Method for obtaining methanol from hydrocarbon gas of gas and gas-condensate deposits, and plant for its implementation

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

 

The technical field

The invention is intended for use in industry, in particular, in the gas-producing enterprises, and relates to a process for producing methanol from gas and gas condensate fields via synthesis gas using the excess heat of the basic process for the recovery of methanol from the aqueous methanol solution returned after inhibition of hydrate formation in the system of gathering, processing and long-distance transportation of gas installation complex gas treatment unit (GTU).

The level of technology

As you know, the main gas and gas condensate field in the Russian Federation are located in remote areas of the Far North, for example, in the Yamalo-Nenets Autonomous region and Yakutia. On the profitability of gas production significantly affects the cost of hydrate inhibitor, such as methanol consumed at a rate of 2.5 kg per 1000 m3gas. Delivery of methanol to the remote fields is carried out with the risk of causing serious environmental damage to nature in a possible spill of methanol, which is a poison, and leads to the fact that the cost of methanol in the field exceed the selling price of factory.

In addition, a further decline in economic performance. gas production and the emergence of copolytechnologies.com risk is due to the fact, on most fields, especially small and medium, a substantial portion of the methanol used for inhibiting hydrate formation, not recycled or reused. Most commonly methanol (in the form of water-methanol mixtures containing salts of metals and other pollutants) is discharged into the drive with the subsequent injection and poisons the environment or burned in special furnaces, consuming gas for heating water-methanol mixture and increasing the carbon dioxide emissions into the atmosphere.

To solve these problems gas producers allows the creation of small installations, combining both receiving and regeneration of methanol and able to work directly on the field, both in the form of independent production and the composition of the complex gas treatment plants (GPP).

Technology of production of methanol is known from the first half of the 20th century and is a well established industrial process.

A method of producing methanol, comprising the process of steam reforming of hydrocarbons under pressure up to 30 ATM in a tubular furnace with fire heating, where the heat to cover the endothermic effect of the decomposition reaction of hydrocarbons with water vapor to hydrogen and oxides of carbon produced by burning fuel in the reaction tube pécs and passed to the reaction mixture. Converted gas after the tube furnace and after mixing with the circulating gas is fed into the synthesis of methanol. After cooling the reacted mixture and condensation of methanol and water from the circulating mixture to maintain the circulating gas of the effective values of partial pressures of carbon oxides, part of the circulating gas in the form of blowdown containing excess hydrogen, derived from the synthesis loop, and is used in the furnace as fuel (avts No. 579220, CL C01B 3/38, 1977).

The main disadvantage of this method, known as from the said patent and academic literature (Karavaev M.M., Leonov V.E. and other Technology of synthetic methanol // M.: Chemistry, 1984, p.72-125) are high energy intensity of the process, a multi-stage and complexity of the equipment that does not allow you to create a profitable small units of methanol directly on the field.

Since the most expensive stage is the generation of synthesis gas, has repeatedly attempted to create cost-effective low-tonnage production of methanol without the stage of synthesis gas, for example, using a direct gas-phase oxidation of methane to methanol at high pressures. The process is carried out at pressures up to 10 MPa and temperatures of 400-450°C in a tubular reactor with a relatively low initial the concentrations of oxygen, followed by cooling gas-liquid mixture and separation of liquid products, of which the rectification into methanol (Arutyunov B.C., O.V. Krylov Oxidative conversion of methane. //M.: Nauka, 1998, s-145; RF patent №2162460, CL C07C 31/04, B01J 12/00, publ. 27.01.2001).

Despite the reduction stages, the rejection of the catalysts and simplification of equipment significant disadvantages of the direct gas-phase oxidation of methane to methanol is a low degree of methane conversion per pass through the reactor and, accordingly, the low yield of methanol, high energy costs and a large number of products, including korrozionnostojkie organic acids. This precludes the practical implementation of this method for small-scale installations of methanol.

Thus, these and other known solutions are not allowed to create a profitable small units of methanol production at the fields.

It was proposed to reduce capital and operating costs due to the integration of the unit to produce methanol in the composition of the field's infrastructure, in particular to integrate it with the installation of complex gas treatment plant (GTP). In this case, the maximum use of auxiliary production available in unit (flare system, treatment facilities, water treatment, electrical power, Instrument air, nitrogen plant, operator).

From the patent of the Russian Federation No. 225422, publ. 20.06.2005, there is a method of production of methanol and installation for its implementation, integrated with the installation of complex gas treatment plant (GTP). The essence of the proposed approach lies in the fact that the hydrocarbon gas with the installation of complex gas treatment plant (GTP) under a pressure of 8.0 MPa and temperature 380-430°C enters the tube space of the tubular reactor pre-steam reforming. The resulting prereforming gas passes to the next stage of the reformer, which produces the final synthesis gas by adding oxygen. The formation of synthesis gas in the shaft reactor occurs at a temperature of 600-950°C and a pressure of 8.0 MPa. The resulting synthesis gas with a temperature of 250-280°C delivered in 2-step isothermal methanol synthesis reactor with an external heat exchanger for cooling the reaction mixture. For the process of methanol synthesis reactor is filled with a copper-containing catalyst SNM-3C. The reaction of methanol synthesis takes place at a temperature 220-280°C and a pressure of 8.0 MPa. The cooled reaction mixture enters the separator for separating methanol from the unreacted products synthesis gas. Methanol-Syrets concentration 78-84% goes to Park storage of methanol. Gases from the separator mainly containing CH4H2and CO2going to use the for own needs unit (boiler, power plant and other heaters) or mixed with the prepared gas unit. but due to the small amounts of unreacted gas on the quality of prepared commercial gas unit no effect.

The disadvantages of this method are the high capital and operating costs arising due to the presence of:

- compressor equipment to ensure high process pressure (8.0 MPa),

- separation block for the synthesis of methanol on two reactor with external coolers and an additional amount of catalyst

- stage and additional equipment produce oxygen.

In addition, the use of oxygen leads to the danger of explosive mixtures with methane and hydrogen, which dramatically reduces the security of the process.

Some disadvantages of the method, known from the patent of the Russian Federation No. 2254322, was eliminated in the RF patent for useful model №102537, publ. 10.03.2011, which can be used as a prototype, which has slightly improved the economic performance of small units of production of methanol. In this way was reduced process pressure up to 2.2 MPa, taken on how best to use heat flows, the methanol synthesis is carried out in a single reactor without external coolers. Also installed were excluded:

- block of raw material preparation, as podgotovlennyy unit sales gas fields of the Far North of the Russian Federation does not contain sulfur compounds, poisoning the catalysts in the conversion of gas-vapor mixture and the methanol synthesis;

- the unit is receiving oxygen;

the cleaning unit of crude methanol from impurities, because the concentration of 85-95% allows the use of methanol obtained as a hydrate formation inhibitor;

block primary water treatment, such as a block, as a rule, is included in unit.

The disadvantages of the method known from RF patent for useful model №102537, are sub-optimal use of heat converted and flue gases, reduced coefficient of performance (COP) of the reformer furnace, the increased gas consumption for production of 1 ton of crude methanol and relatively low concentration of production of methanol. These drawbacks lead to the deterioration of economic indicators of small units of production of methanol.

In addition, a significant drawback of all the methods and systems is the inability to reuse the methanol produced at the facility and used as a hydrate formation inhibitor in unit. The use in the composition of small units of methanol block the regeneration of water-methanol mixture improves the economic performance of the unit to produce methanol, in particular, improves the quality and reduces the cost of production of methanol, and fixes to anitelea environmental risks of gas production.

The technical result of the claimed invention is to provide a cost-effective way, combining the production of methanol and regeneration of methanol from water-methanol mixture, returned after inhibition of hydrate formation in the installation of complex gas within a single complex unit. This improves the economic performance setup methanol, in particular, improves the quality and reduces the cost of production of methanol, and eliminates additional environmental risks of gas production.

The principal technological scheme allows to obtain methanol hydrocarbon gas gas and gas condensate fields and includes the catalytic steam reforming in the reforming furnace to receive the converted gas waste heat recovery converted and flue gases, including steam medium pressure of 0.4-0.5 MPa, drying and compression of the synthesis gas to a pressure of 4.5 to 5.5 MPa, the direction of the steam condensate is separated from the converted gas and other media for re-use in the evaporation of the methanol synthesis at low temperature catalyst in one stage. In addition, in contrast to known solutions, the installation includes an integrated heat and material flows regeneration unit methanol (aqueous methanol solution)used in the unit in Kutch is TBE hydrate inhibitors. Due to the absence of harmful emissions is environmentally friendly production.

Thus, owing to the totality of the proposed technical solutions to complex plant for production of methanol acquires new properties, not known from modern technology - production of methanol and regeneration of methanol from water-methanol mixture, returned after inhibition of hydrate formation in the setting of complex gas preparation, providing significant technical, economic and environmental advantages of using such installations in industry, in particular, at the enterprises of gas (reducing gas consumption per 1 tonne of methanol, reduce environmental risks).

This technical result is achieved in the method of producing methanol from hydrocarbon gas gas and gas condensate fields, including catalytic steam reforming gas of the reformer furnace with getting converted gas heat recovery converted and flue gases, separation, dehydration, compression, synthesis gas, methanol synthesis from synthesis gas at low temperature catalyst, the separation of methanol, and the methanol rectification, the method additionally includes the stage of regeneration of the methanol from the aqueous methanol solution used in the installation is complex gas treatment plant (GTP) as a hydrate formation inhibitor, and the mixture of methanol-rectified with regenerated methanol.

Steam reforming gas is conducted at high temperature Nickel catalyst at 780-980°C and 2.0-2.5 MPa, while in the furnace reformer additionally served heated to 200-250°C air, resulting in increased efficiency (energy efficiency) operation of the reformer furnace, and the reduction of gas consumption by 1-2% per 1 ton of methanol.

In the method provided by heat recovery of flue gases produced by the combustion of fuel gas in the reforming furnace, which is used to produce steam medium pressure of 0.4-0.5 MPa for heating apparatuses stage methanol regeneration, as well as to heat the gas mixture supplied to the conversion, to superheat the saturated water vapor to preheat the hydrocarbon gas supplied to the mixing with superheated steam for feedwater heating, for heating the air supplied to the burner of the reformer furnace.

In the method provided by heat recovery converted gas generated in the reforming furnace, is used to produce saturated vapor for heating demineralized water, to heat the water-methanol solution in methanol regeneration, to heat the cube distillation of methanol.

In the method provided by the mixture of methanol-rectified fortress 86-98% wt., obtained when rectifica the AI synthesized methanol, with regenerated methanol fortress 96-99% weight. to further strengthen it, which goes together with the synthesized methanol for use in installations gas industries.

This technical result is achieved in a device for producing methanol from a hydrocarbon gas and gas condensate fields, including successively installed and interconnected through a system of pipelines source of feed water and the hydrocarbon source gas, including the installation of complex gas unit heat exchange apparatus for heating the gas and vapor mixture, oven catalytic steam reforming to obtain a converted gas cooling heat exchangers converted gas heater demineralized water separators converted gas compressor and converted circulating gas, the heat exchanger-recuperator synthesis gas, methanol synthesis reactor for catalytic production of methanol from synthesis gas (a mixture of converted and circulating gases), heat exchangers cooling of the products of the synthesis of methanol, column distillation of methanol, and the installation further comprises a regeneration unit of methanol from the aqueous methanol solution used in the installation of a complex of the second gas as a hydrate formation inhibitor and a host of mixing the synthesized methanol-rectified and regenerated methanol.

The source of the hydrocarbon gas includes a processing block of the source gas, where, if necessary, separation, reduction and heating.

Block heat exchange apparatus for heating a hydrocarbon gas and steam-gas mixture due to the heat of the flue gases produced by the combustion of the fuel gas of the reformer furnace, includes serially connected air heater connected to the blower, heater fuel gas heater feedwater heater hydrocarbon gas, steam generator, superheater, reheater steam-gas mixture.

Moreover, the output of the reformer furnace in the converted gas is connected to the supply line of the converted gas to the methanol synthesis reactor, through the HRSG, optionally connected to paromomycin saturated vapor and superheated water.

For using the heat of the reformed gas outlet of the reformer furnace is connected through a waste-heat boiler in addition to the rectification column reboiler methanol, and the reboiler of the column regeneration water-methanol solution.

Cooling heat exchangers converted gas include the HRSG to produce steam, heat exchanger-boiler column regeneration water-methanol solution, the heat exchanger-boiler Colo is by distillation of methanol, the demineralized water heater, air cooler converted gas.

Installation of complex gas contains the block of preparation of chemically treated water, the block of preparation of raw materials, auxiliary production, including flare production, treatment facilities, sources of electrical energy, compressed air supply to pneumatic devices and instrumentation (EC & I), chemical laboratory, operator.

The source of feed water includes serially connected processing block chemically treated water coming from the installation of complex gas and from another source of water, the preparation unit of demineralized water, which is connected with demineralized water heater, deaerator and feedwater heater unit heat-exchange equipment.

Distillation column of methanol series connected with a capacitor of methanol vapor and reflux tank for collecting methanol-rectified.

In the deaerator additionally receives the condensate from the converted gas separators and block reception and preparation of the water-methanol solution installation methanol regeneration. Included in the extra organization condensate collection allows for a 15-20% reduction in the water consumption of the complex is the situation of methanol for the needs of vaporization.

The regeneration unit of methanol includes interconnected block reception and preparation of the water-methanol solution for reducing, filtering, degassing and heating the aqueous-methanolic solution coming from the installation of complex gas column regeneration water-methanol solution, a condenser for methanol and reflux tank for collecting the regenerated methanol.

Air heater unit heat-exchange apparatus is connected with a burner of the reformer furnace for additional supply heated to 200-250°C air, resulting in increased efficiency (energy efficiency) operation of the reformer furnace, and the reduction of gas consumption by 1-2% per 1 ton of methanol.

The superheater unit heat-exchange apparatus is additionally connected through reduction-cooling installation with boiler columns methanol regeneration for additional heating of the water-methanol solution.

The output of the feed water heater is connected with paromomycin for saturated steam entering the superheater unit heat-exchange equipment.

Site mixing the synthesized methanol-rectified and the regenerated methanol is connected by means of pipelines and pumps with reflux tank columns of the distillation of methanol and column regeneration water-methanol is Astor.

Cooling heat exchangers products of methanol synthesis include connected in series heat exchanger-heat exchanger syngas and air cooler circulating gas.

The output of the methanol synthesis reactor is additionally connected to the heat exchanger-recuperator synthesis gas for use heat products of the synthesis of methanol to heat the synthesis gas.

The implementation of the invention

Installation scheme that implements the claimed invention, is presented in figure 1.

The composition of the objects installation methanol production:

1. The preparation unit of the source gas separation, reduction, heating);

2. Tube furnace steam reforming;

3. The heater of the steam-gas mixture;

4. The superheater coil;

5. The steam generator in the flue gas;

6. The heater source gas;

7. The heater nutrient (demineralized and deaerated water;

8. The fuel gas heater;

9. Air heater;

10. The smoke exhauster;

11. Chimney;

12. The blower;

13. The block of preparation of demineralized water;

14. The deaerator;

15. Parosbornoj;

16. The circulation pump boiler water;

17. The HRSG;

18. The heat exchanger-boiler the rectification column methanol;

19. The converted gas separator;

20. The demineralized water heater;

22. Air cooler converted gas;

23. The converted gas separator;

24. Booster compressor converted gas;

25. Compressor circulating gas;

26. The heat exchanger-heat exchanger syngas;

27. Starting fire heater methanol synthesis reactor;

28. The methanol synthesis reactor;

29. Air cooler circulating gas;

30. The separator methanol;

31. The separator purge gases synthesis;

32. Capacity-degasser methanol;

33. Reflux the capacity of the rectification column methanol;

34. A condenser methanol rectification column;

35. Distillation column of methanol;

36. The capacitor excess low-pressure steam;

37. The collection vessel steam condensate;

38. Stripping capacity gas condensate;

39. Block reception and preparation of the water-methanol solution (reduction, filtration, degassing, heating);

40. The heat exchanger-boiler column regeneration water-methanol solution;

41. Column regeneration water-methanol solution;

42. A condenser methanol column regeneration water-methanol solution;

43. Reflux the capacity of the column regeneration water-methanol solution.

Comprehensive ustanavlivaetsya methanol works as follows. Arriving at the installation of the gas goes into the preparation unit 1, where the gas optionally separated with the separation of the liquid condensate is heated to 30-40°C and throttled to a pressure of 2.0 to 2.5 MPa. Part of the prepared gas is heated flue gases to 220-270°C in the heater 8 and is directed to the burner of the reformer furnace 2. At the same time on the burner through the heater 9 is supplied heated to 200-250°C, the air supplied by the blower 12. Heated air increases the efficiency (energy efficiency) operation of the reformer furnace 2, which leads to the reduction of gas consumption by 1-2% per 1 ton of methanol.

The main quantity of the prepared gas is mixed with saturated steam from parosbornoj 15, is heated in the heater 6 to 350-450°C and mixed with superheated steam obtained in the superheater 4. Technological scheme provides automatic adjustment of the ratio of costs of natural gas and steam entering the conversion, with the required ratio of steam : gas = (2,7-3,2):1, which depends on the composition of the gas. The obtained gas-vapor mixture with a temperature of 350-450°C is fed to heat exchanger 3.

Superheated low pressure steam from the superheater 4 through reduction-cooling installation (ROWE), where for regulating the steam temperature water is pumped from the deaerator 14, comes in to petrinic column regeneration aqueous-methanolic solution of 40 for heating the regenerated methanol. The excess steam after the boiler is used to supply heat to the block, reception and preparation of aqueous-methanolic solution of 39. Obtained in this block the condensate flows into the collection vessel steam condensate 37.

The distillate regeneration of water-methanol solution is condensed in the cooling apparatus, for example, the system of air or water cooling (AVO) 42 (condenser methanol column regeneration) and sent to the reflux tank 43, where the methanol fortress 96-98% weight. partially enters the irrigation of the upper part of the column regeneration 41 and then is mixed with the regenerated methanol to further strengthen and sent together with the synthesized methanol-rectified for use in installations gas industries.

The heat exchangers and the superheaters positions 3-9 together constitute a block of heat-exchange apparatus (BTA), is necessary for effective utilization of heat of flue gases of the reformer furnace 2. After heat recovery, flue gases with temperatures up to 200°C induced-draft fan 10 are released into the atmosphere through the flue 11 to a height of not less than 30 m, providing a dispersion of emissions to concentrations not exceeding the maximum permissible values.

Heated due to the heat of flue gases up to 500-600°C, the gas-vapor mixture is fed into the reaction tube furnace reformin is as 2, where high temperature Nickel catalyst at 780-980°C and 2.0-2.5 MPa reaction takes place the conversion of prepared water vapor gas with the formation of the converted gas. The use of high temperature catalyst increases the conversion of methane to 3-4%, improves the composition of the reformed gas by reducing the proportion of inert components, in particular the residual methane with typical steam reforming 4-5% to 1-2%. when the hydrogen content of 45-50% vol., carbon monoxide 9-10% vol., water vapor 30-35% vol., carbon dioxide and inert components (the rest is up to 100% vol.). The improved composition of the reformed gas allows to reduce specific consumption of gas per 1 ton of methanol by 3-5%.

The output temperature of the reformed gas 780-900°C, and the temperature of the flue gases at the outlet of the radiant zone of the furnace reformer 2 to about 950°C is automatically controlled by the fuel gas in the burner of the reformer furnace 2. Heat converted gas leaving the reaction zone of the reformer furnace 2, is used in the recovery boiler 17. By cooling the gas with 780-900°C to 300-380°C produces saturated water vapor pressure of 2.0-2.5 MPa, which parosbornoj 15 is supplied to the mixing with the prepared gas in the superheater 4 to obtain superheated steam.

The feed water is brought to sootvetstvujushchijemu in block primary water treatment unit, after block preparation of demineralized water 13 is supplied to the heater 20 and the tank 14. In addition, in the deaerator 14 receives the condensate from the Stripping tank of gas condensate 38, in which he gathers from the converted gas separators 19, 21 and 23. Additional amount of water enters the deaerator 14 from the collection tank of the steam condensate 37, which also receives the condensate low pressure steam from the block receiving and preparing water-methanolic solution of 39 installation methanol regeneration. The collection of the condensate allows 15-20% reduction in water consumption integrated installation of methanol for the needs of vaporization.

Technological scheme provides consistent heat recovery converted gas in the HRSG 17, the rectification column reboiler methanol 18 and demineralized water heater 20, where by cooling the converted gas produces wet steam, heating cube the rectification column methanol and heated demineralized water, respectively.

Finally the converted gas is cooled in the air or water cooling (DAC) 22. After each stage of cooling is the separation of the condensate in separator 19, 21 and 23. Segregated condensate enters the deaerator 14 and, as indicated above, is used in the system parool is adowanie installation. Drained the converted gas is supplied to the inlet of the compressor converted gas 24.

The mixture is converted circulating gas (synthesis gas), compressed to 4.5-5.5 MPa, with discharge of the compressor unit 24 is supplied to the inlet of the compressor circulating gas 25, and then into the heat exchanger-heat exchanger syngas 26, where it is heated by the products of the reaction of methanol synthesis. The mixture is converted circulating gas enters the reactor 28 synthesis of methanol. When you run the installation for heating up to 200÷280°C. the synthesis gas entering the synthesis reactor 28 is used launchers fire the heater 27.

On the shelves of the reactor 28 is a low-temperature copper or other catalyst known from modern technology, the use of which determines the parameters of the synthesis process (for a copper-containing catalyst of low pressure: gas flow rate to the catalyst 5000-15000 h-1, 200÷280°C and 4.5-5.5 MPa). To achieve a more complete degree of conversion of carbon oxides in the synthesis gas provides for circulation of the synthesis gas with a constant output from the separator 31 purge gases for disposal on the torch unit to maintain a given level of inert components in the synthesis gas. Circulating the gas after the separator methanol 30 receives namestie with fresh converted to gas and then to the suction side of the compressor 25.

Temperature control in the area of catalysis of the synthesis reactor 28 is carried out automatically by the cold mixture and converted circulating gas via the bypass lines. The flow of cold gas is collected from the discharge of compressor unit 25.

Provided by heat recovery of the reaction products leaving the synthesis reactor 28 to preheat the mixture and converted circulating gas in the heat exchanger-recuperator 26. Next, the cooled reaction gas is fed to the condensation of methanol in air cooler 29, and then into the separator 30 is designed to separate the methanol from the gas-liquid mixture.

Separated in the separator 30 methanol raw is served in the capacity of the crystallizer 32, which, after discharge pressure is directed to the rectification. The process of distillation of crude methanol is carried out in a Packed distillation column 35, the cube is heated due to the heat converted gas into the heat exchanger, the heater 18. The temperature in the bottom part of column 35 is regulated by the bypass converted gas by a heat exchanger of the boiler. CBM product of the column 35 (salt-containing effluents), is sent to the treatment plant unit.

The distillate of the column 35 is condensed in the air cooler 34 (condenser methanol rectification column and is sent to repl the UNC capacity 33, where methanol fortress 86-98% weight. partially enters the irrigation of the upper part of the column 35 and further strengthening is mixed with the regenerated methanol fortress 96-99% of the weight.

The resulting mixture in the form of production of methanol strength of not lower than 96% in weight. served on the warehouse methanol unit, where directed for use in installations gas industries.

1. A method of producing methanol from hydrocarbon gas gas and gas condensate fields, including catalytic steam reforming gas of the reformer furnace with getting converted gas heat recovery converted and flue gases, separation, dehydration, compression, synthesis gas, methanol synthesis from synthesis gas at low temperature catalyst, the separation of methanol, and the methanol rectification, characterized in that it additionally includes the stage of regeneration of the methanol from the aqueous methanol solution used in the installation of complex gas as a hydrate formation inhibitor, and a mixture of methanol-rectified with regenerated methanol.

2. The method according to claim 1, characterized in that the steam reforming gas is conducted at high temperature Nickel catalyst at 780-980°C and 2.0-2.5 MPa.

3. The method according to claim 1, characterized in that the furnace reformer additionally served heated to 200-250°C in the spirit.

4. The method according to claim 1, characterized in that the heat of the flue gases is used to produce steam medium pressure of 0.4-0.5 MPa for heating apparatuses stage methanol regeneration.

5. The method according to claim 1, characterized in that the heat of the flue gases produced by the combustion of the fuel gas of the reformer furnace is used to heat the gas mixture supplied to the conversion, to superheat the saturated water vapor to preheat the hydrocarbon gas supplied to the mixing with superheated steam for feedwater heating, for heating the air supplied to the burner of the reformer furnace.

6. The method according to claim 1, characterized in that the heat converted gas generated in the reforming furnace, is used to produce saturated vapor for heating demineralized water, to heat the water-methanol solution in methanol regeneration, to heat the cube distillation of methanol.

7. The method according to claim 1, characterized in that methanol is rectified fortress 86-98% wt. mixed with regenerated methanol fortress 96-99 wt.%.

8. Device for producing methanol from a hydrocarbon gas and gas condensate fields, including successively installed and interconnected through a system of pipelines source of feed water, a source of hydrocarbon gas, the heat exchange unit AP is aratory to heat the gas and vapor mixture, oven catalytic steam reforming to obtain a converted gas cooling heat exchangers converted gas heater demineralized water separators converted gas compressor and converted circulating gas, the heat exchanger-recuperator synthesis gas, methanol synthesis reactor for catalytic production of methanol from synthesis gas (a mixture of converted and circulating gases), heat exchangers cooling of the products of the synthesis of methanol, column distillation of methanol, characterized in that it further comprises a regeneration unit of methanol from the aqueous methanol solution used in the installation of complex gas as a hydrate formation inhibitor and a host of mixing the synthesized methanol-rectified and regenerated methanol.

9. Installation according to claim 8, characterized in that the heat exchanger apparatus for heating a hydrocarbon gas and steam-gas mixture due to the heat of the flue gases produced by the combustion of the fuel gas of the reformer furnace, includes serially connected air heater connected to the blower, heater fuel gas heater feedwater heater hydrocarbon gas, steam generator, superheater, reheater steam-see the sea.

10. Installation according to claim 9, characterized in that the air heater unit heat-exchange apparatus is connected with a burner of the reformer furnace for additional supply heated to 200-250°C air.

11. Installation according to claim 9, characterized in that the superheater unit heat-exchange equipment through reduction-cooling installation is connected with the column methanol regeneration for additional heating of the water-methanol solution.

12. Installation according to claim 9, characterized in that the output of the feed water heater is connected with paromomycin for saturated steam entering the superheater unit heat-exchange equipment.

13. Installation according to claim 8, characterized in that the output of the reformer furnace in the converted gas is connected to the supply line of the converted gas to the methanol synthesis reactor through the HRSG, optionally connected to paromomycin saturated vapor and superheated water.

14. Installation according to claim 8, characterized in that the output of the reformer furnace to heat the converted gas is connected through a waste-heat boiler in addition to the rectification column reboiler of methanol and the reboiler of the column regeneration water-methanol solution.

15. Installation according to claim 8, characterized in that the heat exchangers cooling reformed gas including the indicate the HRSG to produce steam, the heat exchanger-boiler column regeneration water-methanol solution, the heat exchanger-boiler column distillation of the methanol, the demineralized water heater, air cooler converted gas.

16. Installation according to claim 8, characterized in that the source of feed water includes serially connected processing block chemically treated water from the plant of complex gas preparation, or from another source of water, the preparation unit of demineralized water, which is connected with demineralized water heater, deaerator and feedwater heater unit heat-exchange equipment.

17. Installation according to item 16, characterized in that the deaerator additionally receives the condensate from the converted gas separators and block reception and preparation of the water-methanol solution installation methanol regeneration.

18. Installation according to claim 8, characterized in that the hydrocarbon source gas includes a processing block of the source gas, where they spend their separation, reduction and heating.

19. Installation according to claim 8, characterized in that the installation of complex gas contains the block of preparation of chemically treated water, the block of preparation of raw materials, auxiliary production, including flare production, treatment facilities, sources of electrical energy, gaty the air supply to pneumatic devices and instrumentation, chemical laboratory, operator.

20. Installation according to claim 8, characterized in that the distillation column of methanol series connected with a capacitor of methanol vapor and reflux tank for collecting methanol-rectified.

21. Installation according to claim 8, characterized in that the regeneration unit of methanol includes interconnected block reception and preparation of the water-methanol solution for pressure regulation, filtration, degassing and heating the aqueous-methanolic solution coming from the installation of complex gas column regeneration water-methanol solution, a condenser for methanol and reflux tank for collecting the regenerated methanol.

22. Installation according to claim 8, characterized in that the node mixing the synthesized methanol-rectified and the regenerated methanol is connected by means of pipelines and pumps with reflux tank columns of the distillation of methanol and column regeneration water-methanol solution.

23. Installation according to claim 8, characterized in that the heat exchangers cooling products for methanol synthesis include connected in series heat exchanger-heat exchanger syngas and air cooler circulating gas.

24. Installation according to claim 8, characterized in that the output of the methanol synthesis reactor is additionally connected to the heat exchanger-ré is operatora synthesis gas for use heat products of the synthesis of methanol to heat the synthesis gas.



 

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FIELD: chemistry.

SUBSTANCE: invention relates to a method for direct conversion of lower C1-C4 paraffins to oxygenates such as alcohols and aldehydes, which are valuable intermediate products of organic synthesis and can be used as components of engine fuel and/or starting material for producing synthetic gasoline and other engine fuels. The method involves passing a mixture consisting of a lower paraffin or oxygen, diluted with an inert gas or air or pure oxygen, through a catalyst bed at temperature not higher than 350°C. The catalyst used is a catalyst system for heterogeneous reactions, which contains microfibre of a high-silica support and at least one active element, the active element being in form of either a MeOxHalv composite or a EwMezOxHaly composite, wherein the element Me in both composites is selected from a group which includes transition metals of groups 5-12 and periods 4 and 5, or elements of lanthanum or lanthanide groups or, preferably, ruthenium; element Hal is one of the halogens: fluorine, chlorine, bromine, iodine, but preferably chlorine; element E in the EwMezOxHaly composite is selected from a group which includes alkali, alkali-earth elements, or hydrogen, and indices w, z, x and y are weight fractions of elements in given composites and can vary in the following ranges: z - from 0.12 to 0.80, x - from 0.013 to 0.34, y - from 0.14 to 0.74, w - from 0 to 0.50.

EFFECT: method enables to achieve high degree of conversion of starting reactants and high selectivity of formation of alcohols.

4 cl, 15 ex

FIELD: chemistry.

SUBSTANCE: present invention relates to a method of producing methanol by bringing a feed stream rich in hydrogen and carbon monoxide in a reactor into contact with a methanol synthesis catalyst to obtain a process stream, followed by cooling thereof, condensation and separation into a gas phase and a liquid phase with crude methanol. The feed stream used is cleaned gas which is obtained by direct-flow gasification of wood processing wastes. The feed stream is enriched with hydrogen by controlled electrolysis of recycled water before bringing the feed stream into contact with a catalyst containing the following, wt %: copper oxide 62, zinc oxide 31, aluminium oxide 7. The feed stream is compressed to pressure of 4.5-5 MPa and then divided into two streams. One stream is fed into the reactor onto the catalyst for contacting through a heat exchanger which simultaneously cools the process stream. The other stream is fed directed onto the catalyst for contacting and reaction temperature is maintained at 250-270°C. After final cooling of the process stream in the still residue of the distillation apparatus, it is separated by throttling into a gas phase and a liquid phase. After separation, the gas phase is divided into two streams. One stream is fed for oxidation into a direct-flow gasifier and the other is mixed with the feed stream before compression.

EFFECT: invention enables to obtain the desired product via a wasteless method using one readily available catalyst.

1 dwg

FIELD: process engineering.

SUBSTANCE: invention relates to production of natural gas and gas condensate treatment in the field. Proposed method comprises WMS degassing, separating free condensate from WMS, heating WMS in regenerator, methanol recovery from WMS in rectifier, cooling methanol vapors, their condensation and draining into reflux collection tank, feeding collected methanol into tower for refluxing and discharging excess methanol into storehouse. Note here that at all gas fields of the deposit, apart from one, WMS is pre-distilled to increase methanol concentration to level sufficient for its safe transfer via pipelines without freezing and transferred to head WMS high recovery installation to produce commercial methanol for reuse. WMS high recovery installation is located at one of gas fields selected with due allowance for WMS transport logistics.

EFFECT: higher quality and lower costs, increased yield, decreased harmful environmental effects.

2 cl, 1 dwg

FIELD: explosives.

SUBSTANCE: invention relates to the method for production of methanol from synthesis gas, including a stage of synthesis gas compression, a stage of catalytic conversion of synthesis gas into methanol in a reactor unit, comprising several catalytic reactors, including operations of heating and conversion of synthesis gas into methanol in each reactor, an operation of reaction products cooling and methanol release after each reactor, an operation of end gases recycling. Besides, the process is carried out under various pressures and with catalysts loaded into reactors with alternating activity under axial and/or radial direction of reagent flow in catalytic reactors in the temperature range of 160-290°C, pressure range of 3-15 MPa, volume speeds of flow 500-10000 hr-1.

EFFECT: method makes it possible to increase efficiency of the process and to produce raw methanol of high quality.

5 cl, 2 ex, 2 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to an oil medium which is suitable for producing dimethyl ether and/or methanol which is used in a synthesis reaction with a suspended layer as a medium which contains a basic component in form of a branched saturated aliphatic hydrocarbon containing 16-50 carbon atoms, 1-7 tertiary carbon atoms, 0 quaternary carbon atoms and 1-16 carbon atoms in branched chains bonded with tertiary carbon atoms; wherein at least one tertiary carbon atom is bonded with hydrocarbon chains with length of 4 or more carbon atoms, lying in three directions. The invention also relates to a method of producing dimethyl ether and a mixture of dimethyl ether and methanol using said oil medium.

EFFECT: use of the present oil medium ensures high efficiency of synthesis.

9 cl, 4 ex, 1 tbl, 1 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a method for thermal oxidation of methane to methanol, involving heating a portion of the initial methane-containing gas from a complex gas treatment plant in a furnace at given pressure and concentration of oxygen in the initial gas of 20-25 vol. %, fed into a reactor into the space behind the jacket of the tubular cooling zone, and from there into the reaction zone where gas-phase oxidation of methane takes place, with subsequent cooling of the reaction mixture in the tubular cooling zone of the reactor, final cooling of the reaction mixture in a cooler-condenser, during which the cooled reaction mixture is divided into waste gases and liquid products to obtain high- and low-pressure vapour and heating water, wherein regulation of the temperature conditions of the reactor is carried out by feeding into the reaction zone of the reactor a portion of the cold initial gas and measuring heating temperature of a portion of the initial gas fed to the input of the tubular part of the cooling zone of the reactor. Air contained in the initial gas is enriched with oxygen to concentration 25-50 vol. %, and the ratio is equal to -(5-15), where is the bulk concentration of methane in the initial gas; is the bulk concentration of oxygen in the initial gas.

EFFECT: method enables to efficiently obtain the end product in one cycle.

1 ex, 3 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to chemistry. A vapour-phase mixture for producing synthetic gas with molar ratio H2O/C equal to at least 2, which contains water vapour and at least one hydrocarbon or an oxygen-containing hydrocarbon with boiling point ranging from -50 to 370°C at atmospheric pressure, is obtained by feeding water vapour into the bottom part of a distillation column and the hydrocarbon or oxygen-containing hydrocarbon into the top part of said distillation column.

EFFECT: invention enables to reduce the content of carbon on the catalyst when producing synthetic gas from said vapour-phase mixture.

3 cl

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing methanol from natural gas, involving heating starting natural gas, obtaining superheated steam from prepared water and mixture thereof with the starting natural gas, single-step conversion of the vapour-gas mixture in a reforming furnace into converted gas, cooling the converted gas and single-step catalytic conversion of the converted gas into methanol in a synthesis reactor, wherein the heat of flue gases from the reforming furnace is used to heat the starting natural gas and the prepared water, superheating the steam and vapour-gas mixture, as well as heating the converted gas before inlet into the synthesis reactor. The invention also relates to apparatus for realising the described method.

EFFECT: use of the present invention increases efficiency of recycling energy from heat flux while simultaneously simplifying the conversion and synthesis processes.

11 cl, 1 tbl, 1 dwg

FIELD: chemistry.

SUBSTANCE: Invention relates to methanol production plant and to method of methanol production by oxidising methane-containing gas at said plant. Proposed plant comprises plant for integrated gas treatment, reactor gas-phase methane-containing gas oxidation consisting of gas-to-gas heat exchanger of reaction zone and gas-to-water heat exchanger of cooling zone, refrigerator-condenser, rectification unit, ecological system and gas burner. Note here that reaction mix maximum heat zone accommodates extra reactor made up of cylindrical tube with feeder of extra portion of cold methane-containing gas including natural gas, refrigerator-condenser communicated via injector with one of gas burner inlets.

EFFECT: higher yield of methanol per 1 m3 of methane in single cycle.

1 ex, 1 dwg

FIELD: chemistry.

SUBSTANCE: method involves partial oxidation of an alkane contained in a gaseous crude stream, which contains an alkane, with oxygen contained in an oxygen-containing crude stream. Said method involves: forming a reactor system, having a back-mixing reaction chamber with injection mixing, which is connected to a tubular flow reactor, wherein said back-mixing reaction chamber with injection mixing ensures dwell time from about 0.05 s to about 1.5 s; feeding said crude stream containing alkanes and said oxygen-containing crude stream into said back-mixing reaction chamber with injection mixing; initiating formation of alkyl free radicals in said back-mixing reaction chamber with injection mixing to obtain a product stream from the back-mixing reaction chamber with injection mixing, containing oxygen, said alkane and at least a portio of said alkyl free radicals; feeding the product stream obtained in the back-mixing reaction chamber with injection mixing into the tubular flow reactor; and converting said product stream obtained in the back-mixing reaction chamber with injection mixing into said alkyl oxygenate in said tubular flow reactor; where said alkane is selected from group consisting of methane, ethane, propane and butane.

EFFECT: invention enables to obtain the end product using an efficient and cheap method without using a catalyst.

34 cl, 2 ex, 36 dwg

FIELD: chemistry.

SUBSTANCE: present invention relates to a method of producing methanol by bringing a feed stream rich in hydrogen and carbon monoxide in a reactor into contact with a methanol synthesis catalyst to obtain a process stream, followed by cooling thereof, condensation and separation into a gas phase and a liquid phase with crude methanol. The feed stream used is cleaned gas which is obtained by direct-flow gasification of wood processing wastes. The feed stream is enriched with hydrogen by controlled electrolysis of recycled water before bringing the feed stream into contact with a catalyst containing the following, wt %: copper oxide 62, zinc oxide 31, aluminium oxide 7. The feed stream is compressed to pressure of 4.5-5 MPa and then divided into two streams. One stream is fed into the reactor onto the catalyst for contacting through a heat exchanger which simultaneously cools the process stream. The other stream is fed directed onto the catalyst for contacting and reaction temperature is maintained at 250-270°C. After final cooling of the process stream in the still residue of the distillation apparatus, it is separated by throttling into a gas phase and a liquid phase. After separation, the gas phase is divided into two streams. One stream is fed for oxidation into a direct-flow gasifier and the other is mixed with the feed stream before compression.

EFFECT: invention enables to obtain the desired product via a wasteless method using one readily available catalyst.

1 dwg

FIELD: explosives.

SUBSTANCE: invention relates to the method for production of methanol from synthesis gas, including a stage of synthesis gas compression, a stage of catalytic conversion of synthesis gas into methanol in a reactor unit, comprising several catalytic reactors, including operations of heating and conversion of synthesis gas into methanol in each reactor, an operation of reaction products cooling and methanol release after each reactor, an operation of end gases recycling. Besides, the process is carried out under various pressures and with catalysts loaded into reactors with alternating activity under axial and/or radial direction of reagent flow in catalytic reactors in the temperature range of 160-290°C, pressure range of 3-15 MPa, volume speeds of flow 500-10000 hr-1.

EFFECT: method makes it possible to increase efficiency of the process and to produce raw methanol of high quality.

5 cl, 2 ex, 2 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to an oil medium which is suitable for producing dimethyl ether and/or methanol which is used in a synthesis reaction with a suspended layer as a medium which contains a basic component in form of a branched saturated aliphatic hydrocarbon containing 16-50 carbon atoms, 1-7 tertiary carbon atoms, 0 quaternary carbon atoms and 1-16 carbon atoms in branched chains bonded with tertiary carbon atoms; wherein at least one tertiary carbon atom is bonded with hydrocarbon chains with length of 4 or more carbon atoms, lying in three directions. The invention also relates to a method of producing dimethyl ether and a mixture of dimethyl ether and methanol using said oil medium.

EFFECT: use of the present oil medium ensures high efficiency of synthesis.

9 cl, 4 ex, 1 tbl, 1 dwg

FIELD: process engineering.

SUBSTANCE: invention relates to multireactor system and method of production by equilibrium-limited reaction. System comprises reaction vessel to sustain working temperatures and pressures of reactions. Note here that said vessel has multiple reaction zones made by separation walls, separation tank to sustain said temperatures and pressures. Note also that said separation tank has multiple separation zones made by separation walls and reaction sets comprising multiple heat exchangers for feed-and-discharge flows. Note that heat exchanger of first reactor set interacts with reaction zone via feed flow while heat exchangers of the other reactor sets interact with reaction zone via return flow.

EFFECT: higher efficiency of methanol cascade system.

20 cl, 7 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing methanol from natural gas, involving heating starting natural gas, obtaining superheated steam from prepared water and mixture thereof with the starting natural gas, single-step conversion of the vapour-gas mixture in a reforming furnace into converted gas, cooling the converted gas and single-step catalytic conversion of the converted gas into methanol in a synthesis reactor, wherein the heat of flue gases from the reforming furnace is used to heat the starting natural gas and the prepared water, superheating the steam and vapour-gas mixture, as well as heating the converted gas before inlet into the synthesis reactor. The invention also relates to apparatus for realising the described method.

EFFECT: use of the present invention increases efficiency of recycling energy from heat flux while simultaneously simplifying the conversion and synthesis processes.

11 cl, 1 tbl, 1 dwg

FIELD: chemistry.

SUBSTANCE: in order to produce synthetic gas containing hydrogen and carbon monoxide, starting material containing methane undergoes partial oxidation using a multichannel burner fitted with a system of separate channels. Methane-containing material, at temperature higher than 500°C, flows through one channel of the burner and oxidising gas flows through another channel. The channel for the methane-containing material and the channel for the oxidising gas are separated from each other by a channel through which a second gas containing hydrogen, carbon monoxide and/or hydrocarbon flows, where the second gas is at temperature 10°C lower than its spontaneous ignition temperature. The second gas is obtained from gaseous by-products of a Fischer-Tropsch synthesis process or from gaseous by-products of a methanol synthesis process.

EFFECT: improved process.

22 cl, 2 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a methanol synthesis method, during realisation of which natural gas and water vapour are fed into a primary conversion section where the two interact to form a gaseous mixture containing CO, CO2, H2 in stoichiometric excess and CH4. Said gaseous mixture containing CO, CO2, H2 in stoichiometric excess and CH4 is fed into a methanol synthesis section where a reaction takes place to produce methanol and the gas stream containing CO, CO2, H2 and CH4 is collected from the methanol synthesis section by blowing. H2 is extracted from the gas stream collected from the methanol synthesis section to obtain a first gaseous phase primarily consisting of H2, and a second gaseous phase containing CO, CO2, H2 and CH4 and essentially not containing H2. The second gaseous phase containing CO, CO2, H2 and CH4 and essentially not containing H2 is then recuperated for use in the conversion process in the primary conversion section. Nitrogen is first removed from natural gas before feeding the natural gas into the primary conversion section. The invention also relates to apparatus for realising the disclosed method.

EFFECT: obtaining end product with high efficiency at low operational and capital expenses and low power consumption.

8 cl, 1 dwg, 1 ex

Methanol synthesis // 2408567

FIELD: chemistry.

SUBSTANCE: present invention relates to a methanol synthesis method involving the following steps: (i) reforming hydrocarbon starting material and separation of water from the resulting mixture with gas reforming to obtain freshly prepared gas containing hydrogen and carbon oxides, where the said mixture with freshly prepared gas has stoichiometric coefficient R defined by the formula: R=([H2]-[CO2])/([CO2]+[CO]), which is less than 2.0; (ii) formation of a mixture of synthetic gas consisting of a stream of said freshly prepared gas, unreacted synthetic gas and hydrogen; (iii) passing the mixture with synthetic gas at high temperature and pressure through a methanol synthesis catalyst bed to obtain a stream of product containing methanol and unreacted synthetic gas; (iv) cooling said stream of product with extraction of a stream of crude methanol from said unreacted synthetic gas; (v) removal of a portion of said unreacted synthetic gas as blowout gas, and (vi) feeding the remaining unreacted synthetic gas to step (ii). Hydrogen is extracted from at least a portion of said blowout gas and a portion of said freshly prepared gas and the extracted hydrogen is added to the mixture with synthetic gas.

EFFECT: disclosed method lowers volume of catalyst and amount of wastes, reduces size of reactors and simplifies purification of crude methanol, which lowers cost of the process.

12 cl, 3 ex, 3 dwg

FIELD: chemistry.

SUBSTANCE: method of preparing a mixture of hydrogen and carbon monoxide from a gaseous mixture of hydrocarbons containing methane, ethane and optionally hydrocarbons with a large number of carbon atoms involves the following steps: (a) preliminary reforming of the mixture of hydrocarbons in the presence of a suitable reforming catalyst with conversion of ethane and optionally hydrocarbons with a large number of carbon atoms to methane, carbon dioxide and hydrogen, (b) heating the gaseous mixture obtained at step (a) to temperature of 750-900°C, (c) partial oxidation by bringing the heated mixture obtained at step (b) into contact with an oxygen source in the burner of the reactor to obtain a reaction stream. The mixture of hydrogen and carbon monoxide obtained at step (c) is used at step (d) for Fischer-Tropsch synthesis, in which gas containing hydrogen and carbon monoxide obtained at step (c) is converted at one or more steps at least partially to liquid hydrocarbons in the presence of a Fischer-Tropsch type catalyst which contains at least one metal or a metal compound selected from group eight of the periodic table of elements.

EFFECT: invention reduces oxygen consumption.

10 cl, 2 dwg, 4 tbl, 4 ex

FIELD: chemistry.

SUBSTANCE: invention relates to chemistry. stream of methanol material reacts with oxygen and optionally a temperature regulator in a partial oxidation reactor to obtain a stream of synthetic gas. The partial oxidation reactor has a burner in an open uncatalysed gas generator with free flow and works in the 1100-2000 °C temperature interval. The synthetic gas stream is divided into a stream with high carbon dioxide content and a mixed stream containing hydrogen and carbon oxide which is then divided into a stream with high hydrogen content and a stream with high carbon oxide content. Re-equipment of the initial installation for producing methanol to an installation for synthesis of acetic acid involves the following steps: provision for the initial installation for producing methanol, having at least one partial oxidation reactor for converting hydrocarbon into a synthetic gas stream and a methanol synthesis loop for converting hydrogen and carbon oxide from the synthetic gas stream to methanol, supply of at least one portion of methanol material stream, oxygen from an air separation unit and, optionally, a temperature regulator, into at least one partial oxidation reactor, mounting the first separation unit for separating a stream with carbon dioxide content and a mixed stream of hydrogen and carbon oxide from the outgoing synthetic gas stream, mounting the second separation unit for separating a stream with high hydrogen content and a stream with high carbon oxide content from the mixed stream, mounting the acetic acid synthesis installation, supplying a stream with high carbon oxide content from the second separation unit and a portion of methanol material stream into the acetic acid synthesis installation and fitting isolation valves for isolation of the methanol synthesis loop from the remaining part of the reconstructed installation.

EFFECT: invention increases cost-effectiveness of the process.

18 cl, 10 dwg

FIELD: process engineering.

SUBSTANCE: proposed device comprises means for direct conversion composed of production means and/or at least one reactor for continuous industrial production, device for intake and/or production of initial matters and/or products as well as conversion control devices. Note here that said means are integrated in single and mobile functional assy that makes an infrastructure and, preferably, is made as a standard transport container.

EFFECT: universal infrastructural device, higher safety.

14 cl, 1 dwg

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