RU2610277C1 - Method for production of methanol and hydrocarbons of gasoline range using synthetic gas - Google Patents

Abstract

FIELD: chemistry.

SUBSTANCE: method is carried out in cascade of three and more flow-through catalytic reactors (FCR). Synthetic gas (SG) with initial ratio hydrogen-carbon monoxide 1.5≤H₂:CO≤2 is passed successively through the first FCRs with catalyst for methanol synthesis with release of methanol as a target product; then the residual SG flow after methanol synthesis with ratio hydrogen- carbon monoxide H₂:CO≥1 is directed to FCR with bifunctional catalyst for synthesis of dimethyl ester (DME) and obtained DME is supplied to FCR for synthesis of hydrocarbons of gasoline range (HGR) with subsequent isolation of HGR and waste products sent for disposal.

EFFECT: method allows to increase the total transformation rate of carbon monoxide and enhance the target product output.

8 cl, 1 dwg, 4 tbl, 6 ex

Description

The invention relates to the field of organic synthesis, in particular to the production of oxygenates (methanol) and gasoline hydrocarbons (gasoline and aromatic hydrocarbons) from synthesis gas obtained by the conversion of carbon-containing raw materials.

LIST OF ABBREVIATIONS

DME - dimethyl ether

RCC - flow catalytic reactor

SG - synthesis gas

UBR - gasoline hydrocarbons (gasoline, aromatic hydrocarbons).

The process of synthesis of methanol from synthesis gas is widely used in industry, since methanol can be used to produce a number of organic products: formaldehyde, methyl terephthalate, synthetic resins, drugs, and can also be used as a solvent for gas hydrates during well operation.

Obtained in the process of the proposed method, dimethyl ether (DME) together with methanol is an intermediate for the further production of gasoline hydrocarbons (UBR), in addition, they can be used directly as motor fuel.

A known method of producing methanol, which includes the reaction of carbon monoxide and dioxide with hydrogen under a pressure of 1.0-15.0 MPa (preferably from 4.0 to 8.0 MPa), at a temperature of 160-300 ° C (preferably from 190 to 270 ° C ), a space velocity of 7000-25000 h ^-1 in the presence of a catalyst containing copper and zinc oxides and at least one metal oxide of the second and fourth groups of the Periodic System that is difficult to recover, the separation of methanol from the reaction mixture and the recycling of substances that did not react in the synthesis of methanol. As a raw material, a mixture of carbon oxides and hydrogen is used, and carbon dioxide is contained in an amount of 1-20 vol. % (preferably 3-12 vol.%). In the reaction gas in contact with the catalyst, the volume ratio of hydrogen to the sum of carbon oxides is 1.3–3.0 times greater than the stoichiometric ratio (British patent 1159095). The disadvantages of this method are the low specific productivity of the copper-containing catalyst (0.191-0.425 kg / l per hour), as well as significant energy costs for recirculation of the gas mixture.

There is also known a method for producing methanol from synthesis gas containing hydrogen and carbon oxides, in which fresh gas is supplied to a reactor without circulation of the gas mixture, and unreacted gas after condensation of methanol is supplied as fresh gas to the reactor with circulation of synthesis gas. The flow reactor is isothermal (application Germany No. 3518362). The disadvantage of the described method is the use of compressors of greater power for circulating the gas mixture in the second stage, and therefore, significant energy consumption.

US Pat. No. 5,472,986 describes a process for producing methanol from synthesis gas in which the stoichiometric amount of hydrogen with respect to carbon oxides does not exceed 90%. The invention uses a recirculation method for hydrogen recovered from tail gases, where a gas enriched in hydrogen and recovered using hydrogen permeable membranes is used as recirculated gas. In the technological scheme of the process, the use of a cascade of reactors is considered. The disadvantage of this method is that the applied method of recirculating gas with a high hydrogen content does not allow to obtain at the entrance to each subsequent reactor the optimal composition of the reacting gas for methanol synthesis. So, however, the parameter H ₂ / (2CO + 3CO ₂ ) used by the authors in the description of the invention at the inlet to each subsequent reactor is 0.9885, 0.9848, 0.9811 and 0.9745, which means that the parameter H ₂ / ( СО + СО ₂ ) does not exceed 2, although it is known that the parameter Н ₂ / (СО + СО ₂ ) = 2 and higher is optimal for the reaction. In addition, the process working pressure described in the method is 72.7 atm, which requires the use of expensive high-pressure compressors.

A known method of producing methanol by contacting a gas mixture containing carbon monoxide, carbon dioxide and hydrogen with a copper-containing catalyst at a temperature of 190-290 ° C and a pressure of 5-10 MPa in two stages. In the first stage, the copper-containing catalyst is brought into contact with a gas mixture containing 5-30 vol.% Carbon monoxide and 0.3-20.0 vol.% Carbon dioxide with a volume ratio of carbon monoxide to carbon dioxide of 0.25-87 and a volume ratio hydrogen to the sum of carbon oxides 2-3.65. This stage is carried out in a flow or cascade type reactor at a space velocity of the initial gas mixture of 4500-100000 h ^-1 , while obtaining a gas mixture containing carbon monoxide, carbon dioxide, hydrogen, methanol vapor and 0.02-1.38 vol. % water vapor, the indicated methanol vapor 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 out in the reactor by circulating the gas mixture with a space velocity of 7000-15000 h ^-1 , after which the gas mixture containing carbon monoxide, carbon dioxide and hydrogen, methanol and water vapors that are removed from the gas mixture (WO 88/00580).

The disadvantages of this method include the low specific productivity of the copper-containing catalyst in the second stage, which, depending on the synthesis conditions, is 0.40-0.68 t / m ³ h, the insignificant contribution of methanol obtained in the first stage to its total amount from 5.42 up to 78.33%, high gas mixture circulation rates. This involves the use of high power compressors and significant energy costs for the circulation of the gas mixture, which significantly impairs the technical and economic performance of the process.

In the works of [Rozovsky A.Ya. Environmentally friendly motor fuels based on natural gas // Chemistry in the interests of sustainable development. 2005. T. 13. S. 701-712; Rozovsky A.Ya. Dimethyl ether and gasoline from natural gas // Zh. Grew up. Chem. about them DI. Mendeleev - 2003] it is mentioned that if in the synthesis of methanol 15-20% of carbon oxides are converted by passing through a reactor with a catalyst, then in the synthesis of DME it is 60-80% under close conditions. Correspondingly, the productivity of a unit volume of the reactor sharply increases, but even more importantly, it can use “poor” synthesis gas obtained by oxidizing natural gas with air and containing 50-60% nitrogen and only 10-15% carbon monoxide. According to various estimates, the direct synthesis of DME from synthesis gas is 5-20% more economical than the synthesis of an equivalent amount of methanol. The increase in CO conversion as a result of the one-step synthesis of DME from synthesis gas on bifunctional catalysts is explained by the rapid conversion of methanol to DME, which allows shifting the reaction equilibrium towards the formation of oxygenates. Thus, the one-step synthesis of DME from a mixture of CO, CO ₂ and H _{2 is} more productive and requires less capital expenditures compared to the preparation of DME from synthesis gas in two stages — through methanol synthesis.

Examples are also known of the direct production of gasoline hydrocarbons directly from synthesis gas. All these technologies are many reactor ones. So, the patent of the Russian Federation No. 2143417 is known, where the increase in the yield of the liquid fraction of C ₅₊ hydrocarbons calculated on the supplied carbon oxides is achieved by catalytic processing of the mixture of CO, CO ₂ and H ₂ in two stages so that in the first stage the feedstock contacts the catalyst, consisting of zeolite type ZSM-5 and a metal oxide component containing, by weight. %: GuO 38-64, ZnO 24-34, Cr ₂ O ₃ 0-22, Al ₂ O ₃ 6-9, mixed in the mass ratio (20-50) :( 80-50), the gas stream after the first stage reactor without separation, they are sent to the second stage, where in contact with a catalyst consisting of a zeolite of the ZSM-5 type and a metal oxide component containing (wt.%): ZnO 65-70, Cr ₂ O ₃ 29-34, W ₂ O ₅ 1 mixed in the ratio (30-90) :( 70-1), the dimethyl ether and the components of the synthesis gas are converted into a gasoline fraction, gaseous hydrocarbons and an aqueous fraction.

A known method of producing DME and / or high-octane gasoline from methanol, developed by the company "Mobil Oil Corporation" (US patent No. 4587373). According to this method, methanol is fed into a reactor containing a ZSM-5 type catalyst at elevated temperature and pressure of 3-20 atm. The reaction products are sequentially separated in separators, an absorber and distillation columns with the release according to option 1 - DME, stable gasoline and olefins, according to option 2 - only stable gasoline and olefins. DME, together with methanol and water in option 2, is recycled to be converted to hydrocarbons. The inventive method has differences from the analogue in the type of processed raw materials and the catalyst used.

A known method of producing hydrocarbons by processing synthesis gas containing hydrogen and carbon oxides and having a molar ratio of CO / H ₂ above 1, provided that the synthesis gas entering the conversion has a molar ratio of CO / CO ₂ from 5 to 20 (patent U.S. No. 4,481,305). According to the invention, the process is carried out in two successive reactors at a pressure of 5-100 atm without intermediate separation of products after the first reactor. In the first reactor, the synthesis gas is in contact with one or more catalysts that convert the synthesis gas at a temperature of 150-400 ° C to methanol and then in the same reactor in DME.

Next, the gas mixture is sent to the second reactor, where in the presence of a zeolite catalyst at a temperature of 150-600 ° C, DME converts to hydrocarbons, mainly liquid under normal conditions.

The main disadvantages of this method are:

1) the low yield of the gasoline fraction on the fed "carbon" of the feedstock (29 wt.%), Since the use of layer-by-layer loading of the catalyst in the 1st reactor does not allow for a high conversion of CO.

2) the process does not provide for obtaining DME as the target product.

Thus, the most promising from the point of view of methanol yield are methods for its production, when the synthesis gas is sequentially passed through a cascade of flow reactors in one stage without recirculation of the gas mixture, while methanol and water are isolated by condensation after each reactor. From the point of view of the subsequent production of hydrocarbons in methods of their direct synthesis from synthesis gas, it is optimal to ensure the maximum conversion of CO and the yield of oxygenates, it does not matter that it will be methanol or DME, or a mixture thereof.

A known method for producing methanol described in the patent of the Russian Federation No. 2181117, according to which methanol is obtained by contacting a gas mixture containing carbon oxides and hydrogen with a copper-containing catalyst at a temperature of 190-290 ° C, a pressure of 5.0-10.0 MPa and a space velocity of 4500 -100,000 h-1. In this case, the initial gas mixture containing 1.0-33.7 vol. % carbon monoxide, 0.3-22.5 vol. % carbon dioxide with a volume ratio of hydrogen to the sum of carbon oxides of 1.91-5.60, as well as 0.5-50.0 vol. % nitrogen, sequentially passed through a cascade of flow reactors in one stage, while methanol and water are isolated by condensation after each reactor.

The use of this method is limited by the upper limit of the carbon monoxide content of 33.7 vol. % in the processed synthesis gas. This is explained by the fact that, at a higher CO content, the ratio of reacting components at the inlet to the cascade of reactors becomes much lower than the stoichiometric one, which leads to a decrease in the degree of conversion of carbon oxides to methanol due to an increasing lack of hydrogen in each subsequent cascade flow reactor. At the same time, during gasification of various technogenic, oil and coal wastes, the technology that is the most promising process for their processing, the content of carbon monoxide in the resulting synthesis gas (even with steam conversion) is usually more than 35%, and the ratio of Н ₂ : СО ≤2. This method provides only methanol.

An object of the present invention is to provide a method for simultaneously producing methanol and gasoline hydrocarbons from synthesis gas in one process with a reduced initial ratio of H ₂ / CO in synthesis gas of not more than 2, as well as increasing the total degree of conversion of carbon monoxide and increasing the yield target products: oxygenates and liquid fraction of C5 + hydrocarbons.

To achieve the technical task, a method is proposed for producing methanol and gasoline hydrocarbons (UBR) from synthesis gas in a cascade of three or more flow catalytic reactors (RCC), which consists in the fact that synthesis gas (SG) with an initial hydrogen-oxide ratio carbon 1,5≤N _2: SO≤2 successively passed through the first downstream RCC with a methanol synthesis catalyst with separation of methanol as the desired product, then the remainder after the methanol synthesis stream IG ratio of carbon-hydrogen oxide H _2: CO 1 is directed to PKR bifunctional catalyst synthesis of dimethyl ether (DME), resulting in direct DME synthesis RCC UBR UBR followed by isolation and waste sent for disposal.

Besides,

- methanol synthesis is carried out at a temperature of 200-270 ° C and a pressure of 50 atm;

- synthesis of DME is carried out at a temperature of 270-320 ° C and a pressure of 50 atm;

- synthesis of UBR is carried out at a temperature of 370-420 ° C and a pressure of 10 atm;

- part of the obtained methanol is sent to RPC synthesis of UBR;

- as a catalyst for the synthesis of methanol using copper-zinc-aluminum catalyst, composition (in wt.%): CuO - 64.86; ZnO - 25.1; Al ₂ O ₃ - 10.04;

- as a catalyst for the synthesis of DME using a mechanical mixture (1 / 1-3 / 1) of aluminum oxide grade A-64 and copper-zinc-aluminum catalyst;

- a catalyst based on crystalline aluminosilicate, such as pentasil, with a molar ratio of SiO ₂ / Al ₂ O ₃ = 20-100 is used as a catalyst for the synthesis of UBR.

The essence of the invention is as follows - methanol and gasoline hydrocarbons are obtained from synthesis gas with a ratio of 1.5≤N ₂ : СО≤2 in a cascade of three or more flow reactors, in the first reactor (s) of the cascade, methanol synthesis is carried out with its isolation as the target product, and in the last two reactors along the cascade, DME is first synthesized without isolation of DME as the target product, and then UBR synthesis.

As the SG passes through the cascade of methanol synthesis reactors, the ratio of H ₂ : CO in the residual flows of the SG decreases, which leads to a decrease in the conversion of methanol synthesis in each subsequent cascade reactor. The degree of reduction in conversion depends on the value of the initial ratio of H ₂ : CO, - the smaller this value, the faster the degree of conversion. The choice of the number of methanol synthesis reactors is carried out on the condition that the ratio of hydrogen-carbon monoxide H ₂ : СО≥1 is reached in the residual SG stream directed to the DME synthesis, as well as a predetermined methanol productivity. The limitation of the hydrogen-carbon monoxide ratio to H ₂ : CO≥1 is significant from the point of view of obtaining the degree of conversion in the synthesis of DME of the same order as in the synthesis of methanol. This ensures the achievement of a technical result, the simultaneous production of methanol and gasoline hydrocarbons from synthesis gas in one technological process, as well as an increase in the total degree of conversion of carbon monoxide and an increase in the yield of oxygenates and the liquid fraction of C5 + hydrocarbons. If it is necessary to increase the productivity of the process by UBR, methanol obtained in its synthesis reactors can be partially added to this stream. The methanol output in this case is accordingly reduced. The claimed parameters of the synthesis in RCC (temperature and pressure) are optimal from the point of view of the yield of the target products and obtained by calculation and experimental methods. The choice of types of catalysts for implementing the proposed method is determined by the specific composition of the synthesis gas streams entering the synthesis reactors.

Based on the results of our own research, as well as literature, the most optimal is the use of the following types of catalysts.

As a catalyst for the synthesis of methanol in the proposed method, a copper-zinc-aluminum catalyst is used, composition (in wt.%): CuO - 64.86; ZnO - 25.1; Al ₂ O ₃ - 10.04 (in the form of cylindrical tablets with a diameter of 5.0 mm and a height of 4.0 mm).

As a catalyst for the synthesis of DME in the proposed method, a mechanical mixture (1 / 1-3 / 1) of aluminum oxide grade A-64 (Ryazan catalyst factory) and the same copper-zinc-aluminum catalyst is used.

As a catalyst for the synthesis of gasoline hydrocarbons, a catalyst based on crystalline aluminosilicate, such as pentasil, with a molar ratio of SiO ₂ / Al ₂ O ₃ = 20-100, characterized by the presence of a residual amount of sodium ions equivalent to a content of 0.05-0.1 wt. . % sodium oxide containing the specified crystalline aluminosilicate and a binder component, and it additionally contains rare earth oxides and zinc oxide in the following ratio, wt. %:

zinc oxide - 0.5-3.0

rare earth oxides - 0.1-5.0

crystalline aluminosilicate - 60-70

the binder is the rest.

The drawing shows a General diagram of the implementation of the method on the example of a cascade of four reactors, where

1 - synthesis gas stream;

2 - the first RCC synthesis of methanol;

3 - reaction products from the output of the first RCC synthesis of methanol;

4 - a separator of reaction products from the output of the first RCC synthesis of methanol;

5 - methanol collection line;

6 - a collection of methanol;

7 - unreacted synthesis gas from the output of the first RCC synthesis of methanol;

8 - second RCC synthesis of methanol;

9 - reaction products from the second RCC synthesis of methanol;

10 - a separator of reaction products from the second RCC synthesis of methanol;

11 - unreacted synthesis gas from the output of the second RCC synthesis of methanol;

12 - RCC synthesis of DME;

13 - reaction products from the output of RCC synthesis of DME;

14 - RCC synthesis of UBR;

15 - reaction products from the output of RCC synthesis of UBR;

16 - separator of the reaction products of the synthesis of UBR;

17 - collection of UBR;

18 - reaction water;

19 is a stream of residual gases for disposal;

20 - methanol stream for UBR synthesis.

Consider the method of the method on the example of a cascade of four reactors.

The synthesis gas stream 1 containing hydrogen and carbon monoxide with a ratio of 1.5 Н H ₂ : CO _{2 2} at a temperature of 200-270 ° C is sent to the first flow catalytic reactor 2 along the cascade with a methanol synthesis catalyst, for example, copper zinc-aluminum catalyst, composition (in wt.%): CuO - 64.86; ZnO - 25.1; Al ₂ O ₃ - 10.04 (in the form of cylindrical tablets with a diameter of 5.0 mm and a height of 4.0 mm). Next, the reaction product stream 3 is sent to a separator 4, in which the obtained methanol and unreacted synthesis gas are separated. Methanol is sent through a methanol collection line 5 to a methanol collector 6, and a stream of unreacted synthesis gas 7 heated to a temperature of 270-320 ° C. is sent to a second flow catalytic reactor 8 with a methanol synthesis catalyst in the second cascade. Next, the reaction product stream 9 is directed to a separator 10, in which the obtained methanol and unreacted synthesis gas are separated. Methanol is sent along a methanol collection line 5 to a collection vessel 6.

Next, the flow of unreacted synthesis gas 11 with a content of hydrogen-carbon monoxide H ₂ : СО≥1, heated to a temperature of 370-420 ° C, is sent to the third flow catalytic reactor 12 with a bifunctional catalyst for the synthesis of DME along the cascade, for example, a mechanical mixture ( 1 / 1-3 / 1) aluminum oxide grade A-64 (Ryazan catalyst factory) and the same copper-zinc-aluminum catalyst. The reaction products 13 from the outlet of the reactor 12 are sent to the gasoline hydrocarbon synthesis catalytic reactor 14. A catalyst based on crystalline aluminosilicate, such as pentasil, with a molar ratio SiO ₂ / Al ₂ O ₃ = 20-100, characterized by the presence of the residual amount of sodium ions equivalent to a content of 0.05-0.1 wt. % sodium oxide containing the specified crystalline aluminosilicate and a binder component, and it additionally contains rare earth oxides and zinc oxide in the following ratio, wt. %:

zinc oxide - 0.5-3.0

rare earth oxides - 0.1-5.0

crystalline aluminosilicate - 60-70

the binder is the rest.

Methanol stream 20 from methanol collection line 5 can be partially added to the inlet stream of hydrocarbon synthesis reactor 14.

The reaction products 15 from the outlet of the reactor 14 are sent to a separator 16, in which UBR (gasoline, aromatic hydrocarbons), reaction water 18 and residual gaseous products 19 containing, including hydrogen and lower hydrocarbons, are isolated. Gasoline and aromatic hydrocarbons are sent to the product collection 17, reaction water 18 is used to produce steam, and the residual gaseous products 19 can be used as fuel gas to produce heat and / or electricity.

The synthesis of methanol and DME is carried out at a pressure of 50 atm, and the synthesis of hydrocarbons at a pressure of 10 atm.

The synthesis gas stream 1 is heated to the desired temperature, as well as the intermediate streams 7, 11, 13, and 20, arriving at the RCC inlets, are carried out using, for example, tubular gas furnaces (not shown in the diagram). Heating can be carried out, for example, by burning part of the residual gaseous products 19.

The invention is illustrated by the following examples.

The calculation of the amount of obtained oxygenates (methanol and DME) was carried out per 1000 m ^{3 of the} initial SG with a different ratio of Н ₂ / СО (1.63 and 1.83) supplied to the RCC cascade (Figure) with the release of methanol after RCC (pos. 2) and RCC (pos. 8), while in the RCC (pos. 12) a bifunctional catalyst for the synthesis of DME is loaded (examples No. 1 and No. 2). In comparative examples No. 3 and No. 4, a variant is considered when a catalyst for the synthesis of methanol is loaded in RCC (item 12).

A comparison of the examples of the invention (No. 1 and 2) and comparative examples (No. 3 and 4) shows that the replacement of the methanol catalyst cascade in the last reactor with a bifunctional direct DME synthesis catalyst leads to a significant increase in the total CO conversion, as well as the total amount of oxygenates obtained (methanol and DME). It should be noted that when working on SG with a ratio of H _{2 /} CO = 1.6.3 (example No. 1), it was possible to achieve a larger relative increase in the amount of oxygenates obtained (24.8%), compared with 20.1% when working on SG with H ₂ /CO=1.83 (example No. 3).

To obtain UBR from oxygenates, gas products from the last reactor of the oxygenate production cascade, containing mainly DME, after mixing with part of the methanol obtained in the first two reactors and additional heating to a temperature of 370-420 ° C, are sent directly to the liquid hydrocarbon production reactor.

Table 2 shows the material balance of the process of processing oxygenates into gasoline at 100% conversion of oxygenates. Oxygenates are obtained from SG with H2 / CO = 1.83. Examples of the method are given, example No. 5, when DME from the last reactor is subjected to conversion to UBR and (for ease of comparison) all methanol from methanol synthesis reactors (according to example No. 2 from table 1), as well as comparative example No. 6, when subjected to conversion all methanol obtained in a cascade of 3 methanol synthesis reactors (according to example No. 4 from table 1).

Table 3 shows the average composition of gaseous hydrocarbons formed in the RCC (item 14) upon receipt of gasoline from oxygenates by the proposed method according to example No. 5.

Table 4 shows the average composition of the UBR formed in the RCC (item 14) upon receipt of gasoline from oxygenates by the proposed method according to example No. 5. (Mac,%).

Thus, according to table 2, the yield of liquid UBR. on the fed "carbon" of the feedstock in the method proposed in the present invention reaches 54.2% by weight, which is significantly higher than, for example, in the analogue invention (29% by weight), according to US patent No. 4,481,305.

Additional advantages of the technical solutions used in the proposed method is that:

- valuable petrochemical products can be produced with a high yield by utilization of various technogenic, oil and coal wastes during gasification of which synthesis gas is obtained with a ratio of 1.6≤N ₂ : СО≤2.

- In the process there are no recirculation flows requiring additional energy costs.

- methanol synthesis reactors and the next DME synthesis cascade reactor operate in the same pressure range.

- depending on the composition of the initial synthesis gas (H ₂ / CO ratio and the amount of CO ₂ and ballast gases), either a reduction or an increase in the number of methanol synthesis reactors in which the H ₂ / CO ratio should not be less than 1 is provided for effective synthesis, 6.

- there is no need for an intermediate separation of oxygenates (mainly DME) before they are fed to the hydrocarbon synthesis reactor.

- provides for the input or output of one or more methanol reactors in a cascade, as well as the option of partial use of the obtained methanol in the synthesis of UBR, which makes it easy to control the capacity of the plant and the ratio of the obtained methanol and hydrocarbons, taking into account market demand for products.

Claims (8)

1. A method of producing methanol and gasoline hydrocarbons (UBR) from synthesis gas in a cascade of three or more flow catalytic reactors (RCC), which consists in the fact that synthesis gas (SG) with an initial ratio of hydrogen-carbon monoxide of 1.5 ≤H ₂ : СО≤2 is sequentially passed through the first SCRs with a methanol synthesis catalyst with the release of methanol as the target product, then the residual SG stream after methanol synthesis with a hydrogen-carbon monoxide ratio of H ₂ : СО≥1 is sent to the SCR with a bifunctional synth catalyst Dimethyl ether (DME), the obtained DME is sent to the RCC for the synthesis of UBR, followed by the separation of UBR and waste sent for disposal. 2. The method according to p. 1, characterized in that the synthesis of methanol is carried out at a temperature of 200-270 ° C and a pressure of 50 atm. 3. The method according to p. 1, characterized in that the synthesis of DME is carried out at a temperature of 270-320 ° C and a pressure of 50 atm. 4. The method according to p. 1, characterized in that the synthesis of UBR is carried out at a temperature of 370-420 ° C and a pressure of 10 atm. 5. The method according to p. 1, characterized in that part of the obtained methanol is sent to RPC synthesis of UBR. 6. The method according to p. 1, characterized in that as a catalyst for the synthesis of methanol using copper-zinc-aluminum catalyst, composition (wt.%): CuO - 64.86; ZnO - 25.1; Al ₂ O ₃ - 10.04. 7. The method according to p. 1, characterized in that as a catalyst for the synthesis of DME using a mechanical mixture (1 / 1-3 / 1) of aluminum oxide grade A-64 and a copper-zinc-aluminum catalyst according to p. 6. 8. The method according to p. 1, characterized in that a catalyst based on crystalline aluminosilicate of the pentasil type with a molar ratio of SiO ₂ / Al ₂ O ₃ = 20-100 is used as a catalyst for the synthesis of UBR.

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