 13.8 vol .-% CO2, 13, 2 vol.-o / o CO, 32.5 vol.-o / o H ₂ , 5.1 vol .-% CH ₄ , 35.4 vol .-% N ₂ + Ar, at a ratio of

H ₂
CO

= 2.46 and

H ₂ - CO ₂
CO + CO ₂

= 0.69

carried out. The efficiency of the catalyst was 7.91 methanol / m ^{3 of} catalyst per 24 hours.

The crude methanol obtained contained 9.9% by weight of water. The organic part of the crude methanol contained 99.469 wt% methanol, 0.17! % By weight dimethyl ether, 0.091% by weight n-propanol, 0.024% by weight isobutanol. The rest was made up of additions such as aldehydes, ketones and others up to 100%.

Example 6

The synthesis of methanol was carried out under the conditions of Example 1, but at a temperature of 200 to 260 ° C, a volume of the catalyst of 1.51, a pressure of 50 atm, a volume velocity of the gas of 15 680 St- ', one Composition of the cycle gas of 9.15% by volume CO ₂ , 15.66% by volume CO, 47.73% by volume H ₂ , 14.4% by volume CH4, 13.1% by volume N ₂ + Ar, 0.02% by volume C ₂ H ₅ , at a ratio of

Jk

CO

= 3.04 and

H ₂ - CO ₂
CO + CO,

= 1.55

carried out.

The efficiency of the catalyst was 12.98 g of methanol / cm ^{3 of} catalyst per 24 hours. The water content of the crude methanol was 10.1% by weight. The organic part of the crude methanol contained 99.341% by weight of methanol, 0.1493% by weight of diethyl ether, 0.1800% by weight of n-propanol, and 0.0637% by weight of isobutanol. The rest was made up of additions such as aldehydes, ketones and others up to 100%.

Example 7

The synthesis of methanol was carried out under the conditions of Example 1, but at a temperature of 224 to 260 ° C, a volume velocity of the gas of 8480St ¹ , a composition of the circulation gas of 7.5 vol .-% CO ₂ , 18.0 vol % CO, 54.5% by volume H ₂ , 11.2% by volume CH ₄ , 8.3% by volume

N ₂ + Ar, 0.0% by volume of C ₂ H ₂ , 0.5% by volume of C ₂ H ₄ , 0.0% by volume of o / o O2, at a ratio of

H ₂
CO

= 3.03 and

H ₂ - CO ₂
CO + CO ₂

- ■ = 1.82

carried out.

The capacity of the catalyst was 7.54 t of methanol / m ^{3 of} catalyst per 24 hours.

The crude methanol contained 8.5% by weight of water. Of the The organic part of the raw methanol contained 99.27% by weight of methanol, 0.1419% by weight of dimethyl ether, 0.0870 wt% n-propanol, 0.0365 wt% isobutanol. The rest was made up of additions such as aldehydes, Ketones and others up to 100%.

Example 8

The synthesis of methanol was carried out on a copper-containing catalyst at a volume of the catalyst of 1.51, a pressure of 50 atm, a temperature of 220 to 265 ⁰ C, a volume velocity of the gas of 10,000 St- ', a composition of the cycle gas of 7.73% by volume CO ₂ , 0.01% by volume C ₂ H ₂ , 0.02% by volume C ₂ H ₄ , 0.02% by volume O ₂ , 21.5% by volume % CO, 51.72% by volume H ₂ , 19.00% by volume CH ₄ + N ₂ + Ar, at a ratio of

H ₂
CO

= 2.41 and

H ₂ - CO ₂
CO + CO ₂

= 1.5

carried out.

The efficiency of the catalyst was

j5 9.5 t methanol / m ³ catalyst per 24 hours. The water content of the crude methanol was 10.91% by weight. The organic part of the crude methanol contained 99.45% by weight of methanol, 0.1061% by weight of dimethyl ether, 0.010% by weight of methyl formate, 0.2430% by weight of n-propanol, 0.054% by weight of isobutanol . The rest was made up of additions such as aldehydes, ketones and others.

Example 9

The synthesis of methanol was carried out on a copper-containing catalyst, a volume of the catalyst of 1.51, a pressure of 50 atm, a temperature of 220-275 ° C, a volume velocity of the gas of 9000St " ¹ , a composition of the cycle gas of 10 , 0% by volume of CO ₂ , 0.1% by volume of C ₂ H ₂ , 0.1% by volume of ethylene, 0.1% by volume of O ₂ , 19.62% by volume of CO, 40 , 52% by volume H ₂ , 29.21% by volume CH ₄ + N ₂ + Ar, at a ratio of

CO

_{= 2} , 06 and

CO + CO ₂

carried out.

The efficiency of the catalyst was 6.51 methanol / m ^{3 of} catalyst per 24 hours. The water content of the crude methanol was 11.68% by weight. The organic part of the crude ethanol contained 98.89% by weight of methanol, 0.313% by weight

b5 dimethyl ether, 0.144% by weight methyl formate, 0.335 % By weight n-propanol, 0.090% by weight isobutanol. The remainder were made up of additives such as aldehydes, ketones and other.

Example 10

The synthesis of methanol was atm on a copper-containing catalyst at a volume of catalyst of 1.5 1, a pressure of 50, a temperature of 220 to 280 ⁰ C, a Volumgeschwindigkeit of the gas 10 000 St ^{"1 was} carried out. This had the Recycle gas with a composition of 13.82% by volume CO ₂ , 12.68% by volume CO, 29.61% by volume H ₂ , 0.1% by volume C ₂ H ₂ , 0.4% by volume .-o / o C ₂ H ₄ , 0.1% by volume O ₂ , 43.29 _{% by volume, CH 4} + N ₂ + are in the ratio of

H ₂
CO

= 2.33 and

H ₂ - CO ₂
CO + CO ₂

= 0.59

The capacity of the catalyst was 5.1 t of methanol / m ^{3 of} catalyst per 24 hours, the water content of the crude methanol was 10.9% by weight, the methanol content of the organic part of the raw methanol was 98.99% by weight, 0.337% by weight of dimethyl ether, 0.08% by weight of methyl formate, and n-propano! 0.296% by weight, of isobutanol 0.014% by weight, of aldehydes, ketones and the rest.

Example 11

The synthesis of methanol was carried out on a copper-containing catalyst at a volume of the catalyst of 1.7 m ³ , a pressure of 45 atm, a temperature of 225 to 275 ° C, a volume velocity of the gas of 9000 St- '. The recycle gas had a composition of 9.1% by volume of CO ₂ , 16.7% by volume of CO, 38.45% by volume of H ₂ , and 0.25 _{% by volume of C 2} H ₂ , 0.4% by volume C ₂ H ₄ , 0.1% by volume O ₂ , 35% by volume CH ₄ + N ₂ + are in the ratio of

H ₂
CO

= 2.24 and

H,

CO ₂

CO + CO-

- = 1.13

Content of the organic part of the crude methanol in methanol 98.5 wt .-%, in dimethyl ether 0.238 % By weight, 0.181% by weight of methyl formate, 0.385% by weight of n-propanol, 0.399% by weight of isobutanol Aldehydes, ketones and others. m. rest.

Example 13

The synthesis of methanol was carried out on a copper-containing catalyst at a volume of

lu catalyst of 20cm ^J, a pressure of 100 atm, a temperature of 280 ⁰ C, a Volumgeschwindigkeit the gas from 18742 St ^"1 carried out. In this case, the recycle gas of a composition of 8.50 exhibited by volume o / o CO ₂ , 16.80% by volume CO, 44.4% by volume H ₂ , 0.1% by volume C ₂ H ₂ , 0.1% by volume C ₂ H ₄ , 0.1% by volume ° / o O ₂ , 30% by volume CH ₄ + N ₂ + Ar a ratio of

Jk co

= 2.6 and

H ₂ - CO ₂
CO + CO ₂

= 1.46

20 on.

The efficiency of the catalyst was 14.8 g of methanol / cm ^{3 of} catalyst per 24 hours, the water content of the crude methanol was 15.3% by weight, the methanol content of the organic part of the crude methanol was 98.3% by weight. o, 0.285% by weight of dimethyl ether, 0.213% by weight of methyl formate, 0.391% by weight of n-propanol, 0.385% by weight of isobutanol, aldehydes, ketones and the rest up to 100%.

Example 14

The synthesis of methanol was applied to a copper-containing catalyst at a volume of catalyst of 1.7 m ^3, a pressure of 50 atm, a temperature J5 220-270 ⁰ C, a Volumgeschwindigkeit of the gas of 15, 000 St 'performed. The recycle gas had a composition of 9.1% by volume CO ₂ , 10.75% by volume CO, 30.85% by volume H ₂ , 49.30% by volume CH ₄ + N ₂ + Are in ratio of

JO

40

The efficiency of the catalyst was 7.14 t of methanol / m ^{3 of} catalyst per 24 hours, the water content of the crude methanol was 10.1% by weight, and the organic part of the crude methanol was 4-5. Methanol 99.0% by weight, of dimethyl ether 0.205% by weight, of methyl formate 0.155% by weight, of n-propanol 0.243% by weight, of isobutanol 0.235% by weight, of aldehydes, ketones and the rest.

H ₂
CO

= 2.87 and

H ₂ - CO ₂
CO + CO ₂

= 1.09

Example 12

The synthesis of methanol was applied to a copper-containing catalyst at a volume of catalyst of 1.7 m ^3, a pressure of 40 atm, a temperature of 220 to 28O ⁰ C ₁ a Volumgeschwindigkeit the gas from 6000St- 'performed. The recycle gas had a composition of 11% by volume of CO ₂ , 15.5% by volume of CO, 35.18% by volume of H ₂ , 0.1% by volume of C ₂ H ₂ , 0.2 Vol.-o / o C ₂ H ₄ , 0.02% by volume O ₂ , 38% by volume CH ₄ + N ₂ + are in a ratio of

H ₂
CO

= 2.27 and

H,

CO ₂

CO + CO ₂

= 0.91

The efficiency of the catalyst was 7.09 t of methanol / m ^{3 of} catalyst per 24 hours, the water content of the crude methanol was 8.3% by weight, and the methanol content of the organic part of the crude methanol was 99.35% by weight. -%, of dimethyl ether 0.285% by weight, of n-propanol 0.110% by weight, of isobutanol 0.051% by weight, of aldehydes, ketones and the rest up to 100%.

Example 15

^r

The synthesis of methanol was atm on a copper-containing catalyst at a volume of catalyst of 20 cm ^3, a pressure of 80, a temperature of 270 ⁰ C, a Volumgeschwindigkeit the gas from 18500 St. performed '. The circulating gas had a composition of 8.7 vol. O / o CO ₂ , 17.3 vol. O / o CO, 43.1 vol.% H ₂ , 32.9 vol. O / oCH ₄ + N ₂ + Arein ratio of

on. b5

The performance of the catalyst at this time was 5.01 t methanol / m ³ of catalyst per 24 hours, the content of the crude methanol to water 9.8 wt .-%, the H _{2 au} f

- = 2.49 and
CO

H ₂ - CO ₂
CO + CO ₂

= 1.43

The efficiency of the catalyst was 12.6 g of methanol / cm ^{3 of} catalyst per 24 hours, the content of water in the crude methanol was 12.1% by weight, the content of methanol in the organic part of the raw maltanose was 99.0% by weight, of dimethyl ether 0.205% by weight, of methyl formate 0.191% by weight, of n-propanol 0.095% by weight, of isobutanol 0.135% by weight, of aldehydes, ketones, etc., the remainder up to 100%.

Claims (1)

Patent claims: 1. Process for the production of methanol from carbon oxides and hydrogen, which are in the gas mixture in addition to nitrogen, argon and methane are included, at a temperature not exceeding 300 ° C and a pressure of 20 to 100 atm in the presence of a copper-containing catalyst, characterized in that that at a ratio of the reacting components in said gas mixture of