Method of producing aromatic hydrocarbons from natural gas and apparatus therefor

FIELD: chemistry.

SUBSTANCE: method includes producing synthesis gas, converting the synthesis gas into methanol, producing a concentrate of aromatic hydrocarbons and water from the methanol in the presence of a catalyst, separating the water, blowing off hydrocarbon residues from the water, separating the formed concentrate of aromatic hydrocarbons and a hydrogen-containing gas, which is at least partially used when producing synthesis gas, to change the ratio H2:CO=1.8-2.3:1 therein. The production of aromatic hydrocarbons from methanol in the presence of a catalyst is carried out in two series-connected aromatic hydrocarbon synthesis reactors - a first low-temperature isothermic aromatic and aliphatic hydrocarbon synthesis reactor and a second high-temperature adiabatic reactor for synthesis of aromatic and aliphatic hydrocarbons from the aliphatic hydrocarbons formed in the first reactor and subsequent stabilisation in a unit for stabilising the concentrate of aromatic hydrocarbons. At least part of the hydrogen-containing gas is fed into a synthesis gas production unit and used to obtain synthesis gas using an autothermal reforming technique with a pre-reforming or non-catalytic partial oxidation unit using oxygen or oxygen-air mixtures as the oxidising agent to change the ratio according to the relationship (m.f.H2-m.f.CO2)/(m.f.CO+m.f.CO2)≥2, where m.f. is the molar fraction of a component in synthesis gas. The invention also relates to an apparatus.

EFFECT: high efficiency of producing concentrates of aromatic hydrocarbons.

12 cl, 2 dwg, 1 ex

 

The technical field to which the invention relates

The invention relates to the field of petrochemicals, and more particularly to methods and devices for obtaining aromatic hydrocarbons from natural gas, which receive the synthesis gas, produced his conversion to methanol, produce further from methanol in the presence of a catalyst concentrate of aromatic hydrocarbons and water, produced water separation, produce blow-off water from hydrocarbons, produce the allocation of the resulting concentrate of aromatic hydrocarbons and hydrogen-containing gas, which is at least partly used in the production of synthesis gas, to change the ratio of N2:FROM 1.8 to 2.3:1, and can be used to produce aromatic hydrocarbons.

Note that here and below we mean by methanol and a mixture of methanol and dimethyl ether as dimethyl ether will still be formed in the reactor and the synthesis is not only from methanol, but also from dimethyl ether.

Aromatic hydrocarbons, especially benzene, toluene, ethylbenzene and xylenes, are important chemical products of mass production in the petrochemical industry. Currently aromatic compounds most often receive a variety of methods from factory�x materials based on crude oil, including catalytic reforming and cracking. However, as global supplies of raw materials on the basis of crude oil decreases, there is a growing need to find alternative sources of aromatic hydrocarbons.

One possible alternative source for aromatic hydrocarbons is methane, which is the main component of natural gas and biogas. Because of the problems associated with transporting large volumes of natural gas, the majority of the natural gas produced along with oil, especially in remote locations, flared. Consequently, a particularly attractive method of increasing the grade natural gas is the conversion of alkanes contained in natural gas, directly into higher molecular weight hydrocarbons, such as aromatic compounds, provided that can be overcome with the attendant technical difficulties.

A significant part of the methods of conversion of methane to liquid hydrocarbons comprises first conversion of methane into synthesis gas, a mixture of hydrogen and carbon oxides (CO and/or CO2). The production of synthesis gas due to the high capital costs and is energy intensive. However, a particularly attractive means of obtaining aromatic compounds, in which at the same time can be �of alocen the synthesis gas, since the synthesis gas may have a high value. The synthesis gas has a high potential value, as it may enter into a subsequent reaction with the formation of methanol, higher alcohols, acetic acid, ammonia, acetone, acetaldehyde, ethylene oxide, ethylene glycol, dimethyl ether, gasoline linear alkanes and/or alkenes. The products from such a wide range is preferable, because these chemicals have a higher value than methane, and they are easier to transport for sale.

The prior art method

According to the first one of its sides, the present invention relates to a method of producing a concentrate of aromatic hydrocarbons from natural gas, which are the synthesis gas, produced his conversion to methanol, produce further from methanol in the presence of a catalyst concentrate of aromatic hydrocarbons and water, produced water separation, produce blow-off water from hydrocarbons, produce the allocation of the resulting concentrate of aromatic hydrocarbons and hydrogen-containing gas, which is at least partly used in the production of synthesis gas, to change the ratio of N2:FROM 1.8 to 2.3:1.

This method is described in the patent of the Russian Federation for the invention №2362760, published in 2009

This method is the most�e closest to the technical essence and achieved technical result is selected as the prototype of the present invention.

The disadvantage of this prototype is small, the efficiency of producing concentrates of aromatic hydrocarbons. This is due to the fact that a large number of substances out in by-products.

Disclosure of the invention as a way

Based on this original observation, the present invention mainly aims to provide a method for obtaining aromatic hydrocarbons from natural gas, allowing, at least, to smooth at least one of the above disadvantages.

To achieve this goal, the production of aromatic hydrocarbons from methanol in the presence of a catalyst produced in two serially connected reactors synthesis of aromatic hydrocarbons, the first low-temperature isothermal reactor synthesis of aromatic and aliphatic hydrocarbons and the second high-temperature adiabatic reactor synthesis of aromatic and aliphatic hydrocarbons formed from the first reactor aliphatic hydrocarbons and subsequent stabilization in the stabilization unit concentrate of aromatic hydrocarbons. At least a portion of hydrogen-containing gas is used for producing synthesis gas using technology autothermal reforming unit prereforming or nekataliticheskogo partial okelani� using as the oxidizing agent oxygen or oxygen-air mixtures to change the ratio according to the relation (M. D. H 2-M. D. CO2)/(MD CO+MD CO2)≥2, where MD is the molar fraction of the component in the synthesis gas.

Thanks to this favorable characteristic becomes possible to increase the efficiency of producing concentrates of aromatic hydrocarbons due to the fact that aliphatic hydrocarbons, obtained in the first reactor synthesis of aromatic hydrocarbons, optionally processed and in the second reactor synthesis of aromatic and aliphatic hydrocarbons, and the processing is at a higher temperature. And due to the fact that a part of the hydrogen-containing gas is used to produce synthesis gas, it becomes possible to increase the yield of methanol as an intermediate raw material and thus yield of aromatic hydrocarbons.

There is a variant of the invention in which thermal stabilization reaction zone of the first reactor synthesis of aromatic and aliphatic hydrocarbons is carried out by heating by an external agent, wherein the removal of heat from the external agent is carried out by evaporation of the methanol in the methanol evaporator installed between the block of methanol synthesis and the first low-temperature isothermal reactor synthesis of aromatic and aliphatic hydrocarbons.

Thanks to this favorable characteristic appears the cooling potential of the first low�isothermal reactor temperature synthesis of aromatic and aliphatic hydrocarbons.

There is a variant of the invention in which the discharge from a convertible product in the separation unit of the product of the conversion of light aliphatic hydrocarbons at least partially served in the reaction zone of the first low-temperature isothermal reactor synthesis of aromatic and aliphatic hydrocarbons and/or in the reaction zone of the second high-temperature adiabatic reactor synthesis of aromatic and aliphatic hydrocarbons, which ensures an increase in the yield of the concentrate of aromatic hydrocarbons.

Thanks to this favorable characteristic appears possible to further increase the useful output of a concentrate of aromatic hydrocarbons, as thus possible to reduce the amount of discharge from the flue gases of light aliphatic hydrocarbons at the expense of their recycling.

There is a variant of the invention in which the catalyst of the first low-temperature isothermal reactor synthesis of aromatic and aliphatic hydrocarbons using a catalyst based on crystalline aluminosilicate type pentasil with SiO2/Al2O3=25-100 containing 0.05-0.1 wt. percent sodium oxide, in which additionally include oxides of zinc, oxides of rare earth elements and a binder component, with the following ratio of components, wt. %:

Zinc oxide0,5-3,0The oxides of rare earth elementsof 0.1-5.0Cobalt oxide0,05-2,5Crystalline aluminosilicate63-70Binderelse

Thanks to this favorable characteristic becomes possible to enhance the performance properties of the catalyst, namely increasing the mechanical strength of granules and its ability to oxidative regeneration.

There is a variant of the invention in which the catalyst of the second high-temperature adiabatic reactor synthesis of aromatic and aliphatic hydrocarbons using a catalyst based on crystalline aluminosilicate type pentasil with SiO2/Al2O3=25-120 containing 0.05-0.1 wt. percent sodium oxide, in which additionally include oxides of zinc, oxides of sodium, oxides of rare earth elements and a binder component, with the following ratio of components, wt. %:

td align="right"> of 0.12 and 0.30
Zinc oxide0,5-3,0
Sodium oxide
The oxides of rare earth elements0,1-3,0
Cobalt oxide0,05-2,5
Crystalline aluminosilicate63,0 of 70.0
Binderelse

and as rare earth oxides composition is used:

Cerium oxide CeO23,0
Lanthanum oxide La2O365,0
Neodymium oxide Nd2O321,0
The oxide of praseodymium Pr6O11else

Thanks to this favorable characteristic becomes possible to enhance the performance properties of the catalyst, namely increasing the mechanical strength of granules and increasing the ability of the catalyst to an oxidative regeneration.

There is a variant of the invention, which is obtained during the synthesis and separation of a concentrate of aromatic hydrocarbons, the hydrogen-containing gas optionally used in the process of hydraulic�of sulfur-containing compounds, removed preferably by stage hydrogenation to hydrogen sulfide.

Thanks to this favorable characteristic becomes possible to recycle the hydrogen-containing gas obtained in the separation unit of the product of the conversion in the hydrogenation of sulfur-containing compounds.

There is a variant of the invention, which together with the hydrogenation of sulfur-containing compounds to hydrogen sulfide in a single reactor and produce the hydrogenation of the olefins contained in the obtained hydrogen-containing gas that prevents the formation of carbonaceous deposits on the surface of the chemisorbent of hydrogen sulfide on the catalyst surface of prereforming used to stabilize the component composition and reduce the ratio of steam/carbon in a convertible in the synthesis gas vapor mixture.

Thanks to this favorable characteristic there is a possibility of preventing the formation of carbonaceous deposits on the surface of the chemisorbent of hydrogen sulfide on the catalyst surface of prereforming, and the ability to stabilize the component composition and reduce the ratio of steam/carbon in a convertible in the synthesis gas vapor mixture.

The set of essential features of the present invention is unknown in the art for methods similar to�about the destination, that allows to make a conclusion on compliance with the criterion of "novelty" for the invention as a method.

The prior art installation

Another aspect of the present invention relates to apparatus for producing a concentrate of aromatic hydrocarbons from natural gas, including unit connected in series for producing synthesis gas unit for producing methanol, block of producing a concentrate of aromatic hydrocarbons and the separation unit of the product of the conversion reaction on water, hydrogen-containing exhaust gas, the fraction of light aliphatic hydrocarbons and stable concentrate of aromatic hydrocarbons, connected to a unit for producing synthesis gas.

This setup is described in the patent of the Russian Federation for the invention №2362760, published in 2009

This installation is the closest to the technical essence and achieved technical result is selected as the prototype of the present invention as a device.

The disadvantage of this prototype is its low efficiency for producing concentrates of aromatic hydrocarbons. This is due to the fact that a large number of substances out in by-products.

Disclosure of the invention as installation

The present invention mainly aims to propose an installation for producing a concentrate of aromatic uglevodorov�s from natural gas, includes unit connected in series for producing synthesis gas unit for producing methanol, block of producing a concentrate of aromatic hydrocarbons and the separation unit of the product of the conversion reaction on water, hydrogen-containing exhaust gas, the fraction of light aliphatic hydrocarbons and thus concentrate of aromatic hydrocarbons, connected to a unit for producing synthesis gas and with the unit for aromatic hydrocarbons, allowing, at least, to smooth at least one of the above disadvantages.

To achieve this, the block of producing a concentrate of aromatic hydrocarbons includes two series-connected reactor synthesis of aromatic hydrocarbons - the first low-temperature isothermal reactor synthesis of aromatic and aliphatic hydrocarbons and the second high-temperature adiabatic reactor synthesis of aromatic and aliphatic hydrocarbons formed from the first reactor aliphatic hydrocarbons. The plant comprises a stabilization unit concentrate of aromatic hydrocarbons. The hydrogen-containing output gas separation unit of product conversion connected to the input unit for producing synthesis gas.

Thanks to this favorable characteristic becomes possible to increase the efficiency of obtaining concentrationsa hydrocarbons by what aliphatic hydrocarbons, obtained in the first reactor synthesis of aromatic hydrocarbons optionally processed and in the second reactor synthesis of aromatic and aliphatic hydrocarbons, and the processing is at a higher temperature.

There is a variant of the invention in which the unit of producing a concentrate of aromatic hydrocarbons further includes a regenerative heater vapor crude methanol obtained in the methanol synthesis reactor (figure not shown).

Thanks to this favorable characteristic becomes possible to remove heat from the products of conversion from the second high-temperature synthesis reactor aromatic and aliphatic hydrocarbons using this heat to superheat the vapors of methanol at the outlet of the evaporator of methanol.

There is a variant of the invention, in which the first low-temperature isothermal reactor synthesis of aromatic and aliphatic hydrocarbons further comprises a circuit with an external coolant, connected to the evaporator of methanol established between the unit for methanol synthesis and the first low-temperature isothermal reactor synthesis of aromatic and aliphatic hydrocarbons.

Thanks to this favorable characteristic becomes possible to remove heat from the first men, and� low-temperature isothermal reactor synthesis of aromatic and aliphatic hydrocarbons at the expense of circuit with external coolant using this heat for the evaporation of methanol.

There is a variant of the invention in which the unit of producing a concentrate of aromatic hydrocarbons optionally includes an additional heater flow that is required to initiate the conversion of propane other aliphatic carbohydrates in the product of the conversion of the temperature of the flow at the outlet of the heater by at least 30°C higher than the maximum temperature in the reaction zone of the first reactor

Thanks to this favorable characteristic enables the initialization process of the conversion of propane and other aliphatic carbohydrates in the conversion.

There is a variant of the invention in which the output of the separation unit of the product of conversion at which the yield of light aliphatic hydrocarbons, is connected with the reaction zone of the first low-temperature isothermal reactor synthesis of aromatic and aliphatic hydrocarbons and/or with the reaction zone of the second high-temperature adiabatic reactor synthesis of aromatic and aliphatic hydrocarbons.

Thanks to this favorable characteristic appears possible to further increase the useful output of a concentrate of aromatic hydrocarbons, as thus possible to reduce the amount of discharge from the flue gases of light aliphatic hydrocarbons with for�et re-processing.

Thus, in the present invention, the task is to ensure the efficiency of producing concentrates of aromatic hydrocarbons. The task is solved with the above characteristics.

The set of essential features of the present invention is unknown in the art for devices of similar purpose, allowing to conclude that conforms to the criterion "novelty" for the invention as installed.

Brief description of the drawings

Other distinctive features and advantages of the invention clearly emerge from the description given below for illustration only and are not restrictive, with reference to the accompanying drawings, in which:

- figure 1 schematically shows a General view of the apparatus for producing aromatic hydrocarbons from natural gas according to the invention,

- figure 2 schematically depicts the steps of the method for obtaining aromatic hydrocarbons from natural gas according to the invention.

According to the figure 1 installation for producing a concentrate of aromatic hydrocarbons from natural gas includes connected in series unit 1 for producing synthesis gas unit 2 for producing methanol, block 3 of producing a concentrate of aromatic hydrocarbons and the separation unit 4 product conversion reaction water, waste hydrogen�containing gas, the fraction of light aliphatic hydrocarbons and stable concentrate of aromatic hydrocarbons, coupled to the receiving unit 1 of the synthesis gas and the receiving unit 3 of the concentrate of aromatic hydrocarbons.

Unit 3 to obtain a concentrate of aromatic hydrocarbons includes two series-connected reactor synthesis of aromatic hydrocarbons - the first low-temperature isothermal reactor 31 synthesis of aromatic and aliphatic hydrocarbons and the second high-temperature adiabatic reactor 32 synthesis of aromatic and aliphatic hydrocarbons formed from the first reactor 31 aliphatic hydrocarbons.

Unit 4 product separation conversion of the reaction water, hydrogen-containing exhaust gas, the fraction of light aliphatic hydrocarbons and stable concentrate of aromatic hydrocarbons contains block 41 condensation of hydrocarbons and reaction water, wastewater and separating a hydrogen-containing gas and volatile concentrate of aromatic hydrocarbons and the block 42 of the stabilized concentrate of aromatic hydrocarbons (connected by line 63 to block 41).

Block of producing a concentrate of aromatic hydrocarbons 3 further includes a regenerative evaporator 33 of methanol obtained in the methanol synthesis reactor 2, and recuperative�th heater (figure 1 not shown) vapor crude methanol reaction medium from the block 32, located on highway 58, between the evaporator 33 of crude methanol and the first low-temperature synthesis reactor 31.

The first low-temperature isothermal reactor 31 synthesis of aromatic and aliphatic hydrocarbons further comprises a circuit 34 with an external coolant, connected to the methanol evaporator 33 installed between the block methanol synthesis 2 and the first low-temperature isothermal reactor 31 synthesis of aromatic and aliphatic hydrocarbons.

Unit 3 to obtain a concentrate of aromatic hydrocarbons optionally includes an additional heater flow that is required to initiate the conversion of propane other aliphatic carbohydrates in the product conversion (figure 1, not shown).

The output of block 42 (highway 65) stabilization of a concentrate of aromatic hydrocarbons at which the yield of light aliphatic hydrocarbons, is connected with the reaction zone of the first low-temperature isothermal reactor 31 synthesis of aromatic and aliphatic hydrocarbons (highway 68) and/or with the reaction zone of the second high-temperature adiabatic reactor 32 synthesis of aromatic and aliphatic hydrocarbons (highway 67).

Unit 1 for producing synthesis gas consists of unit autothermal reforming unit 12 unit adiabat�ical prereforming 11 and the heat recovery unit 13. They are on the highway 52, 53, 54, 56.

Block adiabatic prereforming 11 is an adiabatic reactor in which the destructive hydrogenation processes and steam reforming of hydrocarbons With2+ with the formation of thermally stable compounds, C1, CO, CO2that allows to increase the temperature of the heating gas mixture before applying it to the unit autothermal reformer 12 and to reduce the ratio of steam/carbon in the gas-vapor mixture. The input unit 11 is supplied a mixture of natural gas is fed via line 51), a hydrogen-containing gas is fed via line 66) and superheated steam supplied via line 70). Before serving, block 11, the mixture is superheated to a temperature of 300-450°C.

Unit autothermal reformer 12 is a separate unit with the blowing of oxygen, which is produced by highway 61. The main advantage of autothermal reforming stage is an exception tubular steam reforming and the ability to work at very low ratio of steam/carbon, allowing the methanol concentration of the methanol at least 94%, suitable for conversion into a concentrate of aromatic hydrocarbons without the stage-building. The lack of hydrogen in the ratio required for the synthesis of methanol) in the synthesis gas produced by �echnology autothermal reforming, fully compensated by the addition to converted the raw hydrogen-containing off-gases from the synthesis of a concentrate of aromatic hydrocarbons, and, if necessary, and the additive in the synthesis gas (highway 56) emitted from flue gas for methanol synthesis (highway 69) of hydrogen.

The recycle hydrogen-containing gas from the separation unit 41 product conversion allows you to maximize the functionality

f=(m d2-M. D. CO2)/(MD CO+MD CO2)

with 1.7-1.9 required to 2.05-2.1 with a low ratio of steam/carbon, reducing energy losses and metal content.

On highway 69 is a hydrogen-containing purge gas from the block 2 for methanol synthesis.

On route 62 is the water supply unit 41 of separating the product of the conversion of the heat recovery unit 13. And through line 55 is the output of superheated steam from the heat recovery unit 13.

Via line 70 is the supply of superheated steam to obtain a gas mixture supplied to the block 11.

The implementation of the invention

The production of aromatic hydrocarbons from natural gas according to the invention is produced as follows.

Stage A1. The production of synthesis gas

Natural gas is supplied to the block 1 of the syngas via line 51, 52. For producing synthesis gas required for methanol synthesis, stoichiometric rela�achenium between H 2, CO, CO2schema is used for producing synthesis gas autothermal reforming or oxygen injection, in which oxygen is used for full and partial oxidation of the carbon in natural gas, in this case, as you know, when reforming of natural gas, these gases can be obtained synthesis gas with a stoichiometric ratio

f=(m d2-M. D. CO2)/(MD CO+MD CO2) less than 1.8, and for the synthesis of methanol by circulating the scheme required the synthesis gas with f≥2.05.

Due to the fact that any block in the synthesis gas is fed additionally, the hydrogen-containing gas (indicated on figure 1 as VSG) with the stage of synthesis of the concentrate of aromatic hydrocarbons from unit 4 via line 66, the output unit for producing synthesis gas 1 will be the synthesis gas with the desired stoichiometric ratio f≥2.05 completely recycled hydrogen-containing waste gas from the synthesis of a concentrate of aromatic hydrocarbons, which increases thermal efficiency of the integrated process.

As for the correction of the composition of the synthesis gas not used steam reformer, the content of CO2in the synthesis gas will be small, which allows to obtain the methanol with a concentration of not lower than 94 wt.%, it allows to refuse from the stage of strengthening crude methanol.

Stage A2. Synthesis �of ethanol

Further, the synthesis gas is fed via line 56 to block methanol synthesis 2, where it is converted to methanol and exhaust gases from the synthesis, which in the figure is not shown, and fed to the methanol evaporator 33 through line 57.

Stage A3. Synthesis of a concentrate of aromatic hydrocarbons

The crude methanol from the block of methanol synthesis 2 arrives on highway 57, 58, 59, 60 unit 3 synthesis of a concentrate of aromatic hydrocarbons consisting of blocks of methanol evaporator 33, regenerative heater vapors of crude methanol (figure 1, not shown), the first low-temperature isothermal reactor 31 synthesis of aromatic and aliphatic hydrocarbons, additional heater product conversion, initiating the conversion of propane and other aliphatic hydrocarbons in the second high-temperature adiabatic reactor 32 raw (figure 1, not shown) and second high-temperature adiabatic reactor 32 synthesis of aromatic and aliphatic hydrocarbons formed from the first reactor 31 aliphatic hydrocarbons.

The temperature in the first reactor is maintained in the interval 450°+/-30°C, and the second 500°+/-50°C. the pressure in the reactors 31 and 32 from 0.7 to 3 MPa.

Stage A4. Heat removal

Dissipate heat from the reactor 31 through evaporation of methanol in the block 33 and the circuits 34. Since the critical t�mperature methanol 242°C, use the evaporation of methanol directly. To remove heat an intermediate heat transfer fluid is used, the composition of which depends on the type of reactor equipment used in the block 31. So, when using a tubular reactor cooled by liquid medium, it can be high-temperature coolant on the basis of, for example, dialkylphenols, or the carriers based on silicon compounds, molten salts, etc While partial removal of heat from the coolant out the evaporation of methanol, 33.

When using a tubular reactor, cooled by lead-bismuth eutectic alloy composition, heat exchange will be carried out by convective movement of the melt between the reaction tubes and tube evaporator of methanol.

When using a reactor with a fixed bed catalyst with heat using heat pipes as an intermediate medium can be used such as sodium and thermally resistant hydrocarbons.

As an intermediate carrier can also be used and methanol in the gaseous state.

In the diagram, the circuit of the intermediate coolant indicated by the dotted line and denoted by 34.

In the conversion of methanol into a concentrate of aromatic hydrocarbons with aromatic hydrocarbons �prasouda also aliphatic hydrocarbons With 2+, the conversion of which (propane) in aromatic hydrocarbons occurs at higher temperatures. For the conversion of gas-vapor mixture from the reactor unit 31 is heated to a temperature 480-530°C and fed to the reactor 32.

Step A5. Diversion of water and hydrogen-containing gas

The mixture from the reactor 32 serves on highway 60 in block 41 of the separation of product conversion, where it is condensed from the exhaust gases of the reaction water which is discharged through line 62 and is discharged through line 66, the hydrogen-containing gas through line 63 is given a concentrate of aromatic hydrocarbons, which enters the stabilization unit 42.

The reaction water is condensed and separated in the separation unit 41 product conversion is supplied to the waste heat recovery boiler 13. Thus recycle of the reaction water.

Thanks to additional two-stage conversion in the reactors 31 and 32 and a low temperature in the reactor 31 can reduce the conversion of methanol to carbon monoxide, which allows the use of hydrogen-containing flue gas without purification from CO2for the hydrogenation of sulfur compounds in natural gas, which increases the functionality of the synthesis gas to the optimal values. Hydrogen-containing gas contains very little CO and CO2partially metanira on the hydrogenation catalyst with sulfur-containing�of dinani, which leads to the formation of steam, reducing the chemisorption capacity of zinc oxide (iron).

Step A6. The stabilized concentrate of aromatic hydrocarbons

Via line 63 a concentrate of aromatic hydrocarbons from the separation unit 41 product conversion serves on the stabilization unit 42, where the gases stabilize the concentrate of aromatic hydrocarbons are also used for conversion into a concentrate of aromatic hydrocarbons, for which they are on highways 65, 67 and 65, 68 fed to the reactors 31 and 32. The output of the product takes place via line 64.

The sequence of steps is exemplary and allows you to rearrange, add, or to perform certain operations at the same time without losing the ability to ensure the preparation of a concentrate of aromatic hydrocarbons from natural gas.

Industrial applicability

The proposed plant for producing a concentrate of aromatic hydrocarbons from natural gas can be carried out by a specialist in practice and in the implementation provides an implementation of the stated purpose, which allows to conclude that the criterion of "industrial applicability" of the invention.

In accordance with the proposed invention the calculations of the method of operation of an installation for producing a concentrate of aromatic hydrocarbons from natural gas�.

The calculations showed the following.

- Hydrogen-containing recycle gas to the stage of prereforming allows you to raise the coefficient of thermal efficiency up to 65%, which is much higher than when the conversion without hydrogen-containing recycle gas 35-40%.Thus, the integration allows you to raise thermal efficiency of not less than 20%, allowing not less than 40-50% increase in output resulting from the conversion of hydrocarbons.

- Due to the recycling reduces the ratio of steam/carbon (due to the presence in convertible mixture of H2and H2O that prevent the formation of soot in the reactors.

- Simplified scheme of installation - no need to install additional steam reformer or to use other correction circuits of the composition of the synthesis gas.

- No need for additional installation of hydrogen for the hydrogenation of sulfur-containing compounds at the stage of desulfurization, as are the exhaust gases from the synthesis of a concentrate of aromatic hydrocarbons. Gases with a high content of olefins hydronauts on stage hydrogenation to H2S.

- Increased yield - concentrate of aromatic hydrocarbons.

- It is possible to synthesize methanol of high concentration, thereby avoiding the stage of his growing�message.

Additional effect:

- the increase in the content of methylbenzol, including xylenes, due to the fact that together with the aromatization reaction takes place and alkylation with methanol benzene rings.

Thus, in the present invention achieved the objective - improving the efficiency of producing concentrates of aromatic hydrocarbons

Examples

To the input unit for producing synthesis gas and the waste heat is fed a mixture desulfuromonas natural gas and hydrogen-containing off-gas from the synthesis unit of the concentrate of aromatic hydrocarbons from methanol. The mixture hereroense for removal of olefins and after mixed with superheated steam, heated to a temperature of 450-650°C and fed into the reactor autothermal reformer 11. (T≈950°C, P = 2-3 MPa). The gas-vapor mixture from the outlet of the reforming reactor is cooled and separated from the condensing water.

A unit for producing hydrogen from hydrogen-containing exhaust gas from the methanol synthesis. A block can consist of the installation of the concentration of hydrogen, operating on the principle of pressure absorption. The degree of extraction of hydrogen from a hydrogen-containing gas 60%.

The synthesis of the crude methanol is carried out by circulating the scheme of the compressed mixture obtained in block 1 of the synthesis gas with the addition of hydrogen in �loc for producing hydrogen from hydrogen-containing exhaust gas from the methanol synthesis.

Block synthesis of a concentrate of aromatic hydrocarbons from crude methanol.

Unit for producing synthesis gas technology autothermal

reforming and heat recovery.

Raw materials (thousand tons a year)

Natural gas methane equivalent 1.031000
Exhaust wash with the synthesis of a concentrate of aromatic hydrocarbons378
Water (steam)800
Oxygen 99.5%1314
Total:3491

Received:

The synthesis gas2834
Water condensing657
Total:3491

A unit for producing hydrogen from waste gases methanol synthesis

Raw material:

The waste gas from the methanol synthesis (H2- 55% vol.)356

Received:

Fuel gases unit of hydrogen 336
Hydrogen 99% of the flue gas for methanol synthesis
the allocation of 60% hydrogen20
Total:356

Block the synthesis of raw methanol (the ratio of the circulation/air blow-off =20)

Raw material:

The synthesis gas2834
Hydrogen 99%20
Received:2854
The methanol 94.5%2498
Exhaust wash356
Total:2854

Blocks synthesis of a concentrate of aromatic hydrocarbons and separation of the product of the conversion.

Raw material:

The methanol, 94.5% of the mass.2498

Received:

Stable catalysate (concentrate arenes),
pressure Reid vapor pressure 70 kPa 663
The water of the reaction, methanol 1.6% of the mass.1457
Exhaust wash378
Total:2498

The stable composition of the catalysate (concentrate of aromatic hydrocarbons)

Methanol0.04%
Aliphatic compounds2,64%
Benzene8.69%
Toluene35.69%
Aromatic hydrocarbons With8+40.10%
Aromatic hydrocarbons With9+12.84%
Total:100.00%

1. Method of producing a concentrate of aromatic hydrocarbons from natural gas, which are the synthesis gas, produced his conversion to methanol, produce further from methanol in the presence of a catalyst concentrate of aromatic hydrocarbons and water, produced water separation, produce blow-off water from residues ug�of evagorou, make a selection of the resulting concentrate of aromatic hydrocarbons and hydrogen-containing gas, which is at least partly used in the production of synthesis gas, to change the ratio of N2:FROM 1.8 to 2.3:1, characterized in that the extraction of aromatic hydrocarbons from methanol in the presence of a catalyst produced in two serially connected reactors synthesis of aromatic hydrocarbons, the first low-temperature isothermal reactor synthesis of aromatic and aliphatic hydrocarbons and the second high-temperature adiabatic reactor synthesis of aromatic and aliphatic hydrocarbons formed from the first reactor aliphatic hydrocarbons and subsequent stabilization in the stabilization unit concentrate of aromatic hydrocarbons, and that at least a portion of hydrogen-containing gas fed to the unit for producing synthesis gas and is used for producing synthesis gas using technology autothermal reforming unit prereforming or non-catalytic partial oxidation using as the oxidizing agent oxygen or oxygen-air mixtures to change the ratio according to the relation (M. D. H2-M. D. CO2)/(MD CO+MD CO2)≥2, where MD is the molar fraction of the component in the synthesis gas.

2. A method according to claim 1, characterized in that thermal stabilization reaction zone of the first reactor synthesis of aromatic and aliphatic hydrocarbons is carried out by heating by an external agent, wherein the removal of heat from the external agent is carried out by evaporation of the methanol in the methanol evaporator installed between the block of methanol synthesis and the first low-temperature isothermal reactor synthesis of aromatic and aliphatic hydrocarbons.

3. A method according to claim 1, characterized in that the discharge from a convertible product in the separation unit of the product of the conversion of light aliphatic hydrocarbons at least partially served in the reaction zone of the first low-temperature isothermal reactor synthesis of aromatic and aliphatic hydrocarbons and/or in the reaction zone of the second high-temperature adiabatic reactor synthesis of aromatic and aliphatic hydrocarbons, which ensures an increase in the yield of the concentrate of aromatic hydrocarbons.

4. A method according to claim 1, characterized in that the catalyst of the first low-temperature isothermal reactor synthesis of aromatic and aliphatic hydrocarbons using a catalyst based on crystalline aluminosilicate pentasil type with SiO2/Al2O3=25-100 containing 0.05-0.1 wt. percent sodium oxide, in which�th additionally include oxides of zinc, the oxides of rare earth elements and a binder component, with the following ratio of components, wt. %:

Zinc oxide0,5-3,0
The oxides of rare earth elementsof 0.1-5.0
Cobalt oxide0,05-2,5
Crystalline aluminosilicate63-70
Binderelse

5. A method according to claim 1, characterized in that the catalyst of the second high-temperature adiabatic reactor synthesis of aromatic and aliphatic hydrocarbons using a catalyst based on crystalline aluminosilicate pentasil type with SiO2/Al2O3=2-120 containing 0.05-0.1 wt. percent sodium oxide, in which additionally include oxides of zinc, oxides of sodium, oxides of rare earth elements and a binder component, with the following ratio of components, wt. %:

Zinc oxide0,5-3,0
Sodium oxideof 0.12 and 0.30
Oxides redkozemel�x 0,1-3,0
Cobalt oxide0,05-2,5
Crystalline aluminosilicate63,0 of 70.0
Binderthe rest,

and as rare earth oxides composition is used:
Cerium oxide CEO23,0
Lanthanum oxide La2O365,0
Neodymium oxide Nd2O321,0
The oxide of praseodymium Pr6O11else

6. A method according to claim 1, characterized in that obtained during the synthesis and separation of a concentrate of aromatic hydrocarbons, the hydrogen-containing gas optionally used in the process of hydrogenation of sulfur-containing compounds that can be removed preferably by hydrogenation to hydrogen sulfide.

7. A method according to claim 6, characterized in that together with the hydrogenation of sulfur-containing compounds to hydrogen sulfide in a single reactor and produce hydrogenation of olefins that are contained in the resulting hydrogen�containing gas, what prevents the formation of carbonaceous deposits on the surface of the chemisorbent of hydrogen sulfide on the catalyst surface of prereforming, to stabilize the composition and reduce the ratio of steam/carbon in a convertible in the synthesis gas vapor mixture.

8. Installation for producing a concentrate of aromatic hydrocarbons from natural gas, including unit connected in series for producing synthesis gas unit for producing methanol, block of producing a concentrate of aromatic hydrocarbons and the separation unit of the product of the conversion reaction on water, hydrogen-containing exhaust gas, the fraction of light aliphatic hydrocarbons and stable concentrate of aromatic hydrocarbons, connected to a unit for producing synthesis gas, wherein that block of producing a concentrate of aromatic hydrocarbons includes two series-connected reactor synthesis of aromatic hydrocarbons - the first low-temperature isothermal reactor synthesis of aromatic and aliphatic hydrocarbons and the second high-temperature adiabatic reactor synthesis of aromatic and aliphatic hydrocarbons formed from the first reactor aliphatic hydrocarbons, and the fact that the plant comprises a stabilization unit concentrate of aromatic hydrocarbons, item, the hydrogen-containing output gas separation unit of product conversion connected to the input unit for producing synthesis gas.

9. Apparatus according to claim 8, characterized in that the block of producing a concentrate of aromatic hydrocarbons further includes a regenerative heater vapor crude methanol obtained in the methanol synthesis reactor.

10. Apparatus according to claim 8, characterized in that the first low-temperature isothermal reactor synthesis of aromatic and aliphatic hydrocarbons further comprises a circuit with an external coolant, connected to the evaporator of methanol established between the unit for methanol synthesis and the first low-temperature isothermal reactor synthesis of aromatic and aliphatic hydrocarbons.

11. Apparatus according to claim 9, characterized in that the block of producing a concentrate of aromatic hydrocarbons optionally includes an additional heater flow that is required to initiate the conversion of propane other aliphatic carbohydrates in the product conversion, the temperature of the flow at the outlet of the heater by at least 30°C higher than the maximum temperature in the reaction zone of the first reactor.

12. Apparatus according to claim 9, characterized in that the output of the stabilization unit concentrate of aromatic hydrocarbons, in which the origin�odit the yield of light aliphatic hydrocarbons, is connected with the reaction zone of the first low-temperature isothermal reactor synthesis of aromatic and aliphatic hydrocarbons and/or with the reaction zone of the second high-temperature adiabatic reactor synthesis of aromatic and aliphatic hydrocarbons.



 

Same patents:

FIELD: oil and gas industry.

SUBSTANCE: invention relates to a method for obtaining hydrocarbon products, which involves the following stages: (a) provision of synthesis gas containing hydrogen, carbon monoxide and carbon dioxide; (b) reaction of conversion of synthesis gas to an oxygenate mixture containing methanol and dimethyl ester, in presence of one or more catalysts, which simultaneously catalyse the reaction of conversion of hydrogen and carbon monoxide to oxygenates, at pressure of at least 4 MPa; (c) extraction from stage (b) of an oxygenate mixture containing quantities of methanol, dimethyl ester, carbon dioxide and water together with non-reacted synthesis gas, introduction of the whole amount of the oxygenate mixture without any additional treatment to a stage of catalytic conversion of oxygenates (d); (d) reaction of oxygenate mixture in presence of a catalyst, which is active in conversion of oxygenates to higher hydrocarbons; (e) extraction of the outlet flow from stage (d) and separation of the outlet flow into tail gas containing carbon dioxide occurring from synthesis gas and carbon dioxide formed at stage (b), liquid hydrocarbon phase containing the higher hydrocarbons obtained at stage (d) and liquid water phase where the pressure used at stages (c)-(e) is mainly the same as that used at stage (b); besides, some part of tail gas obtained at stage (e) is recirculated to stage (d), and the rest part of tail gas is discharged.

EFFECT: this method is a method in which there is no recirculation of non-reacted synthesis gas to a synthesis stage of oxygenates and without any cooling of a conversion reaction of dimethyl ester to higher hydrocarbons.

6 cl, 2 ex, 1 tbl, 2 dwg

FIELD: chemistry.

SUBSTANCE: claimed invention relates to liquid fuel compositions. Invention deals with liquid fuel composition, containing, at least, one fuel component and from 0.1%(vil.) to 99.5% (vol.) of fraction of distillation of component, which contains, at least, one C4+ compound, derived from water-soluble oxygenated hydrocarbon. Method includes supply of water and water-soluble oxygenated hydrocarbon, including C1+O1+ hydrocarbon, in water liquid phase and/or vapour phase; supply of H2; carrying out catalytic reaction in liquid and/or vapour phase between oxygenated hydrocarbon and H2 in presence of deoxygenation catalyst at temperature of deoxygenation and pressure of deoxygenation to obtain oxygenate, which contains C1+O1-3 hydrocarbon in reaction flow; and carrying put catalytic reaction in liquid and/or vapour phase for oxygenate in presence of condensation catalyst at temperature of condensation and pressure of condensation to obtain C4+ compound, where C4+ compound includes representative, selected from the group, consisting of C4+ alcohol, C4+ ketone, C4+ alkane, C4+ alkene, C5+ cycloalkane, C5+ cycloalkene, aryl, condensed aryl and their mixture. Invention also relates to petrol composition, Diesel fuel composition, kerosene composition and methods of obtaining thereof.

EFFECT: improved characteristics of fuel composition, containing component, obtained from biomass.

9 cl, 19 dwg, 14 tbl, 59 ex

FIELD: chemistry.

SUBSTANCE: method includes stage of contact of pyrolysis oil, produced from biomass, with first catalyst of oxygen removal in presence of hydrogen under first, preliminarily set conditions of hydropurification with formation of first effluent stream of pyrolysis oil with low oxygen content. First catalyst of oxygen removal contains neutral catalytic carrier, nickel, cobalt and molybdenum. First catalyst of oxygen removal contains nickel in quantity from 0.1 to 1.5 wt % in terms of oxide. Version of method is also claimed.

EFFECT: extension of assortment of oxygen removal methods.

10 cl, 1 dwg

FIELD: chemistry.

SUBSTANCE: method consists in successive application on carrier - amorphous aluminium oxide - by method of soaking with following drying and annealing of: water solution of thermally unstable salt of element, selected from the first group, including titanium, tin, zirconium, then water solution of thermally unstable salt of element, selected from the second group, including molybdenum, tungsten, and after that water solution of thermally unstable salt of element, selected from the third group, including cobalt, nickel. Obtained catalyst contains, wt %: oxide of element from the first group - 4.2-15.0, oxide of element from the second group - 12.4-14.2, oxide of element from the third group - 2.1-3.8, remaining part - aluminium oxide. After that, catalyst is activated first by soaking in hydrogen medium at temperature 450-500°C, pressure 5-8 MPa for 3-4 h, then sulfidation at temperature 250-300°C, pressure 5-8 MPa for 3-4 h. And sulfidation is carried out with mixture of hydrogen sulfide and hydrogen with concentration of hydrogen sulfide 10-15 vol%.

EFFECT: method makes it possible to obtain catalyst, which has increased isomerisation ability and preserves catalytic activity with respect to reaction of isomerisation for long time, which results in obtaining Diesel fuel, which has improved low-temperature properties.

4 ex

FIELD: chemistry.

SUBSTANCE: method of biodiesel production is realised by the re-etherification in mixing natural oil, alcohol and a catalyst and following separation of the target product. The method is characterised by the fact that at the first stage of the re-etherification iron sulphate (II) is applied as the catalyst, after which iron sulphate and precipitated glycerol are separated and the mixture of alcohol, oil and ethers of fatty acids are supplied to the second stage of the re-etherification, at which as the catalyst used is an enzyme - lipase, immobilised on the surface, after which glycerol and the enzyme catalyst are separated and the mixture of alcohol and biodiesel is directed to a stage of the target product separation.

EFFECT: method makes it possible to simplify the process of the re-etherification reaction and increase the completeness of the reaction process.

6 cl, 1 tbl

FIELD: process engineering.

SUBSTANCE: invention relates to hydraulic treatment of hydrocarbon fuel. Proposed method comprises production of hydrocarbon stock to be processed including renewable organic substance with hydrogen flow and its feed to hydraulic treatment by bringing said hydrocarbon stock in contact with at least one stationary catalyst bed. Exit flow is fed into hot separator for extraction of top fraction from hot separator and of bottom fraction from separator bottom. Top fraction is fed to water steam conversion while exit flow is directed into cold separator for extraction of gaseous top fraction from cold separator as gas flow enriched with hydrogen to be directed to circulation. Gaseous top fraction is fed to hydrogen sulphide recuperation plant to extract a gaseous flow with decreased content of hydrogen sulphide and carbon dioxide to be fed back in the process.

EFFECT: production of hydrogen to allow decreasing the fresh hydrogen demand at hydraulic treatment stage.

9 cl, 2 dwg, 3 tbl, 2 ex

FIELD: chemistry.

SUBSTANCE: claimed invention relates to methods (processes) and systems for processing triglyceride-containing oils of biological origin with obtaining base oils and fuels for vehicles. Method of obtaining base oil and Diesel fuel includes the following stages: a) processing triglyceride-containing vegetable oil with realisation of oligomerisation and deoxygenation of components on the basis of unsaturated fatty acids, contained in it, with obtaining oligomerised mixture, with said processing including hydration and further removal of water; b) isomerisation of oligomerised mixture above isomerisation catalyst with obtaining isomerised mixture, and isomerised mixture contains base oil component and Diesel fuel component, and isomerised mixture contains, at least, 10 wt % of alkanes with number of carbon atoms 30 or higher, and c) distillation of isomerised mixture with obtaining base oil and Diesel fuel, where oligomerised mixture includes oligomer component, and said oligomer component includes, at least, 50 wt % of dimeric compounds.

EFFECT: processing of oils of biological origin into wide range of products with good level of properties.

11 cl, 4 dwg, 1 ex

FIELD: chemistry.

SUBSTANCE: present invention describes a method of producing hydrocarbon raw material for synthesis of biofuel from lignin. The method involves hydrotreatment of lignin-containing raw material to obtain raw material for biofuel. The lignin-containing raw material contains lignin which is separated from black liquor from a pulping method. The lignin is separated from black liquor from a pulping method by injecting carbon dioxide (CO2) gas. The lignin-containing raw material further contains still residues from an oil refining plant.

EFFECT: as a result of hydrotreatment of lignin contained in raw material for biofuel, oxygen content and average molecular weight of the latter decreases compared to lignin.

8 cl, 6 dwg

FIELD: process engineering.

SUBSTANCE: invention relates to catalysis, particularly, to extraction of catalyst in conversion of oxygenates into olefins. Proposed method comprises the jobs that follow. Flow of the products of oxygenates conversion into olefins is bypassed into reaction shutdown tower. Bottom flow of said tower containing the catalyst is removed. Bottom flow of said tower is separated to obtain in fact clarified fluid and flow bearing the catalyst. Catalyst-bearing flow is bypassed into drying chamber and dried therein to obtain in fact dry catalyst by mixing it with dry heated gas whereat said gas is heated to 150°C to 250°C. Dried catalyst is bypassed into catalyst regenerator for the latter to be recovered.

EFFECT: catalyst extraction.

9 cl, 1 dwg

FIELD: oil and gas industry.

SUBSTANCE: hydrofining method to obtain hydrocarbon compositions includes hydrofining of mixture that contains component (A) - gas oil in quantity from 20 up to 95 wt %; component (A1) - benzene in quantity from 1 up to 40 wt %; component (B) of biologic origin containing fatty acid esters, probably including freed fatty acids; quantity of biologic component is from 4 up to 60 wt %. Moreover all percent ratios are referred to total weight of all components. Hydrocarbon composition (C) has been also claimed; this composition can be used as propellant and/or fuel; it is obtained by hydrofining method; it has cetane number more than 50, density of 820-845 kg/m3, content of polyaromatic compositions less than 1 by wt % in regard to total weight of hydrocarbon compound and total content of polyaromatic compositions less than 20 be wt % in regard to total weight of the composition.

EFFECT: obtaining hydrocarbon composition with improved low-temperature properties.

39 cl, 4 tbl, 2 ex

FIELD: oil and gas industry.

SUBSTANCE: invention is referred to conversion process of associated and natural gases with high content of heavy methane homologs by direct partial oxidation of hydrocarbon gas and further carbonylation of the received products. At that hydrocarbons gas is mixed up with oxygen or oxygen-containing gas with mole ratio of hydrocarbon in heavy components: oxygen of 10-1:1 and selective oxidation of heavy components is made at temperature of 350-420°C and pressure of 10-40 bar and the received products are subjected to processing in presence of carbonylation catalysts with production of liquid products of carboxylic acids and their ethers and dry fuel gas purified from heavy components and enriched with methane.

EFFECT: method is the simplest and the most economically feasible for processing of associated oil gas and natural gas with high content of methane homologs with production of dry gas and a range of valuable liquid products.

3 ex

FIELD: chemistry.

SUBSTANCE: claimed invention relates to method of obtaining methanol, which includes the following stages: a) conversion of hydrocarbon raw material at the stage of conversion process to obtain fresh synthesis-gas, which contains carbon oxides and hydrogen; b) reaction between components of fresh synthesis-gas in the circuit of methanol synthesis to obtain raw methanol; c) processing raw methanol to obtain methanol with required purity degree, characterised by the fact that it additionally includes the following stages: d) trapping at least one flow with high content of CO2 in the process of raw methanol processing and e) recirculation of said at least one flow with high content of CO2 in form of input flow for conversion process. Invention also relates to installation for claimed method realisation and to method of reconstructing installation for obtaining methanol.

EFFECT: claimed inventions make it possible to correct stoichiometric factor of synthesis gas.

15 cl, 3 dwg, 6 tbl, 1 ex

FIELD: chemistry.

SUBSTANCE: invention can be used in the chemical industry. A method of the combined methanol and ammonia production from an initial raw material is realised by means of the following stages. First, synthesis-gas of the methanol production, which contains hydrogen, carbon oxides and nitrogen, is obtained by steam reforming of an initial hydrocarbon raw material at the first stage of reforming and then at the second stage of reforming with air blast. After that, carried out are: catalytic conversion of the synthesis-gas carbon and hydrogen oxides at a single-pass stage of methanol synthesis and the discharge of the methanol-containing output product, and an effluent gas flow, containing nitrogen, hydrogen and non-converted carbon oxides. The non-converted carbon oxides of the gas flow from the preceding stage are removed by hydrogenation to methane at the stage of the catalytic methanation with the formation of synthesis-gas, which has a molar ratio H2:N2, equal 3:1. Ammonia is synthesised by the catalytic conversion of nitrogen and hydrogen, with the discharge of the ammonia-containing product and effluent gas flow, containing hydrogen, nitrogen and methane.

EFFECT: claimed invention provides the creation of a simple and cheap method of the combined production of methanol and ammonia.

7 cl, 1 dwg, 1 tbl

FIELD: oil and gas industry.

SUBSTANCE: invention is related to the method of methanol recovery from gas-vapour mixture at its storage and transhipment and may be used in chemical industry, petrochemical industry, oil and gas producing and processing industries. The method includes extraction of vapours from the gas-vapour mixture in the plant vessel, cooling of the gas-vapour mixture and condensation of vapours in the vapour-condensing unit, condensate return to the vessel and emptying of the vessel. At that cooling of the gas-vapour mixture in the vapour-condensing unit consisting of a vessel for cooled methanol and a packed column installed on it is made to counter-flow interaction of the gas-vapour mixture containing vapours of methanol cooled up to the temperature within the range of minus 25 up to minus 36°C at pressure close to atmosphere pressure when condensed methanol is returned to the vessel for cooled methanol.

EFFECT: method allows increasing quality of storage due to recovery and return of methanol vapours to the vessel.

1 dwg, 1 tbl

FIELD: chemistry.

SUBSTANCE: method is realised by a contact of a feeding flow, enriched with hydrogen and carbon monoxide, with a catalyst of methanol synthesis. The obtained in this way technological flow is cooled, condensed and subjected to separation into a gas phase and a liquid phase with raw methanol. As the feeding flow used is synthesis-gas, obtained by steam gasification of charcoal, representing a product of pyrolysis of preliminarily dried wood wastes. Before the contact of the feeding flow with the catalyst, containing in a mole ratio CuO:ZnO:Cr2O3:MnO:MgO:Al2O3:BaO, equal to 1:0.3:(0.15-0.2):(0.05-0.1):(0.05-0.1):(0.25-0.3):0.05 respectively, its compressing to pressure 3.5-4.5 MPa is performed. After that the flow is supplied into a reactor, where a temperature of 250-300°C is supported due to evaporation of recycled water, released from raw methanol, with steam from recycled water from the reactor being directed to charcoal gasification. Cooling of the technological flow is realised conductively from the feeding flow, and condensation is performed by throttling. After separation the gas phase is divided into two flows, one flow is directed for combustion into a pyrolysis chamber, and the second flow is directed to ejection with a ratio of the gas flow to the feeding flow equal to 10:1, respectively.

EFFECT: invention makes it possible to obtain methanol in a waste-free environmentally friendly way without application of additional energy resources.

1 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to an improved method of producing methanol, dimethyl ether and low-carbon olefin from synthesis gas. The method includes a step of contacting synthesis gas with a catalyst under conditions for converting the synthesis gas into methanol, dimethyl ether, and low-carbon olefins, characterised, wherein the catalyst contains an amorphous alloy consisting of components M-P, M-B or M-B-P, wherein component M represents two or more elements selected from lanthanides and the third, fourth and fifth series of groups IIIA, IVA, VA, IB, IIB, IVB, VB, VIB, VIIB and VIII of the Periodic Table of Elements.

EFFECT: method increases selectivity of the target product by conducting the process in conditions which ensure high conversion of CO and availability of carbon.

16 cl, 3 dwg, 3 tbl, 11 ex

FIELD: chemistry.

SUBSTANCE: invention describes a methanol synthesis method which comprises conversion of hydrocarbon-containing material to obtain synthesis gas (1) containing carbon monoxide and hydrogen and a reaction between components of fresh synthesis gas in a synthesis loop (10) to obtain raw methanol and removing hydrogen-containing purge gas (20) from the synthesis loop. The purge gas is heated by heat recuperation via indirect heat exchange with at least one high-temperature heat source in said method, said heat source being adapted to heat purge gas to temperature not lower than 200°C to obtain a heated purge gas (33), and said heated purge gas, as such, is expanded in a corresponding expander (34), and energy is obtained due to expansion of the purge gas in the expander, wherein said high-temperature heat source used is hot waste gas from the conversion process, wherein the material is converted to fresh synthesis gas (1) or a stream of hot steam. The invention also relates to a methanol synthesis apparatus and a method of reconstructing a methanol synthesis apparatus.

EFFECT: disclosed objects improve overall energy balance of the process.

13 cl, 2 dwg, 2 ex

FIELD: chemistry.

SUBSTANCE: invention relates to an improved method for synthesis of methanol, wherein raw methanol (101) is obtained in a synthesis section and purified in a distillation section (D) to obtain pure methanol (104), a stream (103) of instantaneously escaping gas and by-products (105, 106). At least a portion of said stream (103) of instantaneously escaping gas is treated to separate from said gas a stream (110) containing methanol, and that methanol-containing stream (110) is returned to the distillation section (D) to increase pure methanol production volume, wherein pressure of at least a portion of the stream (103) of the instantaneously escaping gas is raised before treating the stream (103) of the instantaneously escaping gas to separate the methanol-containing stream. The invention also relates to an apparatus for carrying out said method and a method of renovating said apparatus.

EFFECT: method enables to increase pure methanol production volume, safe power consumption and reduce emission of pollutants.

10 cl, 3 dwg, 2 tbl, 2 ex

FIELD: oil and gas industry.

SUBSTANCE: method includes heating of source natural gas, mixing of superheated steam with source natural gas, one-stage conversion of gas and steam mixture in reformer to converted gas, cooling of converted gas and its division into two flows. The first flow is subject to one-stage catalytic conversion to methanol while the second flow is subject to catalytic synthesis with production of liquefied hydrocarbon gas which is sent to conversion together with source natural gas and liquid hydrocarbons subjected to stabilisation in rectification tower. Plant for implementation of the above method is suggested also in order to produce synthetic liquid hydrocarbons and methanol; the plant is integrated into production train facilities.

EFFECT: effective coproduction of methanol and synthetic liquid hydrocarbons in the same flow diagram during processing.

15 cl, 1 dwg

FIELD: oil and gas industry.

SUBSTANCE: invention refers to a method and a plant for methanol production from gas of gas deposits and gas-condensate deposits through synthesis gas using excess heat of the main process of methanol recovery from water-methanol solution returned after inhibition of hydrate formation in a system of collection, treatment and further transport of gas of a complex gas treatment plant (CGTP). Method involves catalytic steam reforming process of gas, heat recovery of converted and flue gases, separation, drying, compression of synthesis gas, synthesis of methanol from synthesis gas on low-temperature catalyst, separation of crude methanol and rectification of methanol, and in addition, stages of methanol recovery from water-methanol solution used in the complex gas treatment plant as a hydrate formation inhibitor and mixing of methanol-rectificate with recovered methanol. In addition, the plant includes a methanol recovery unit and a mixing assembly of synthesised methanol-rectificate and recovered methanol.

EFFECT: creation of an efficient method combining production and recovery of methanol within the framework of a single complex plant; improvement of economic indices of the methanol plant; improvement of quality and reduction of prime cost of methanol production, and elimination of additional environmental gas production risks.

24 cl, 1 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a method of increasing molar ratio of methyl to phenyl in one or more aromatic compounds in feed stock. The method involves: A) conducting a reaction between an effective amount of one or more aromatic compounds and an effective amount of one or more reagents which methylate aromatic compounds, which include at least either an alkane, cycloalkane, alkane radical or cycloalkane radical, in the presence of a catalyst which contains a zeolite, to obtain a product which is characterised by molar ratio of methyl to phenyl which is at least 0.1 times greater than that of the feed stock.

EFFECT: invention enables to convert benzene to other substituted aromatic compounds while minimising undesirable products and/or secondary reactions.

16 cl, 1 ex, 1 tbl

Up!