WO2008100170A1 - Methanol producing method and a plant for carrying out said method - Google Patents

Abstract

The invention relates to organic chemistry, in particular to a method for producing ethanol by oxidising a hydrocarbon-containing gas and to a plant for the production thereof. The inventive method is characterised in that it consists in forming a reaction mixture in the reactor module (1) of a cooling area (4-1, 4-2) by continuously supplying a coolant in the direction of the reaction mixture flow after exit thereof from a mixing area (3-1, 3-2), wherein the coolant flow is formed in such a way that it is provided with a space for placing at least one part of a reaction area (5-1, 5-2) therein and the temperature of the reaction mixture inside the coolant flow is maintained within a range of 520-600°C in said part of the reaction area (5-1, 5-2), thereby making it possible to increase the yield of a target product and to reduce the formation of by-products. The cooling area (4-1, 4-2) is embodied in such a way that it makes it possible to modify the coolant flow-rate for providing the required temperature of the reaction mixture inside the coolant flow.

Description

 METHOD OF METHANOL PRODUCTION AND INSTALLATION FOR ITS

IMPLEMENTATION

Technical field

The invention relates to the field of organic chemistry, and in particular to a technology for producing methanol by direct oxidation of a hydrocarbon-containing gas - natural, associated gas, oil refining production, and can be used in the chemical, petrochemical, oil and gas industries.

State of the art

The resources of hydrocarbon-containing gases, which are environmentally friendly fuel and valuable chemical raw materials, are large, however, transportation of raw materials in a gaseous state and the direct use of such gases in the form of gaseous energy carriers in many cases, in particular for vehicles, is uneconomical. More technologically advanced is the use of liquid hydrocarbon products, in particular methanol, as a universal fuel and the initial product of many chemical industries. In addition, oil and gas producers themselves need large volumes of methanol to be used as a means of preventing the formation of hydrates in gaseous media during the extraction and transportation of hydrocarbon gases.

Various methods are known for producing methanol from hydrocarbon-containing gases.

The industry widely uses steam and steam-oxygen conversion of methane to synthesis gas (a mixture of CO and H ₂ ) with its subsequent catalytic conversion to methanol, but these processes require sophisticated technological equipment, have high requirements for the purity of the source gas, and require large amounts of energy to produce synthesis gas and its purification, contain a large number of intermediate stages of the process, which makes it unprofitable for small and medium-sized production with a capacity of less than 2000 tons / day.

At present, direct interest, without obtaining synthesis gas, gas-phase oxidation of methane to methanol at high pressures is of great interest. The process is carried out at pressures up to 10 MPa and initial temperatures of 300-500 ⁰ C in tubular reactors at relatively low initial concentrations of oxygen with subsequent cooling of the gas-liquid mixture and separation of liquid products, from which methanol is isolated by distillation.

A number of known methods for producing methanol based on the direct oxidation of methane.

A known method of producing methanol from methane-containing natural gas (US, 4618732, Bl), comprising mixing natural gas with air or oxygen, supplying these gases to an inert surface reactor and their interaction at elevated pressures of 1-10 MPa, elevated temperatures of 300-400 ⁰ C, with an initial oxygen concentration of 2-20% in the mixture and a reaction time of 2-1000 s in the absence of any additional materials in the reaction zone that significantly affect the selectivity of the reaction or the yield of products, followed by the release of methanol from the reaction gas and directing unreacted methane to a similar process or recycling it to the reactor.

The disadvantage of this method is the need to use inert materials or coatings for the manufacture of the reactor, which, as a rule, have low structural and operational characteristics and are poorly combined with other structural materials of the reactor, which makes it more expensive. Moreover, a long reaction time requires large equipment sizes, which also significantly increases its cost. In addition, with the declared high oxygen concentrations and the absence of measures to remove the heat of reaction, heating the reaction mixture can reach several hundred degrees, which will inevitably lead to a sharp decrease in methanol yield and abundant soot formation.

A known method for the production of methanol (RU, 2200731, Cl; WO 03031380), comprising separately supplying compressed and heated hydrocarbon-containing gas and compressed oxygen-containing gas to the mixing zones of successive reactors, followed by gas-phase oxidation of the hydrocarbon-containing gas in successive reaction zones of reactors at an initial temperature of up to 500 ⁰ C, pressure up to 10 MPa and oxygen content not more than 6 vol. %, cooling the reaction mixture “through the wall” before each subsequent reaction zone, final cooling the reaction mixture before separation after the last reaction zone of the last reactor, separating the cooled reaction gas-liquid mixture into the exhaust gas and liquid products, rectification of liquid products with the release of methanol, the supply of exhaust gases to the original hydrocarbon-containing gas or to combustion, in which the reaction is carried out at a constant temperature with controlled heat removal by cooling the reaction mixture with water condensate through the wall to produce steam. In this case, a decrease in the reaction temperature is achieved through the use of a complex and expensive reactor design combined with a waste heat boiler and connected to a high pressure steam circuit. In addition, with this design of the reactor, processes on the surface of the reactor have a great influence on the process, which even with relatively inert surface material (quartz) lead to the formation of a significant amount of reaction by-products - carbon oxides and water, which significantly reduces the yield of the target product.

The closest technical solution (prototype) is a method for the production of methanol, including the separate supply of sequentially compressed and heated hydrocarbon-containing gas and compressed oxygen-containing gas to the mixing zone of the reactor, subsequent gas-phase oxidation of the hydrocarbon-containing gas at an initial temperature of up to 500 ⁰ C, pressure up to 10 MPa and oxygen content no more than 8 about. % in the reaction zones of up to five reactors in series, with an additional supply of oxygen-containing gas to the subsequent mixing zones of each reactor, cooling the reaction mixture by 70-150 ⁰ C before each subsequent oxidation step and hardening in the last reaction zone by lowering the temperature of the reaction mixture less than 200 ⁰ C for a time of less than 0.1 of its stay in the reaction zone, the separation of methanol from the cooled reaction gas-liquid mixture, the supply of exhaust gases to the end carbon-containing gas or for combustion, the supply of waste liquid oxygen-containing products after separation of methanol into the first mixing zone of the reactor (RU, 2162460, Cl).

This method of methanol production compares favorably with others in the possibility of obtaining a higher degree of methane conversion per pass through the use of several reactors in series, a higher selectivity for methanol formation and the ability to avoid soot formation by cooling the reaction mixture before each subsequent oxidation step. The disadvantage of this method is the complex design of the reactor, including a gas-gas heat exchanger to remove a large amount of heat before each subsequent oxidation stage, which makes the whole process expensive and metal-intensive. The large thermal inertia of the heat exchange equipment makes the process difficult to control. In addition, adverse catalytic reactions occurring on the walls of the reactor and leading to a decrease in the yield of the target product, methanol, as well as to additional heating of the walls of the reactor, have a strong negative effect on the process.

In all of the above methods, due to the high thermal effect of the reaction, the reaction mixture is either heated to temperatures above 600 ⁰ C, which leads to intensive soot formation and a decrease in the yield of the target product as a result of its thermal decomposition in the reactor itself, or heating is limited by a serious complication of the design reactor due to the inclusion of intermediate heat exchangers.

Although the use of built-in heat exchangers (RU, 2200731, Cl) allows a reaction with controlled heat removal and even at a constant temperature, the complexity of the reactor design, as well as the use of built-in heat exchangers with high heat inertia, make it difficult to control the methanol production process.

Disclosure of invention

As it was established by the authors in the course of research, gas-phase oxidation at a constant temperature below 48O ⁰ C, as proposed in some of the above methods, or under conditions not exceeding 480 ⁰ C, the temperature of heating the reaction mixture, significantly increases the reaction time and, accordingly, leads to either to a significant decrease in the productivity of methods for producing methanol, or to the need to increase the size of the reactor.

In this case, there is a threat of incomplete conversion of an oxygen-containing gas in the reactor, which can lead to the formation of an explosive mixture containing oxygen at the outlet.

As was established during the research, the optimal temperature of the gas-phase oxidation process is 520-570 ⁰ C.

It was also found that a significant decrease in methanol yield occurs due to the intense catalytic oxidation of the initial hydrocarbon-containing gas, as well as already formed methanol and other products, on the wall of the reactor with the formation of deep oxidation products - water and carbon dioxide.

At the same time, at high reaction temperatures, the indicated catalytic effect manifests itself not only on the wall surface made, for example, of stainless steel, but also on walls made of relatively inert materials, which are sometimes proposed to be used as a coating of the inner walls of a reactor, for example, quartz ( US 4,618,732, Bl).

The catalytic reaction of deep oxidation, which, in comparison with the gas-phase reaction, forms methanol, has a much greater thermal effect, intense on the walls of the reactor and more intense in the wall layer containing active particles diffusing from the surface of the walls, leads to additional heating of the surface of the reactor and its corrosion, which leads to tightening requirements for the choice of material and leads to a rise in the cost of the reactor.

Therefore, in the production of methanol, to ensure a high methanol yield, not only the gas-phase oxidation reaction in the optimal temperature range is required, but also the minimization of the reaction intensity on the surface of the walls of the reactor and in the wall layer.

The aim of the invention is to simplify the design and reduce the metal consumption of the reactor, reduce corrosion of the inner surface of the walls of the reactor, increase safety and control process, eliminate the formation of by-products and increase the yield of the target product.

When creating the invention, the task was to maintain the temperature of the reaction mixture in the desired temperature range at the desired ratio of hydrocarbon-containing gas and oxidizing agent in the reaction mixture, as well as to reduce the concentration of corrosive substances on the inner surface of the walls of the reactor, to reduce the temperature of the walls of the reactor and the stresses of the reactor material by limiting the supply heat to the reaction mixture during the processes of its oxidation and exclude contact of the hot reaction mixture with the internal the surface of the walls of the reactor.

The problem was solved by creating a method for the production of methanol, which is carried out sequentially: mixing separately supplied starting reagents: sequentially compressed and heated carbohydrate containing gas and compressed oxygen containing gas, gas-phase oxidation of a hydrocarbon-containing gas at elevated temperature and pressure up to 10 MPa and subsequent cooling of the reaction mixture in the formed, respectively, mixing, reaction zone and cooling zone, and then cooled the resulting mixture containing methanol, methanol is separated, and the exhaust gases are sent to the source hydrocarbon-containing gas or for utilization, characterized in that the cooling zone The reaction mixture is formed by supplying refrigerant in the direction of movement of the reaction mixture stream after the reaction mixture leaves the mixing zone, with the formation of a refrigerant stream having a space inside the stream to accommodate at least part of the reaction zone, and in this part of the reaction zone inside the refrigerant stream maintains the temperature of the reaction mixture in the range from 520 to 600 ⁰ C.

Moreover, according to the invention, it is advisable to maintain the temperature of the reaction mixture inside the refrigerant stream, preferably in the range of 520-57O ⁰ C.

In addition, according to the invention, it is advisable to subject the reaction mixture repeatedly to sequentially mixing with separately supplied compressed oxygen-containing gas, to gas-phase oxidation and cooling in repeatedly mixing, reaction and cooling zones, and in this case to supply the original compressed and heated hydrocarbon-containing gas to the first of the mixing zones, and oxygen-containing gas to be supplied to each of the mixing zones

In addition, according to the invention, it is advisable to form a cooling zone by repeatedly supplying refrigerant.

Moreover, according to the invention, a refrigerant selected from the group consisting of: a portion of the original cold hydrocarbon-containing gas is used as a refrigerant; chilled hydrocarbon-containing off-gas; an aqueous solution of organic by-products formed after the separation of methanol; a gas-vapor mixture of an aqueous solution of organic by-products with an initial hydrocarbon-containing gas or with a cooled hydrocarbon-containing exhaust gas. Moreover, according to the invention, it is advisable to provide the temperature of the reaction mixture in the reaction zone by controlling the parameters of the refrigerant flow.

The problem was also solved by creating a plant for the production of methanol from carbohydrate-containing gas, including:

- at least one reactor having a housing in which at least one reaction module is placed, in which are formed in series:

- a mixing zone adapted for mixing the feed products fed to the module and forming a reaction mixture stream;

- a reaction zone for accommodating a stream of a reaction mixture subjected to gas phase oxidation,

- a cooling zone adapted to accommodate at least a portion of the reaction mixture stream within the refrigerant stream in the direction of movement of the reaction mixture stream and configured to vary the flow rate of the refrigerant to ensure the temperature of the reaction mixture is not higher than 600 ⁰ C, and comprising a device for measuring temperature in the reaction zone in the region to the cooling zone and the temperature in the part of the reaction zone located inside the refrigerant stream; a system for preparing a source hydrocarbon-containing gas, providing the possibility of its sequential compression to 1.0-10.0 MPa and heating to 300-5OO ° C, and feeding it into the mixing zone of the reaction module; a system for preparing an oxygen-containing gas, providing the possibility of its compression up to 1.0-10.0 MPa, and feeding it into the mixing zone of the reaction module;

- a system for supplying refrigerant to the cooling zone, comprising a device for supplying the refrigerant in a continuous stream with the formation of a space inside the stream to accommodate at least part of the reaction zone, and configured to control the parameters of the refrigerant stream;

- a system of pipelines and devices providing cooling of reaction products and their separation into components to be separated or disposed of.

Moreover, according to the invention, it is desirable that the refrigerant supply system in the cooling zone contains several devices that provide the supply of refrigerant in a continuous stream with the formation of a space inside the stream to accommodate at least part of the reaction zone, and configured to control the parameters of the refrigerant stream;

In addition, according to the invention, the system for supplying refrigerant to the cooling zone can be equipped with a device for generating a flow of refrigerant in the form of a hollow cylinder.

Moreover, according to the invention, it is advisable that the reactor contains several reaction modules placed sequentially in the vessel one after the other.

Moreover, according to the invention, it is advisable that the installation be adapted for use as a refrigerant part of the original cold hydrocarbon-containing gas or a cooled off-gas hydrocarbon-containing gas or an aqueous solution of organic by-products formed after methanol or vapor-gas mixture of an aqueous solution of organic by-products with the original hydrocarbon-containing gas is isolated or gas-vapor mixture of an aqueous solution of organic by-products with chilled waste levodorodsoderzhaschim gas.

Brief Description of the Drawings

The invention is further explained by the description of examples of the implementation of one of the variants of the method for the production of methanol according to the invention using the installation according to the invention, the scheme of which is shown in the attached drawing Fig.l.

However, the above installation diagram does not limit the options for its implementation and does not limit patent claims.

Best Mode for Carrying Out the Invention

The method for producing methanol according to the invention can be carried out in a plant according to the invention, for example, shown in FIG. 1, comprising a reactor 1 in which two reaction modules 2-1 and 2-2 are placed in series one after another, each of which has mixing zones 3-1 and 3-2, cooling zones 4-1 and 4-2 of the reaction mixture and reaction zones 5-1 and 5-2, respectively, The mixing zone 3-1 is adapted to receive and mix the starting products supplied to the reaction module 2-1: a sequentially compressed and heated hydrocarbon-containing gas and an initial compressed oxygen-containing gas.

The mixing zone 3-2 is adapted to receive and mix the reaction products supplied to the reaction module 2-2 from the reaction module 2-1 and additionally compressed oxygen-containing gas supplied to the reaction module 2-2.

In this case, the compression, heating and supply of hydrocarbon-containing gas can be performed in a system containing, for example, pipelines 6 for supplying gas from a gas source, a compressor 7 for compressing gas, a gas distribution manifold 8, a heat exchanger 9, in which heat leaving the reactor is used for heating 1 oxidation products, and a pipe 10 for supplying a heated hydrocarbon-containing gas to the reactor 1

Compression and supply of oxygen-containing gas can be carried out using a system containing a compressor 11 and pipelines 12-1 and 12-2.

Moreover, according to the invention, the mixing zones 3-1 and 3-2 are also adapted for forming at the outlet of each mixing zone a flow of the reaction mixture having the desired arrangement in the reaction module in the direction of the cooling zone. For example, in the middle of the reaction module, in a single stream spaced from the walls of the module body.

The reaction mixture cooling zones 4-1 and 4-2 are adapted to supply refrigerant to the internal cavity of the module, for example, using a refrigerant refrigerant supply system configured to control refrigerant flow parameters, for example, refrigerant volume and flow rate, and flow configuration.

Moreover, according to the invention, using the refrigerant supply devices 13-1, 13-2 and 13-3, a refrigerant stream can be formed in the form of a hollow cylinder having 5-1 and 5-2 around the reaction mixture in the area of the reaction zone a refrigerant layer sufficient to ensure that the temperature of the reaction mixture in the reaction zone is not higher than 600 ⁰ C.

Moreover, according to the invention, the supply of refrigerant is carried out in the direction of flow of the reaction mixture with the formation of a refrigerant stream having a space inside the stream to accommodate the flow in it the reaction mixture is completely along the entire length of the stream or part thereof. This can be achieved, for example, by performing devices 13-1, 13-2 and 13-3 of the supply of refrigerant, for example, collector type, having slit-like outlet openings located near the inner surface of the reactor vessel 1 or in the plane of the cross section of the vessel at the inlets in zones 4-1 and 4-2 of cooling. The devices 13-1, 13-2 and 13-3 of the refrigerant supply can be made with the possibility of regulating the thickness of the refrigerant layer around the flow of the reaction mixture, for example, by changing the angle of inclination and the orifice of the slits.

In addition, the refrigerant supply devices 13-1 and 13-2 can be configured to provide a refrigerant stream having a space inside to accommodate the entire stream of the reaction mixture or part thereof and having a different thickness of the refrigerant layer, for example, device 13 -1 and 13-2 of the refrigerant supply can be made multi-tiered and multi-level, placed, for example, in various cross sections of the reaction modules 2-1 and 2-2.

As a refrigerant according to the invention, a cold hydrocarbon-containing feed gas or a cooled hydrocarbon-containing exhaust gas or an aqueous solution of organic by-products formed after methanol evolution, or a gas-vapor mixture with a hydrocarbon-containing or cooled hydrocarbon-containing exhaust gas, which can be delivered to devices 13-, can be used. 1, 13-2 and 13-3 of the refrigerant supply to the cooling zones 4-1 and 4-2 can be carried out through pipelines.

In addition, reaction zones 5-1 and 5-2 are equipped with devices 14-1, 14-2 and 14-3 for measuring temperature inside the zones and at the boundaries with cooling zones 4-1 and 4-2.

The methanol production device according to the invention may also contain at least one more heat exchanger 15 for cooling the products leaving the heat exchanger 9 and other devices connected by a piping system to provide cooling and separation of the products into components to be separated or recycled. For example, using a separator 16 - separation of gaseous and liquid products, using a column 17 - separation of methanol in the collector 18 from an aqueous solution of organic by-products sent to the collection tank 20. In addition, gaseous products from the separator 16 using the compressor 19 can be fed into the mixer 22, and water the solution from the collection tank 20 with the help of the pump 21 can also be supplied to the mixer 22, and then the mixture of gaseous products with the aqueous solution can be used as a refrigerant in the cooling zones 4-1 and 4-2.

The following are examples 1 and 2 of a method for producing methanol according to the present invention in plants according to the invention.

Moreover, in examples 1 and 2, the method for producing methanol was carried out in plants according to the invention using one reactor 1, including two cylindrical reactor modules 2-1 and 2-2, in which the mixing zones 3-1 and 3 were respectively formed: -2, cooling zones 4-1 and 4-2 and reaction zones 5-1 and 5-2. Moreover, in the reactor module 2-1:

- the mixing zone 3-1 was made in the form of a multi-flow mixer of the “tube-in-tube” type, and due to intensive turbulization of the incoming flows of the initial gaseous products, their rapid mixing was ensured with the formation of a stream of a homogeneous reaction mixture;

- in the reaction zone 5-1, about 2/3 of the reaction mixture flow along its length was placed before entering the cooling zone 4-1, and the remaining 1/3 of the reaction mixture flow was placed inside the cooling zone 4-1;

- the formation of the cooling zone 4-1 was carried out by supplying a flow of refrigerant through a multi-threaded device located around the circumference of the reactor module 2-1, forming a flow of refrigerant in the form of a hollow cylinder.

Moreover, in the reactor module 2-2:

- mixing zone 3-2 was performed similarly to mixing zone 3-1 in module 2-1;

- cooling zone 4-2 was formed by supplying refrigerant through two multi-threaded devices similar to a multi-threaded device installed in the cooling zone 4-1 of the reactor module 2-1. Moreover, these multi-threaded refrigerant supply devices were placed at a distance of 1/3 and 2/3 of the length of the reactor module 2-2 from the mixing zone 3-2.

The difference in the methods for producing methanol in examples 1 and 2 was in the form of the used refrigerant:

- in example 1 used a vapor-gas mixture of an aqueous solution of organic by-products formed after the separation of methanol in column 17, and said vapor-gas mixture from a collection vessel 20 was supplied to cooling zones 4-1 and 4-2 with a stream of an initial cold hydrocarbon-containing gas;

- in example 2, a similar vapor-gas mixture from a collection tank 20 was fed into cooling zones 4-1 and 4-2 with a stream of cooled off-gas-containing off-gas.

Moreover, in example 2, the execution of the installation according to the invention was a recirculation scheme.

In examples 1 and 2, hydrocarbon-containing gas was piped 6 from a gas source through a compressor 7 to a manifold 8, for example, a piping for gas distribution. The main stream of the hydrocarbon-containing gas was supplied to the heat exchanger 9 for heating the gases leaving the reactor 1. The auxiliary stream of the hydrocarbon-containing gas from the manifold 8 was supplied to the mixer 22 to form a refrigerant stream.

Pipeline 10 indicated the main stream — heated hydrocarbon-containing gas — into the reactor module l. Compressed oxygen-containing gas was also supplied to the reactor modules 2-1 and 2-2 from compressor 11 via pipelines 12-1 and 12-2. In the mixing zone 3-1, the heated hydrocarbon-containing gas was mixed with compressed oxygen-containing gas.

In the reaction zone 5-1, part of the hydrocarbon-containing gas was oxidized with oxygen, which caused the mixture to heat up, but the temperature in the oxidation zone was maintained in the required range of 520-570 ⁰ C according to the invention by cooling the reaction mixture with a coolant stream supplied through the device 13-1 to zone 4-1 of cooling. The flow rate of the refrigerant was controlled using device 14-1.

The processes taking place in the mixing, reaction and cooling zones are described above.

A mixture of products of the oxidation process and feed gases from reactor 1 was fed into a heat exchanger 9, where the feed stream of a hydrocarbon-containing gas was heated. The final cooling of the stream, if necessary, was carried out in the heat exchanger 15. From the heat exchanger 15, the stream was fed to a separator 16, in which liquid products, including organic by-products, were separated. For comparison, an example 3 of methanol production according to the production method described above as an analogue characterizing the prior art of the present invention (RU, 2162460, Cl) is presented.

In all examples 1-3, the initial hydrocarbon-containing gas was a mixture of the following composition,% by volume: methane - 98, carbon dioxide - 1 and nitrogen - 1.

The temperatures of the initial hydrocarbon-containing and oxygen-containing gases at the inlet of the methanol production unit were about 20 C.

However, in Example 1, all exhaust gas from the separator 16 was sent for disposal, and in Example 2, the exhaust gases from the separator 16 were partially supplied for disposal. In this case, gases partially pressurized by the compressor 19 were supplied to the mixer 22 to form a refrigerant stream ..

Then, in both Example 1 and Example 2, liquid products from the separator 16 were fed to a distillation column 17 to isolate the target product, methanol, from the mixture, which was then taken to methanol collector 18. An aqueous solution of organic by-products was collected in a collection tank 20 and then pumped 21 to a mixer 22 to form a refrigerant stream.

The main process parameters are presented in the table.

Table

The table shows that, compared with the known production method according to example 3, in the methanol production methods presented in examples 1 and 2, the working pressure in the reactor is lower and is 7.5 MPa, the temperature at the inlet to the reactor is increased and is 450 ⁰ C, and due to the partial disposal of secondary of products, the methanol yield is higher than in example 3, and is 654 kg / hour (example 1) and 808 kg / hour (example 2).

Thus, from the presented data, it can be concluded that the use of the method for producing methanol according to the invention in a plant according to the invention leads to an increase in the efficiency of the process for producing methanol, improving the operating conditions of structural elements of the plant. In addition, with the exception of the surface-type heat exchange section from the design of the reactor, it reduces the metal consumption of the reactor by 3 times and simplifies its design.

Industrial applicability

The methanol production method according to the invention can be carried out in a plant for its implementation according to the invention using known technologies, known structural materials and equipment. The plant for producing methanol according to the invention can be used in complexes of traditional methanol production with modification of process piping and equipment used in the reactor unit.

Claims

Claim 1. A method for the production of methanol, in which sequentially mixing separately supplied starting reagents is carried out: sequentially compressed and heated hydrocarbon-containing gas and compressed oxygen-containing gas, gas-phase oxidation of a hydrocarbon-containing gas at elevated temperature and pressure up to 10 MPa, subsequent cooling of the reaction mixture in the formed, respectively, mixing , the reaction zone and the cooling zone, and then the resulting mixture containing methanol is cooled, methanol is separated, and the waste the basics are sent to the source hydrocarbon-containing gas or for disposal, characterized in that the cooling zone of the reaction mixture is formed by continuously supplying refrigerant in the direction of movement of the reaction mixture stream after the reaction mixture leaves the mixing zone, with the formation of a refrigerant stream having a space for placement inside the stream, at least part of the reaction zone, and in this part of the reaction zone inside the refrigerant stream, the temperature of the reaction mixture is maintained in the range from 520 to 600 ⁰ C. 2. The method according to p. 1, characterized in that the temperature of the reaction mixture inside the refrigerant stream is preferably maintained in the range of 520-570 ⁰ C. 3. The method according to claim 1, characterized in that the reaction mixture is repeatedly subjected to sequential mixing with separately supplied compressed oxygen-containing gas, gas-phase oxidation and cooling in repeatedly mixed, reaction and cooling zones, and wherein the initial compressed and heated hydrocarbon-containing gas served in the first of the mixing zones, and oxygen-containing gas is fed into each of the mixing zones 4. The method according to claim 1, characterized in that the cooling zone is formed by repeatedly supplying refrigerant continuously. 5. The method according to p. 1, characterized in that the use of a refrigerant selected from the group including: part of the original cold hydrocarbon-containing gas; chilled hydrocarbon-containing off-gas; an aqueous solution of organic by-products formed after the separation of methanol; gas-vapor mixture of an aqueous solution of organic by-products with the original hydrocarbon-containing gas or with a cooled off-gas hydrocarbon-containing gas. 6. The method according to p. 1, characterized in that the temperature of the reaction mixture in the reaction zone is provided by controlling the parameters of the flow of refrigerant. 7. Installation for the production of methanol from hydrocarbon-containing gas, including: - at least one reactor having a housing in which one reaction module is placed, in which are formed in series: - a mixing zone adapted for mixing the feed products fed to the module and forming a reaction mixture stream; - a reaction zone for accommodating a stream of a reaction mixture subjected to gas phase oxidation, - a cooling zone adapted to accommodate at least a portion of the reaction mixture stream inside the refrigerant stream in the direction of movement of the reaction mixture stream and configured to vary the refrigerant flow rate to ensure that the temperature of the reaction mixture inside the refrigerant stream is not higher than 600 ⁰ C, and comprising devices for measuring the temperature in the reaction zone in the region to the cooling zone and the temperature in the part of the reaction zone located inside the refrigerant stream; a system for preparing the initial hydrocarbon-containing gas, providing the possibility of its sequential compression to 1.0-10.0 MPa and heating to 300-500 ⁰ C, and feeding it into the mixing zone of the reaction module; a system for preparing an oxygen-containing gas, providing the possibility of its compression up to 1.0-10.0 MPa, and feeding it into the mixing zone of the reaction module; - a system for supplying refrigerant to the cooling zone, comprising a device for supplying refrigerant with a stream with the formation of a space inside the stream to accommodate at least part of the reaction zone, and configured to control the parameters of the refrigerant stream; - a system of pipelines and devices providing cooling of reaction products and their separation into components to be separated or disposed of. 8. The installation according to claim 7, characterized in that the refrigerant supply system to the cooling zone comprises several devices arranged along the length of the reactor module that supply the refrigerant in a continuous flow with the formation of a space inside the flow to accommodate at least part of the reaction zone, and made with the ability to control the parameters of the refrigerant flow; 9. The installation according to claim 7, characterized in that the refrigerant supply system to the cooling zone is equipped with a device that ensures the formation of a refrigerant stream in the form of a hollow cylinder. 10. Installation according to claim 7, characterized in that the reactor contains several reaction modules arranged sequentially in the vessel one after the other. 11. Installation according to claim 7, characterized in that it is adapted to supply a refrigerant selected from the group including: a portion of the initial cold hydrocarbon-containing gas; chilled hydrocarbon-containing off-gas; an aqueous solution of organic by-products formed after the separation of methanol; a gas-vapor mixture of an aqueous solution of organic by-products with an initial hydrocarbon-containing gas or with a chilled off-gas from a hydrogen-containing gas.