METHODS FOR PRODUCING AROMATIC HYDROCARBONS FROM NATURAL GAS AND INSTALLATION FOR IMPLEMENTING SAME

Abstract

The invention relates to the field of gas chemistry and, more specifically, to methods and devices for producing aromatic hydrocarbons from natural gas, which involve producing synthesis gas, converting same into methanol, producing, from the methanol, in the presence of a catalyst, a concentrate of aromatic hydrocarbons and water, separating the water, air stripping hydrocarbon residues from the water, and separating-out the resultant concentrate of aromatic hydrocarbons and hydrogen-containing gas, the latter being at least partially used in the production of synthesis gas to adjust the ratio therein of H.sub.2:CO 1.8-2.3:1, and can be used for producing aromatic hydrocarbons. According to the invention, the production of aromatic hydrocarbons from methanol in the presence of a catalyst is carried out in two consecutively-connected reactors for synthesizing aromatic hydrocarbons: in a first, low-temperature isothermal reactor for synthesizing aromatic and aliphatic hydrocarbons, and in a second, high-temperature adiabatic reactor for synthesizing aromatic and aliphatic hydrocarbons from aliphatic hydrocarbons formed in the first reactor, and the subsequent stabilization thereof in an aromatic hydrocarbon concentrate stabilization unit. At least a portion of the hydrogen-containing gas is fed to a synthesis gas production unit and is used for producing synthesis gas using autothermal reforming technology. The installation carries out the method. The achieved technical result consists in increasing the efficiency of producing concentrates of aromatic hydrocarbons.

Claims

1 to 12. (canceled)

13. A method of converting natural gas into aromatic hydrocarbons, the method comprising: a. mixing natural gas, superheated steam and recycled hydrogen-containing gas to form a first mixture; b. feeding the first mixture into a synthesis gas unit; c. the synthesis gas unit converting the first mixture into a synthesis gas; d. feeding the synthesis gas into a methanol unit; e. the methanol unit converting the synthesis gas into methanol; f. feeding the methanol into a condensing unit; the condensing unit comprising a low-temperature isothermal reactor containing a first catalyst and a high temperature adiabatic reactor containing a second catalyst; the condensing unit converting the methanol into a second mixture comprising aromatic and aliphatic hydrocarbons; g. feeding the second mixture into a separation unit; the separation unit separating water, hydrogen-containing gas, light aliphatic hydrocarbons and stable concentrate of aromatic hydrocarbons, wherein the hydrogen-containing gas is recycled into the first mixture.

14. The method of claim 13, wherein the methane comprises biogas.

15. The method of claim 13, wherein the methane comprises natural gas extracted with petroleum.

16. The method of claim 13, wherein the synthesis gas unit comprises an adiabatic pre-reforming unit.

17. The method of claim 13, wherein the synthesis gas unit comprises an autothermal reforming unit;

18. The method of claim 16, wherein the synthesis gas unit comprises an autothermal reforming unit.

19. The method of claim 13, wherein the synthesis gas unit comprises a heat recovery unit.

20. The method of claim 18, wherein the synthesis gas unit comprises a heat recovery unit.

21. The methods of claims 13, 15, 16, and 17, wherein the first mixture has a temperature of 300 C. to 450 C. as it is fed into the synthesis gas unit.

22. The method of claim 13, wherein the synthesis gas has a ratio of H.sub.2 to CO of 1.8-2.3 to 1.

23. The method of claims 22, wherein the first mixture has a temperature of 300 C. to 450 C. as it is fed into the synthesis gas unit.

24. The method of claim 13, wherein the synthesis gas has a stoichiometric ratio of f 2.05.

25. The method of claim 13, wherein the methanol has a concentration of at least 94% by weight.

26. The method of claim 13, wherein the first and second catalyst are the same.

27. The method of claim 13, wherein the first catalyst is a pentasil-type crystalline aluminosilicate with SiO.sub.2/Al.sub.2O.sub.3=25-100, comprising: 0.05-0.1 wt. % sodium oxide; and zinc oxides, rare earth oxides, cobalt oxide, crystalline aluminosilicate and a binding component.

28. The method of claim 27, wherein the first catalyst comprises weight % ratios of: zinc oxide 0.5-3.0; rare earth oxides 0.1-5.0; cobalt oxide 0.05-2.5; crystalline aluminosilicate: 63-70; and the remainder being the binding component.

29. The method of claim 27, wherein wherein the synthesis gas has a stoichiometric ratio of f2.05.

30. The method of claim 28, wherein wherein the synthesis gas has a stoichiometric ratio of f2.05.

31. The method of claim 13, wherein the second catalyst is a pentasil-type crystalline aluminosilicate with SiO.sub.2/Al.sub.2O.sub.3=25-120 comprising: 0.05-0.1 wt. % sodium oxide; and, zinc oxides, sodium oxide, rare earth oxides, cobalt oxide, crystalline aluminosilicate and a binding component.

32. The method of claim 28, wherein the second catalyst is a pentasil-type crystalline aluminosilicate with SiO.sub.2/Al.sub.2O.sub.3=25-120 comprising: 0.05-0.1 wt. % sodium oxide; and, zinc oxides, sodium oxide, rare earth oxides, cobalt oxide, crystalline aluminosilicate and a binding component.

33. The method of 31, wherein the second catalysis comprises weight % of: zinc oxide 0.5-3.0; sodium oxide 0.12-0.30; rare earth oxides 0.1-3.0; cobalt oxide 0.05-2.5; crystalline aluminosilicate 63.0-70.0; and the remainder the binding component.

34. The method of claim 33, wherein the rare earth components comprise CeO.sub.2, La.sub.2O.sub.3 and Nd.sub.2O.sub.3 and Pr.sub.6O.sub.11.

35. The method of claim 34, wherein the rare earth components comprise weight % of: cerium oxide CeO.sub.2 3.0; La.sub.2O.sub.3 65.0; Nd.sub.2O.sub.3; 21.0 Pr.sub.6O.sub.11 the remaining % of rare earch components; and a binding component.

36. The method of 32, wherein the second catalyst comprises weight % of: zinc oxide 0.5-3.0; sodium oxide 0.12-0.30; rare earth oxides 0.1-3.0; cobalt oxide 0.05-2.5; crystalline aluminosilicate 63.0-70.0; and the remainder the binding component.

37. The method of claim 36, wherein the rare components comprise CeO.sub.2, La.sub.2O.sub.3 and Nd.sub.2O.sub.3 and Pr.sub.6O.sub.11.

38. The methods of claims 34 and 35, wherein the synthesis gas has a stoichiometric ratio of f2.05.

39. The method of claims 13, wherein the stable concentrate of aromatic hydrocarbons are selected from the group consisting of benzene, toluene, ethylbenzene and xylenes.

40. A method of converting natural gas into aromatic hydrocarbons including one or more of benzene, toluene, ethylbenzene and xylenes, the method comprising: mixing natural gas, superheated steam and a predetermined amount of recycled hydrogen-containing gas to form a first mixture; converting the first mixture into a synthesis gas; converting the synthesis gas into methanol; converting the methanol into a second mixture comprising aromatic and aliphatic hydrocarbons; and separating hydrogen-containing gas from the mixture comprising aromatic and aliphatic hydrocarbons; thereby providing the recycled hydrogen-containing gas; wherein the predetermined amount of recycled gas is selected to provide a ratio of H.sub.2 to CO of 1.8-2.3 to 1 in the synthesis gas.

41. The method of claim 40, wherein the methanol has a concentration of at least 94% by weight.

42. The method of claim 40, wherein the heat efficiency coefficient of the method is from 55% to 65%.

43. A method of converting natural gas into aromatic hydrocarbons including one or more of benzene, toluene, ethylbenzene and xylenes, the method comprising: mixing natural gas, superheated steam and a predetermined amount of recycled hydrogen-containing gas to form a first mixture; converting the first mixture into a synthesis gas; converting the synthesis gas into methanol; converting the methanol into a second mixture comprising aromatic and aliphatic hydrocarbons; and separating hydrogen-containing gas from the mixture comprising aromatic and aliphatic hydrocarbons; thereby providing the recycled hydrogen-containing gas; wherein the predetermined amount of recycled gas is selected to provide a stoichiometric ratio of f2.05.

44. The method of claim 31, wherein the methanol has a concentration of at least 94% by weight.

45. The method of claim 31, wherein the heat efficiency coefficient of the method is 65%.

46. A method for producing a concentrate of aromatic hydrocarbons from natural gas, the method comprising: producing a synthesis gas, converting the synthesis gas into a methanol, then producing, from the methanol, in the presence of a catalyst, a concentrate of aromatic hydrocarbons and water, separating the water, air stripping hydrocarbon residues from the water, and separating-out a resultant concentrate of aromatic hydrocarbons and, the hydrogen-containing gas being recycled to control the production of synthesis gas to adjust the ratio of the synthesis gas to H.sub.2:CO 1.8-2.3:1; wherein the production of aromatic hydrocarbons from methanol in the presence of a catalyst is carried out in two consecutively-connected reactors for synthesizing aromatic hydrocarbons: in a first, low-temperature isothermal reactor for synthesizing aromatic and aliphatic hydrocarbons, and in a second, high-temperature adiabatic reactor for synthesizing aromatic and aliphatic hydrocarbons from aliphatic hydrocarbons formed in the first reactor, and the subsequent stabilization of the concentrate of aromatic hydrocarbons in a stabilization unit; wherein at least a portion of the hydrogen-containing gas is fed to a synthesis gas production unit and is used for producing synthesis gas using autothermal reforming technology with a pre-reforming unit or non-catalytic partial oxidation using oxygen or oxygen-air mixtures as the oxidant to adjust the ratio therein according to the relationship (the MF of H.sub.2 the MF of CO.sub.2)/(the ME of CO+the MF of CO.sub.2)2, wherein ME stands for the mole fraction of the component in the synthesis gas.

47. An system for producing a mixture comprising aromatic and aliphatic hydrocarbons, the a system comprising: a. a low-temperature isothermal reactor containing a first catalyst and a high temperature adiabatic reactor containing a second catalyst; b. wherein the first catalyst is a pentasil-type crystalline aluminosilicate with SiO.sub.2/Al.sub.2O.sub.3=25-100, comprising: 0.05-0.1 wt. % sodium oxide; and zinc oxides, rare earth oxides, cobalt oxide, crystalline aluminosilicate and a binding component; c. wherein the first catalyst comprises weight % ratios of: zinc oxide 0.5-3.0; rare earth oxides 0.1-5.0; cobalt oxide 0.05-2.5; crystalline aluminosilicate: 63-70; and the remainder being the binding component; d. wherein the second catalyst is a pentasil-type crystalline aluminosilicate with SiO.sub.2/Al.sub.2O.sub.3=25-120 comprising: 0.05-0.1 wt. % sodium oxide; and, zinc oxides, sodium oxide, rare earth oxides, cobalt oxide, crystalline aluminosilicate and a binding component; e. wherein the second catalysis comprises weight % ratios of: zinc oxide 0.5-3.0; sodium oxide 0.12-0.30; rare earth oxides 0.1-3.0; cobalt oxide 0.05-2.5; crystalline aluminosilicate 63.0-70.0; and the remainder the binding; f. wherein the second catalyst rare earth components comprise CeO.sub.2, La.sub.2O.sub.3 and Nd.sub.2O.sub.3 and Pr.sub.6O.sub.11; and, g. wherein the second catalyst rare earth components comprise weight % ratios of: cerium oxide CeO.sub.2 3.0; La.sub.2O.sub.3 65.0; Nd.sub.2O.sub.3; 21.0 Pr.sub.6O.sub.11; and the remainder a material.

48. A system for producing a concentrate of aromatic hydrocarbons from natural gas, the system comprising: a. a synthesis gas unit in fluid communication with a methanol unit in fluid communication with a concentrate of aromatic hydrocarbons unit in fluid communication with a separation unit; b. the concentrate of aromatic hydrocarbons unit comprising a first and a second consecutively-connected reactors for synthesizing aromatic hydrocarbons; i. the first reactor comprising a low-temperature isothermal reactor for synthesizing aromatic and aliphatic hydrocarbons; ii. the second reactor comprising a high-temperature adiabatic reactor for synthesizing aromatic and aliphatic hydrocarbons from the aliphatic hydrocarbons formed in the first reactor; c. the separation unit comprising an outlet for hydrogen-containing gas separated by the separation unit, wherein the outlet is in fluid communication with the synthesis gas, whereby hydrogen-containing gas is capable of being recycled.

49. The system of claim 48, comprising an external heat carrier circuit connected to a methanol evaporator, wherein the methanol evaporator is positioned between and in fluid communication with the methanol unit and the first reactor.

50. The system of claim 48, wherein the concentrate of aromatic hydrocarbons units comprises a flow heater having an inlet and an outlet, wherein the inlet is in fluid communication with the first reactor, and the outlet is in fluid communication with the second reactor, wherein the flow heater is capable of initializing a conversion process of aliphatic carbohydrates, wherein the temperature of a flow at the heater outlet is at least 30 C. higher than the maximum temperature in a reaction zone of the first reactor.

51. The system of claim 48, wherein an outlet of the stabilization unit is in fluid communication with the concentrate of aromatics unit; whereby light aliphatic hydrocarbons can be discharged to to a reaction zone of the first reactor for synthesizing aromatic and aliphatic hydrocarbons, to a reaction zone of the second reactor for synthesizing aromatic and aliphatic hydrocarbons, or both.

Description

A SHORT DESCRIPTION OF THE DRAWINGS

[0059] The other distinguishing features and advantages of the invention clearly follow from the description given above as a form of illustration and are not limiting with references to the attached drawings in which:

[0060] FIG. 1 is a schematic perspective view of the processing unit for producing aromatic hydrocarbons from natural gas, according to the invention, and

[0061] FIG. 2 schematically shows the steps of the method for producing aromatic hydrocarbons from natural gas, according to the invention.

[0062] According to FIG. 1, the processing unit for producing a concentrate of aromatic hydrocarbons from natural gas includes the following consecutively connected elements: a unit (1) for producing synthesis gas, a unit (2) for producing methanol, a unit (3) producing a concentrate of aromatic hydrocarbons and a unit (4) for separating the conversion product into reaction water, discharge hydrogen-containing gas, a fraction of light aliphatic hydrocarbons, and a stable concentrate of aromatic hydrocarbons, which is connected to the unit (1) for producing synthesis gas and the unit (3) for producing a concentrate of aromatic hydrocarbons.

[0063] The unit (3) for producing a concentrate of aromatic hydrocarbons comprises two consecutively-connected reactors for synthesizing aromatic hydrocarbons: a first, low-temperature isothermal reactor (31) for synthesizing aromatic and aliphatic hydrocarbons, and a second, high-temperature adiabatic reactor (32) for synthesizing aromatic and aliphatic hydrocarbons from aliphatic hydrocarbons formed in the first reactor (31).

[0064] The unit (4) for separating the conversion product into reaction water, discharge hydrogen-containing gas, a fraction of light aliphatic hydrocarbons, and a stable concentrate of aromatic hydrocarbons comprises a unit (41) for condensing the hydrocarbons and reaction water, disposing of the waste water and separating out the hydrogen-containing gas and unstabilized concentrate of aromatic hydrocarbons, and a unit (42) for stabilizing the concentrate of aromatic hydrocarbons (connected by line (63) to unit (41)).

[0065] The unit (3) for producing a concentrate of aromatic hydrocarbons additionally comprises a recuperative evaporator (33) for recovering the methanol obtained in the methanol synthesis reactor (2) and a recuperative heater (not shown on FIG. 1) for the crude methanol vapors of the reaction medium from unit (32), which is situated on line (58) between the crude methanol evaporator (33) and the first, low-temperature synthesis reactor (31).

[0066] The first, low-temperature isothermal reactor (31) for synthesizing aromatic and aliphatic hydrocarbons additionally comprises a circuit (34) with an external heat carrier connected to the methanol evaporator (33) mounted between the methanol synthesis unit (2) and the first, low-temperature isothermal reactor (31) for synthesizing aromatic and aliphatic hydrocarbons.

[0067] The unit (3) for producing a concentrate of aromatic hydrocarbons additionally comprises an additional flow heater (positioned on the line 59) which is needed to initialize the conversion process of propane and other aliphatic hydrocarbons in the conversion product (not shown in FIG. 1).

[0068] The outlet of the unit (42) (line 65) for stabilizing the concentrate of aromatic hydrocarbons, through which the light aliphatic hydrocarbons are discharged, is connected to the reaction zone of the first low-temperature isothermal reactor (31) for synthesizing aromatic and aliphatic hydrocarbons (line 68) and/or to the reaction zone of the second high-temperature adiabatic reactor (32) for synthesizing aromatic and aliphatic hydrocarbons (line 67).

[0069] The unit (1) for producing the synthesis gas consists of an autothermal reforming unit (12) with an adiabatic pre-reforming unit (11) and a heat recovery unit (13). These are found on lines (52), (53), (54) and (56).

[0070] The adiabatic pre-reforming unit (11) is an adiabatic reactor in which processes of destructive hydrogenation and steam conversion of hydrocarbons C.sub.2+ occur to form thermally stable compounds C.sub.1, CO, and CO.sub.2, which makes it possible to increase the heating temperature of the steam-gas mixture before feeding same to the autothermal reforming unit (12), and to reduce the steam/carbon ratio in the steam-gas mixture. A mixture composed of natural gas (fed along line (51)), hydrogen-containing gas (fed along line (66)) and superheated steam (fed along line (70)) is fed to the inlet of unit (11). Before being fed to unit (11), the mixture is superheated to a temperature of 300-450 C.

[0071] The autothermal reforming unit (12) is a separate apparatus which blows oxygen along line (61). The main advantage of autothermal reforming is to exclude the step of tubular steam conversion and the possibility of operating with a very low steam/carbon ratio. This enables the production of crude methanol with a methanol concentration of at least 94%, which is suitable for converting into a concentrate of aromatic hydrocarbons without a concentration step. In addition, the lack of hydrogen (in a ratio required for synthesizing methanol) in synthesis gas produced by autothermal reforming is fully compensated by the addition, to the raw material to be converted, of hydrogen-containing discharge gas from the synthesis of the concentrate of aromatic hydrocarbons, and also, when necessary, by the addition, to the synthesis gas (line (56)) of hydrogen removed from the discharge gases from synthesizing methanol (line (69)).

[0072] Recycling hydrogen-containing gas from the conversion product separating unit (41) makes it possible to increase the function:

f=(the MF of H.sub.2 the MF of CO.sub.2)/(the MF of CO+the MF of CO.sub.2)

from 1.7-1.9 to the required 2.05-2.1 with a low steam/carbon ratio which reduces the amount of energy lost and the size of the heat exchangers used.

[0073] The hydrogen-containing gas is blown from the methanol synthesis unit (2) through line (69).

[0074] Water is fed from the conversion product separating unit (41) through line (62) to the heat recovery unit (13). The superheated steam is drawn from the heat recovery unit (13) along line (55).

[0075] The superheated steam is fed along line (70) for the production of the steam and gas mixture to be fed to unit (11).

Implementation of the Invention

[0076] According to the invention, aromatic hydrocarbons are produced from natural gas in the following manner.

Step A1. The Production of Synthesis Gas.

[0077] Natural gas (denoted as NG in FIG. 1) is fed to a synthesis gas production unit (1) along lines (51) and (52). In order to produce synthesis gas with the stoichiometric ratio between H.sub.2, CO and CO.sub.2 required for methanol synthesis, a scheme for producing synthesis gas is used in a process of autothermal reforming or oxygen blowing, in which oxygen is used for the partial and complete oxidation of the carbon in natural gas, wherein, as is known, during the conversion of natural gas by said gases, it is possible to obtain synthesis gas with the stoichiometric ratio:

f=(the MF of H.sub.2 the MF of CO.sub.2)/(the MF of CO+the MF of CO.sub.2) less than 1.8, and

synthesizing methanol through a circulation scheme requires synthesis gas with f2.05.

[0078] Due to the fact that hydrogen-containing gas (denoted in FIG. 1 as HRG) is additionally fed to the unit for producing synthesis gas from the step for synthesizing the concentrate of aromatic hydrocarbons from unit (4) along line (66), synthesis gas with the required stoichiometric ratio f 2.05 would be at the outlet of the unit for producing synthesis gas (1), wherein the discharge hydrogen-containing gas from the synthesis of the concentrate of aromatic hydrocarbons is fully recycled, which increases the thermal efficiency coefficient of the integrated process.

[0079] Since a steam reformer is not used to correct the composition of the synthesis gas, the content of CO.sub.2 in the synthesis gas is small, which enables the production of crude methanol with a concentration of at least 94 wt. %, which makes it possible to eliminate the step of concentrating the crude methanol.

Step A2. Synthesizing Methanol

[0080] Afterwards the synthesis gas is fed along line (56) to the methanol synthesis unit (2) where same is converted to crude methanol and discharge synthesis gases which are not shown in the figure and is sent to the methanol evaporator (33) along line (57).

Step A3. Synthesizing the Concentrate of Aromatic Hydrocarbons

[0081] The crude methanol from the methanol synthesizing unit (2) enters lines (57), (58), (59) and (60) of unit (3) for synthesizing the concentrate of aromatic hydrocarbons, which is composed of units for evaporating methanol (33), a recuperative heater for the crude methanol vapors (not shown in FIG. 1), the first, low-temperature isothermal reactor (31) for the synthesis of aromatic and aliphatic hydrocarbons, and an additional heater for the conversion product which initiates the conversion of propane and other aliphatic hydrocarbons in the second, high-temperature adiabatic reactor (32) of crude methanol (not shown in FIG. 1) and the second, high-temperature adiabatic reactor (32) for the synthesis of aromatic and aliphatic hydrocarbons from the aliphatic hydrocarbons formed in the first reactor (31).

[0082] In addition, the temperature in the first reactor is kept within the range 450+/30 C., and in the second reactor the temperature is kept within the range 500+/50 C. The pressure in reactors (31) and (32) is from 0.7 to 3 MPa.

Step A4. Heat Removal

[0083] Heat is removed from reactor (31) by evaporating methanol in unit (33), and due to the presence of the circuit (34). It is not possible to directly use a methanol evaporator because the critical temperature for methanol is 242 C. An intermediate heat carrier is used for heat removal, the composition of which depends on the type of reactor equipment used in unit (31). Thus, when using a tube reactor cooled by a liquid medium, the heat carrier can be a high-temperature heat carrier based on, for example, dialkylbenzenes or heat carriers based on silicon compounds, molten salts, etc. Furthermore, some of the heat is removed from the heat carrier in the methanol evaporation unit (33).

[0084] When using a tube reactor of a eutectic composition to be cooled by a lead-bismuth alloy, heat exchange takes place due to the convective motion of the melt between the reaction tubes and the tubular methanol evaporator.

[0085] When using a reactor with an immovable catalyst layer with heat removal using heat tubes, both sodium and heat resistant hydrocarbons can be used as an intermediate heat carrier.

[0086] Methanol in a gaseous state can also be used as an intermediate heat carrier.

[0087] The circuit for circulating the intermediate heat carrier is denoted by a dotted line in the scheme and by the number 34.

[0088] Converting methanol into a concentrate of aromatic hydrocarbons results in the formation of aliphatic hydrocarbons C.sub.2+ in addition to said aromatic hydrocarbons, wherein a portion of said aliphatic hydrocarbons C.sub.2+ (propane) is converted to aromatic hydrocarbons at high temperatures. In order to convert same, the steam-gas mixture of reactor unit (31) is heated to a temperature of 480-530 C. and fed to reactor (32).

Step A5. Removing Water and Hydrogen-Containing Gas

[0089] Afterwards, the mixture from the reactor (32) is fed along line (60) to the unit (41) for separating the conversion product, where the reaction water from the discharge gases is condensed and removed through line (62), hydrogen-containing gas is removed through line (66) and the concentrate of aromatic hydrocarbons is removed through line (63), which enters the stabilization unit (42).

[0090] The reaction water to be condensed and separated in the conversion product separation unit (41) is fed to a heat recovery boiler (13). The reaction water is recycled in this manner.

[0091] The additional two-stage conversion in reactors (31) and (32) and the reduced temperature in reactor (31) make it possible to reduce the methanol conversion to carbon oxides, which makes it possible to use the discharge hydrogen-containing gas without removing CO.sub.2 therefrom to hydrogenate the sulfur-containing compounds in natural gas, thereby improving the functional of synthesis gas to the optimal values. Hydrogen-containing gas contains very little CO or CO.sub.2, which partially methanate sulfur-containing compounds on a hydrogenating catalyst, which leads to the formation of steam that reduces the chemisorption ability of zinc oxide or iron oxide.

Step A6. Stabilizing the Concentrate of Aromatic Hydrocarbons

[0092] The concentrate of aromatic hydrocarbons is fed through line (63) from the unit (41) for separating the conversion product to a stabilization unit (42), where the gases from the stabilization of the concentrate of aromatic hydrocarbons are also used to convert to a concentrate of aromatic hydrocarbons, wherein said gases are sent through lines (65), (67) and (65), (68) to reactors (31) and (32). The product (denoted in FIG. 1 as Product) is discharged through line (64).

[0093] The sequence of steps is an example and makes it possible to rearrange, add or produce various operations at the same time without losing the ability to produce a concentrate of aromatic hydrocarbons from natural gas.

INDUSTRIAL APPLICABILITY

[0094] The proposed processing unit for producing a concentrate of aromatic hydrocarbons from natural gas can be implemented by a person skilled in the art in practice, and when implemented, provides for the execution of the claimed purpose, which makes it possible to conclude that the invention satisfies the criterion of industrial applicability.

[0095] According to the proposed invention, calculations were made concerning the method for operating the processing unit for producing a concentrate of aromatic hydrocarbons from natural gas.

[0096] The calculations are shown below. [0097] Recycling hydrogen-containing gas in the pre-reforming stage makes it possible to raise the heat efficiency coefficient to 65%, which is a much higher than during conversion without recycling the hydrogen-containing gas, in which case the coefficient is 35-40%. Therefore, integrating the processes makes it possible to raise the heat efficiency coefficient by no less than 20%, which makes it possible to increase the yield by at least 40-50% of hydrocarbon raw material as a result of the conversion. [0098] Recycling reduces the steam/carbon ratio (because of the presence of H.sub.2 as well as H.sub.2O in the mixture to be converted, both of which hinder the formation of soot in reactors). [0099] The scheme of the processing unit is simplified, wherein there is no need to mount an additional steam reformer or to use other schemes for correcting the composition of synthesis gas. [0100] There is no need in the additional processing unit to separate hydrogen from hydrogen rich gas for the hydrogenation of sulfur-containing compounds in the desulfurization stage because the discharge gases from the synthesis of the concentrate of aromatic hydrocarbons can be used for this purpose. Gases with a high olefin content are hydrogenated at the hydrogenation step to H.sub.2S. [0101] The production yield of the concentrate of aromatic hydrocarbons is increased. [0102] It is possible to synthesize highly concentrated crude methanol, which makes it possible to eliminate the step of concentrating same.

[0103] Additional Technical Result: [0104] to increase the content of methylbenzenes including xylenes because, together with aromatization, a reaction occurs and the benzene rings undergo alkylation using methanol.

[0105] Thus, this invention solves the problem of interest which is to increase efficiency in the production of concentrates of aromatic hydrocarbons.

EXAMPLES

[0106] A mixture of desulfurized natural gas and discharge hydrogen-containing gas from the unit for synthesizing a concentrate of aromatic hydrocarbons from methanol is fed to the inlet of the unit for producing synthesis gas and recovering heat. The mixture is hydrogenated to remove the olefins and then mixed with superheated steam and heated to a temperature of 450-650 C. and fed to the autothermal reforming reactor (11). (T 950 C., P 2-3 MPa). The steam-gas mixture from the reforming reactor (12) outlet is cooled and the condensed water therefrom is separated.

[0107] The unit for producing hydrogen from the discharge hydrogen-containing gas from the methanol synthesis: This unit can be composed of a processing unit for concentrating hydrogen which functions according to the principle of short-cycle absorption. The degree of extraction of hydrogen from the hydrogen-containing gas is 60%.

[0108] The crude methanol is synthesized along a circulation scheme from a compressed mixture of synthesis gas obtained in unit 1 with the addition of hydrogen obtained in the unit for producing hydrogen from discharge hydrogen-containing gas from synthesizing methanol.

[0109] The unit for synthesizing a concentrate of aromatic hydrocarbons from crude methanol.

[0110] The Unit for Producing Synthesis Gas by Means of the Technique of Autothermal Reforming and Heat Recycling.

[0111] Raw material (thousands of metric tons per year).

TABLE-US-00001 Natural gas with methane equivalent 1.03 1000 The discharge hydrogen-containing gas from 378 synthesizing the concentrate of aromatic hydrocarbons Water (steam) 800 Oxygen 99.5% 1314 Total: 3491 Produced: Synthesis gas 2834 Condensed water 657 Total: 3491

[0112] The Unit for Producing Hydrogen from Discharge Gases from Synthesizing Methanol

[0113] Raw ingredient:

TABLE-US-00002 Discharge gas from synthesizing methanol (H.sub.2 55 vol. %) 356 Produced: Fuel gas from the unit for separating hydrogen 336 99% hydrogen from the discharge gases from synthesizing 20 methanol with extraction of 60% of the hydrogen Total: 356

[0114] The Unit for Synthesizing Crude Methanol (Circulation/Purge Ratio=20)

TABLE-US-00003 Raw material: Synthesis gas 2834 99% hydrogen 20 Produced: 2854 Crude methanol 94.5% 2498 Discharge hydrogen-containing gas 356 Total: 2854

[0115] The Units for Synthesizing the Concentrate of Aromatic Hydrocarbons and for Separating the Conversion Product.

TABLE-US-00004 Raw material: Crude methanol, 94.5 wt. % 2498 Produced: Stabilized product (arene concentrate) Reid vapor pressure of 70 kPa 663 Reaction water, with 1.6 wt. % methanol 1457 Discharge hydrogen-containing gas 378 Total: 2498

[0116] The Composition of Stabilized Product (Concentrate of Aromatic Hydrocarbons)

TABLE-US-00005 Methanol 0.04% Aliphatic compounds 2.64% Benzene 8.69% Toluene 35.69% Aromatic hydrocarbons C.sub.8+ 40.10% Aromatic hydrocarbons C.sub.9+ 12.84% Total: 100.00%