Installation and the method of production of the synthesis- gas from the natural gas

FIELD: chemical industry; installations and the methods of production of the synthesis-gas from the natural gas.

SUBSTANCE: the invention is pertaining to the field of chemical industry, in particular, to the installation and the method for simultaneous production from the natural gas of the methanol synthesis-gas, the ammoniac synthesis-gas, carbon monoxide and carbon dioxide. The installation consists of the in-series connected to each other assembly units and includes: the first reactor (A), in which at feeding of oxygen realize the transformation of the natural gas into the synthesis gas consisting of carbon monoxide, carbon dioxide, hydrogen and the steam; the second reactor (B), in which exercise the regular transformation of carbon monoxide into carbon dioxide; if necessary the compressor (C) using which the formed gases may be contracted; absorbing apparatus D, which serves for absorption of carbon dioxide and production of he mixture of monoxide with hydrogen used for synthesizing methanol; the refrigerating separator E, in which at feeding of the liquid nitrogen receive the ammoniac synthesis gas and simultaneously produces carbon monoxide, argon and methane. The invention allows to increase profitability of the installation due to production at one installation of several products.

EFFECT: the invention ensures the increased profitability of the installation due to production at one installation of several products.

15 cl, 1 dwg, 1 tbl

 

The objects of the invention are installation and method for the simultaneous generation of synthesis gas, for example, methanol synthesis gas, ammonia synthesis gas, carbon monoxide and carbon dioxide by separation from natural gas of the gas mixture.

It is known that for the production of methanol, ammonia, pure carbon monoxide, carbon dioxide and other synthesis gas must be constructed corresponding production units, each of which can be synthesized, as a rule, only one of these gases [2 and 3]. Methods for the simultaneous production of methanol and ammonia only became known from German patent application DE-OS 3336649, Japanese patent application JP 2000063115 and European patent 0853608. Suitable for this path, with important technical value, includes the transformation of natural gas into synthesis gas, which as a major component parts contains carbon monoxide, carbon dioxide and hydrogen. Methods of obtaining synthesis gas is described, for example, in German patent application DE-OS 3345064 and European patent application EP-A-0999178.

However, from an economic point of view would be highly advantageous if it were possible to make a complete separation of the constituent parts of the synthesis gas on a specific production installation, so that you could get on one individual item is poizvodstvennaja line with high purity methanol synthesis gas, ammonia synthesis gas, carbon monoxide and carbon dioxide, suitable for direct use in subsequent chemical syntheses. Such a combined device for separation of gases would have especially high profitability, not only because of savings due to increased volumes generated by the products, but also due to the fact that instead of several units, each of which focused on the production of only one product, it would take a few nodes that are included with only one single installation. This setup could have a particularly high efficiency in the case, if she had so flexible design to volumes produced on her gas could meet the needs of these gases.

It was found that the above requirements can be met by setting intended for simultaneous reception from natural gas methanol synthesis gas, ammonia synthesis gas, carbon monoxide and carbon dioxide, which is a separate production line, including the following, sequentially connected to each other nodes:

the first reactor And in which when the oxygen supply carry out the conversion of natural gas into synthesis gas consisting of carbon monoxide, dioxide angle of the ode, hydrogen and water;

the second reactor, in which regulated the conversion of carbon monoxide to carbon dioxide;

- if necessary, the compressor, whereby the resulting gases can be subjected to compression;

- absorber D, which serves to absorb carbon dioxide and a mixture monoxide with hydrogen used for methanol synthesis;

- refrigeration separator E, which when the supply of liquid nitrogen to get the ammonia synthesis gas and simultaneously emit carbon monoxide, argon and methane.

Technological scheme shown symbolically in the drawing.

The first reactor And is designed to produce synthesis gas and allows the desulfurization of flowing the gas mixture, its saturation with water vapor, the heating of the heater with the catalytic cleavage of long-chain hydrocarbons to methane, partial oxidation with oxygen, as well as cooling gas with steam. A node of this type, also called the reactor Period (catalytic partial oxidation = catalytic partial oxidation - eng.), often used in the installations, and its description is given in the literature (Hermann Göhna, "Concepts for Modern Methanol Plants." Proceedings of the 1997 World Methanol Conference, Tampa, Florida, USA (December 1997)). We are talking about a cylindrical tank with a vertical convex walls. In the upper part of the reservoir Ave is usmotreny burner or mixer, in which pipes enter mixed with water vapor, natural gas, steam and oxygen. Burner or mixer provide intensive mixing of the three gas flows in the upper part of the tank, where very high speed is realized main phase partial oxidation of natural gas. Next, the hot gases pass through located in the lower part of the tank catalyst, where the transformation of natural gas. Catalytic partial oxidation can be described by the following chemical equations:

In the reactor And enter this amount of water vapor that the molar ratio of water vapor to the unoxidized hydrocarbons ranged from 1.4 to 3.0, preferably of 1.7. In the reactor And enter this amount of oxygen that the molar ratio of oxygen to oxygenated hydrocarbons ranged from 0.45 to 0.7, preferably 0,52. In practice, the exact quantity of the injected oxygen is set so that the temperature coming out of the reactor And the gas mixture was in the range of from 900 to 1050°With, in the General case 950°C. the purity of the oxygen is bound with installation for air separation F (see drawing), in the General case is in the range from 90 to 99.5%, but usually 99.5%. In the reactor, And using a catalyst based on Nickel oxide, for example, catalyst type G-31E, G-90LDP or G-90B, which can be purchased from the firm Süd-Chemie AG (München). Turning natural gas into synthesis gas is under pressure from 20 to 100 bar, preferably under a pressure of about 40 bar.

The reactor And connected to the second reactor, in which you can regulate the formation of carbon dioxide from carbon monoxide while generating hydrogen. The reactor is equipped with a bypass pipe through which obtained in the first reactor And the synthesis gas may be fully or partially skipped past the reactor, which allows you to adjust the degree of its transformation. In a reactor in the presence of high-temperature catalysts for the oxidation of carbon monoxide to carbon dioxide in the form of a single-stage or two-stage process with intermediate cooling.

If there was no demand in the carbon dioxide or minor requirements obtained in the reactor And the synthesis gas is directed past the reactor and then through the pipeline [4] directly into the compressor, where the gas mixture may be subjected to compression. The function of the compressor is to increase the pressure of the images is of segosa in the reactor And gas up to 60-100 bar, in the General case, up to 80 bar. However, if the pressure is withdrawn from the reactor And the gas exceeds 40 bar, you can refuse the use of the compressor C. Used in this case, the compressor is a known device commonly used in many chemical plants.

After the compressor With the gas mixture through the pipeline [5] is sent to the absorber D, which is extracted from the gas mixture of carbon dioxide. Carbon dioxide can be extracted both physical and chemical methods. In physical absorption of carbon dioxide is absorbed by cold methanol or cold glycol ether. The chemical absorption of carbon dioxide is absorbed preferentially by alkanolamines, sodium carbonate or other alkaline substance. Absorber D preferably includes two reaction stages, with the first reaction stage carried out gross emissions of carbon dioxide to a residual molar concentration of from 1 to 10 wt.%, (in terms of dry gas, preferably carbon dioxide to remove residual content of 2.2 wt.% At the second stage of absorption of the remainder of the carbon dioxide to remove residual molar concentration less than 50 parts per million, preferably less than 10 parts per million in Addition, the absorber D contains a device for controlled lowering of the pressure contained in the absorbent is gas, so you can regenerate carbon dioxide. In addition, the absorber D contains a device for the regeneration of the absorbent by heating device to maintain the constancy of the composition of the adsorbent, as well as to establish a pressure contained in the solvent gas to the desired process value. Regenerated as indicated above, the carbon dioxide may be fully or partially used in the subsequent syntheses, for example, to obtain a urea. Excess carbon dioxide can be discharged into the atmosphere. The literature describes various methods of removing carbon dioxide ("Gas Production", Ullmans''s Encyclopedia of Industrial Chemistry, Vol.A12, VCH Verlagsgesellschaft mbh (1989; Max App Ammonia, Methanol, Hydrogen, Carbon Monoxide, Modern Production Technologies. British Sulphur Publishing - a Division of CRU Publishing Ltd, 31 Mount Pleasant, London WC1X0AD.ISBN 1673387261 (published 1997; Emil Supp "How to produce Methanol from Coal". Springer-Verlag (1990).

Next, the gas mixture, freed from carbon dioxide by pipeline [7] send in the cooling separator E, in which by introducing liquid nitrogen undertake partial condensation and the allocation of carbon monoxide and hydrogen. This method is described in the simultaneously filed German patent application ...(L1P13)... This way we obtain a methanol synthesis gas consisting of carbon monoxide and hydrogen. The purity obtained in the refrigeration separate the e of carbon monoxide can be further improved by washing methane.

Received in the refrigeration separator E. carbon monoxide may also be directed to the installation for the production of acetic acid by carbonylation of methanol.

Admixtures of methane and argon is extracted by washing with nitrogen in the cooling separator E, and can be used as fuel gas for heat production in the reactor A.

Cold separator s gas is cooled to a temperature between -200°and -150°C. the Gas at the same temperature is subjected to instantaneous evaporation in one or more evaporative cylinders, allowing the hydrogen is separated from the carbon monoxide. When the instantaneous evaporation of the first formed is enriched in carbon monoxide liquid hydrogen. To extract methane gas carbon monoxide is washed with liquid carbon monoxide and then heated to room temperature. Hydrogen is passed through the second wash column, where it is washed with liquid nitrogen to remove traces of carbon monoxide, argon and methane. Next, to get suitable for ammonia synthesis gas mixture, set the molar ratio of hydrogen and nitrogen of 3:1.

Refrigeration separator E also includes molecular sieve designed to highlight traces of carbon dioxide before the low-temperature separation of gas and, consequently, to produce synthesis gas, the e containing carbon dioxide. Refrigeration separator E is also known, is described in detail in the literary source device (W L E Davey "Cold Box for The Production of Multiple Products from a Stream of Syngas". German Patent Application (2002) (L1P13).

In the drawing, the node F is a typical installation for air separation, providing flow oxygen with a purity between 90 and 99.5%. In addition, the node F receives the nitrogen purity than 99,995%.

Gases generated by the system according to the invention as described above have such a high purity that can be used in further chemical syntheses.

The performance of the installation according to the invention, designed to receive the following amounts of products, and implemented on the installation method of separating a synthesis gas shown in the following example.

a) Required to synthesize 4000 tons of methanol per day, part of which is used to produce acetic acid. For the synthesis of methanol required synthesis gas of the following composition: stoichiometric coefficient of Sn=2,05, the concentration of carbon dioxide in the range from 2%to 3%, the nitrogen concentration less than 0.5%. Stoichiometric factor (Sn) calculated using the following formula:

While [N2][CO2] and [CO2] [] Denote the molar concentration of hydrogen dioc the IDA and carbon monoxide in the synthesis gas.

b) Simultaneously on the same installation can be derived synthesis gases for the synthesis of 1200 tons of acetic acid per day. For the synthesis of acetic acid required methanol and carbon monoxide with a purity of at least 98%.

(C) Simultaneously on the same installation can be derived synthesis gases for the synthesis of 4000 tons of ammonia per day, part of which is used for the synthesis of urea. For the synthesis of ammonia required a mixture of hydrogen and nitrogen with a molar ratio of 3:1, and this gas mixture should contain less than 10 parts per million of oxygen.

and Finally, on the same setup can also be obtained synthesis gases for the synthesis of 6,270 tons of urea per day. For the synthesis of urea needed fresh ammonia and carbon dioxide with a purity greater than 98.5 per cent.

These requirements can be met by implementing the following sequence of technological operations, and the composition of separate gas flows presented in the table.

1. Synthesized from natural gas crude synthesis gas is produced in the reactor And by setting the pressure at a level of about 45 bar. Coming out of the reactor And the synthesis gas has the composition [2];

2. Approximately 82% of the crude synthesis gas reactor in the form of a gas stream [3] skip past the reactor, while 18% crude synthesis gas is sent to the reactor for controlled turning of monoo the sid of carbon in carbon dioxide. Coming out of the reactor In the gas stream [4] combined with the gas stream [3].

3. The cooled and condensed gas stream [4] is compressed by the compressor to a pressure of about 80 bar.

4. The compressed gas is sent to the absorber D, from which, after reaching the average degree of saturation of the adsorbent with carbon dioxide and decrease concentration of carbon dioxide almost to 2.2% divert approximately 43% of the synthesis gas. The composition of the exhaust synthesis gas corresponds to the composition of the gas stream [6]. From the rest of the gas by fine treatment at the second stage of absorption extract carbon dioxide to a residual concentration of less than 10 parts per million of free gas in the form of a gas stream [7] send in the cooling separator E.

5. Cold separator S from synthesis gas to remove carbon monoxide, which is directed to the synthesis of acetic acid in the form of a gas stream [10] or on the synthesis of ammonia in a gas stream [11], and also set aside in the form of the residual gas stream [8], and the gas flow [8] combined with a methanol synthesis gas, receiving the gas flow [9]. Contained in the synthesis gas impurities, in particular methane, argon and carbon monoxide, is extracted and sent as a fuel gas in the reactor A.

6. Obtained in the absorber D carbon dioxide in the form of material flow [15] is used for the synthesis of urea.

The above-described divided the e synthesis gas on a separate install on multiple individual fractions is only one example, demonstrating the infinite possibilities of obtaining the gas compositions for specific chemical syntheses carried out by combining the nodes included in the installation according to the invention, and the method of chemical transformations. Through the conversion and modification of individual components and process steps implemented on a separate installation of natural gas can be obtained also special gas mixture suitable for the implementation of other important syntheses, for example, Fischer-Tropsch synthesis, synthesis of oxaspiro, etilenglikola, and other processes.

1. Installation for simultaneous receipt of natural gas methanol synthesis gas, ammonia synthesis gas, carbon monoxide and carbon dioxide, characterized in that a separate production line, consisting of serially interconnected nodes includes

the first reactor And in which when the oxygen supply carry out the conversion of natural gas into synthesis gas mixture comprising carbon monoxide, carbon dioxide, hydrogen and water vapor;

the second reactor, in which regulated the conversion of carbon monoxide to carbon dioxide;

the absolute is ber D, which serves to absorb carbon dioxide and a mixture monoxide with hydrogen used for methanol synthesis;

refrigeration separator E, which when the supply of liquid nitrogen to get the ammonia synthesis gas and simultaneously emit carbon monoxide, argon and methane.

2. Installation according to claim 1, characterized in that it includes a compressor, through which can be compressed resulting in reactors a and b gases.

3. Installation according to claim 1 or 2, characterized in that the catalytic partial oxidation of natural gas to the reactor And provided with a pipeline for input natural gas, water vapor and oxygen.

4. Installation according to claim 1, wherein the second reactor is equipped with a bypass pipeline [3], through which is received in the first reactor And the synthesis gas can be fully or partially to skip past the reactor and, consequently, to adjust the degree of oxidation, in particular the formation of carbon dioxide from carbon monoxide.

5. Installation according to claim 2, characterized in that includes a compressor, through which can be set gas pressure, providing the possibility of physical or chemical absorption of carbon dioxide in the absorber D.

6. Installation according to claim 1, characterized in that the absorber D is supplied by pipeline to enter the synthesis gas and pipelines for features is and consisting of carbon monoxide and hydrogen methanol synthesis gas, carbon dioxide released from carbon dioxide, synthesis gas, and gases of the corresponding composition suitable for other syntheses.

7. Installation according to claim 1, characterized in that the cooling separator E is supplied by pipelines to enter freed from carbon dioxide, synthesis gas, and liquid nitrogen, and piping for removal of ammonia synthesis gas, net of carbon monoxide, combustible gas containing methane, argon and carbon monoxide and containing carbon monoxide and hydrogen in the liquid.

8. Way to simultaneously obtain a methanol synthesis gas, ammonia synthesis gas, carbon monoxide and carbon dioxide from natural gas by filing for the installation according to claims 1-7 of water vapor and oxygen, characterized in that the molar ratio of water vapor to the oxygenated hydrocarbons in the first reactor is from 1.5 to 3.0, preferably of 1.7.

9. The method according to claim 8, characterized in that the molar ratio of oxygen to oxygenated hydrocarbons in the first reactor is from 0.45 to 0.7, preferably 0,52.

10. The method according to claim 8, characterized in that for the conversion of natural gas into synthesis gas using a catalyst containing Nickel oxide.

11. The method according to claim 8, characterized in that for the conversion of natural gas into synthesis gas using pressure from 25 to 100 bar, preferably the pressure is s about 40 bar.

12. The method according to claim 8, characterized in that for the oxidation of carbon monoxide to carbon dioxide in the second reactor in the presence of high-temperature catalysts perform a single-stage or two-stage process with intermediate cooling.

13. The method according to claim 8, characterized in that the pressure obtained in the reactors And In the synthesis gas through the compressor is set in the range from 60 to 100 bar, preferably 80 bar.

14. The method according to claim 8, characterized in that the absorber D from synthesis gas in one or more stages by chemical or physical release carbon dioxide.

15. The method according to claim 8, characterized in that the synthesis gas is cooled in the separator by introducing liquid nitrogen to a temperature of -150 to -200°s, thanks To emit methane, argon and carbon monoxide and residual hydrogen gas is mixed with nitrogen in a molar ratio of 3:1 to produce ammonia synthesis gas.



 

Same patents:

FIELD: chemical industry; methods of production of hydrogen and a methanol.

SUBSTANCE: the invention is pertaining to the method of production of the industrial hydrogen and methanol from the converted gas consisting mainly of CO2, H2. The method of production of hydrogen and methanol from the converted gas containing carbon oxides and hydrogen includes the synthesis of methanol. For execution of the methanol synthesis feed the converted gas with the volumetric ratio of H2-CO2/CO+CO2, equal to 2.03-5.4, which is conducted in the reactor system including the flow reactor or the cascade of the floe reactors and / or the reactor with the recycle of the gas mixture with production of methanol, the unreacted gas and the blow-down gas. At that the mixture of the unreacted and converted gases is fed for purification from carbon carbon dioxide with its extraction and batch feeding of the carbon dioxide into the converted gas delivered for the synthesis of methanol. The blow-down gases are subjected to the fine purification from the impurities with production of hydrogen. The invention allows to upgrade the method due to maximum usage of the carbon dioxide.

EFFECT: the invention ensures improvement of the method of production of hydrogen and a methanol due to maximum usage of the carbon dioxide.

2 cl, 1 dwg, 1 tbl, 5 ex

FIELD: industrial organic synthesis and chemical engineering .

SUBSTANCE: invention relates to a process of producing liquid oxygenates, including methanol, C2-C4-alcohols, formaldehyde, lower organic acids, or mixtures thereof, and to installation for implementation the process. Process comprises successively supplying natural gas from complex gas preparation plant to a series of "gas-gas" heat exchangers and into annular space of at least one tubular reaction zone of reactor, wherein natural gas is heated to temperature of the beginning of reaction, whereupon heated gas is passed to the entry of the tubular reaction zone mixer, into which compressed air or oxygen is also injected to provide gas-phase oxidation in reaction zone of reactor. Resulting reaction mixture is discharged from reactor into a series of "gas-liquid" and "gas-gas" heat exchangers, wherein reaction mixture is cooled to ambient temperature and sent to separator, wherefrom liquid phase is passed through lower carboxylic acid recovery vessel to the system of rectification columns to isolate the rest of mixture components, whereas leaving gas is recycled to complex gas preparation plant. More specifically, oxidation is carried out within temperature range 240 to 450°C and pressure from 2 to 10 MPa at residence time of reaction mixture in reactor 2-6 sec and oxidant concentration 2 to 15 wt %. In reactor having mixers hollow and at least one tubular reaction zones, required temperature is maintained constant throughout all length of tubular reaction zone and at entries for compressed air or oxygen in mixers of each of tubular reaction zones and hollow reaction zone. Liquid oxygenate production plant is composed of aforesaid complex gas preparation plant, a series of "gas-gas" heat exchanger to heat natural gas, reactor, a series of "gas-liquid" and "gas-gas" heat exchangers to cool reaction mixture obtained in reactor, gas-liquid separator, lower carboxylic acid recovery vessel, and system of rectification columns to isolate the rest of products.

EFFECT: enabled implementation of the process directly near gas and gas condensate deposits, increased conversion of methane per one passage through reactor, and increased yield of oxygenates due to improved design of plant.

6 cl, 1 dwg, 1 tbl

FIELD: industrial organic synthesis catalysts.

SUBSTANCE: invention relates to copper-containing catalysts for low-temperature synthesis of methanol in fluidized bed at high pressure and provides catalyst, whose preparation involves impregnation and which contains oxides of copper, zinc, chromium, magnesium, aluminum, boron, and barium and has following molar ratio: CuO:ZnO:Cr2O3, MgO:Al2O3:B2O3:BaO = 1:(0.7-1.1):(0.086-0.157):(0.05-0.15):(0.125-0.2):(0.018-0.029):(0.04-0.075).

EFFECT: increased mechanical strength and wear resistance of catalyst.

1 tbl

FIELD: industrial organic synthesis catalysts.

SUBSTANCE: invention relates to copper-containing catalysts for low-temperature synthesis of methanol in fluidized bed at low pressure and provides a wear-resistant catalyst, whose preparation involves impregnation and which contains oxides of copper, zinc, chromium, magnesium, aluminum, and boron and has following molar ratio: CuO:ZnO:Cr2O3, MgO:Al2O3:B2O3 = 1:0.3:(0.15-0.2):(0.1-0.025):(0.25-0.3):(0.08-0.1).

EFFECT: increased mechanical strength and wear resistance of catalyst.

1 tbl

FIELD: industrial organic synthesis catalysts.

SUBSTANCE: invention relates to copper-containing catalysts for low-temperature synthesis of methanol in fluidized bed at median pressure and provides catalyst, whose preparation involves impregnation and which contains oxides of copper, zinc, chromium, magnesium, aluminum, boron, and barium and has following molar ratio: CuO:ZnO:Cr2O3, MgO:Al2O3:B2O3:BaO = 1:0.3:(0.014-0.038):(0.047-0.119):(0.05-0.1):(0.007-0.014):(0.0292-0.054).

EFFECT: increased mechanical strength and wear resistance of catalyst.

1 tbl

FIELD: industrial organic synthesis.

SUBSTANCE: invention relates to improved process of producing methanol from purge gas produced in basic methanol or ammonia synthesis. Process comprises dispensing compressed carbon dioxide into basic synthesis purge gas, heating resultant gas mixture to starting synthesis temperature, passing thus heated gas through methanol synthesis catalyst, cooling reacted gas, recovering condensed crude methanol, and separating non-condensed gas stream into return stream and purge stream, the former being designed for mixing with basic synthesis purge gas stream and passed to one or two circulation jet compressors. Circulation is effected by energy provide either by (i) pressure of basic synthesis purge gas, which is supplied to jet compressor and further dispensed into compressed carbon dioxide stream, or by (ii) pressure of compressed carbon dioxide, which is dispensed into jet compressor and then introduced into basic synthesis purge gas stream, or by (iii) pressure of basic synthesis purge gas and pressure of indicated compressed carbon dioxide, both being supplied to one or two jet compressors. Ammonia or methanol production purge gas is successfully used for production of methanol without utilizing additional hydrogen-containing streams.

EFFECT: reduced methanol production cost.

4 cl, 5 dwg, 1 tbl, 4 ex

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to a new method for preparing methanol and other aliphatic alcohols by gas-phase interaction of hydrocarbon gases with water vapor under effect of ultraviolet radiation. Methanol and other aliphatic alcohols are prepared by direct hydroxylation of hydrocarbon gas or mixture of hydrocarbon gases with water vapor. For this aim hydrocarbon gas and vapor or mixture of gases and vapor are fed into reactor wherein the reaction mass is subjected for effect of ultraviolet radiation in wavelength range 240-450 nm at temperature lower vapor formation point. The end product is isolated from vapor-gaseous mixture by condensation and unreacted gas or mixture of gases removed from the reaction zone is purified from the end product by bubbling through water layer and recovered into reactor by adding the parent gaseous component in the amount equal to consumed one. The process is carried out for a single stage and can be realized under atmosphere pressure. Invention can be used in chemical, petroleum chemical, petroleum processing and petroleum and gas extracting industry.

EFFECT: improved preparing method.

2 cl, 1 tbl, 8 ex

FIELD: organic chemistry, chemical technology.

SUBSTANCE: method for synthesis of methanol involves the following stages: removing hydrocarbon gas to be processed, sulfur elimination, catalytic steam conversion to obtain converted gas, heat utilization with separation of water, synthesis of methanol and separation of condensed methanol. Hydrocarbon gas with unstable composition is removed under pressure 0.001 MPa, not less, and sulfur elimination of hydrocarbon gas with unstable composition is combined with stage of step-by-step stabilization of pressure to form steam-gaseous mixture. Methanol synthesis is carried out for at least two successive flow steps with reducing volume of catalyst under pressure 1.5 MPA, not less, and separation of methanol between successive stages. Method provides significant reducing cost of gas processing and service of devices and allows carrying out the processing in mobile traveling devices in field conditions. Invention can be used in processing gas with unstable composition, for example, casing-head petroleum gas in petroleum-extracting holes, in field conditions in small traveling devices.

EFFECT: improved preparing method.

2 cl, 2 dwg

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to the improved method for preparing methanol. Method involves the successive feeding hydrocarbon-containing gas, injection of chemically purified water, carrying out the preliminary steam reforming for preparing synthesis gas and carrying out the final reforming if formed gas with addition of oxygen under pressure for carrying out synthesis of methanol, heating reactor for preliminary reforming by flow of obtained synthesis gas going out from reactor for the final reforming that is fed to intertubular space of reactor for preliminary reforming followed by cooling synthesis gas obtained as result of reforming by vapor-gas mixture and carrying out synthesis of methanol in 2-step reactor. Cooling the reaction mixture for carrying out isothermal reaction for synthesis of methanol in intermediate external heat exchanger of two-step reactor is carried out with vapor-gas mixture and cooling flow going out from reactor for synthesis of methanol is carried out with vapor-gas mixture and chemically purified water. Also, invention relates to unit for preparing methanol including the source of hydrocarbon-containing gas and unit for complex preparing gas, reactor for preliminary vapor reforming heated with flow going out from reactor for final reforming, two-step reactor for synthesis of methanol, heat exchangers for cooling synthesis gas, heat exchangers for cooling flow going out from reactor for synthesis of methanol, separator for separation of reaction products and exhausting gases and crude methanol. The unit for preparing methanol is assembled with unit for complex gas preparing including block for preparing chemically purified water, block for preparing raw, additional manufacture involving torch making, cleansing constructions, sources of electric energy, air of control and measuring instruments and automatic equipment, chemical laboratory and operating block. Two-step reactor for synthesis of methanol joined with heat exchanger for cooling synthesis gas with vapor-gas mixture, intermediate external heat exchanger for cooling the reaction mixture with vapor-gas mixture is joined in-line with heat exchanger for cooling flow obtained in reactor with vapor gas mixture, heat exchanger for cooling of chemically purified water and separator for separation of reaction products. Ignition device is assembled in reactor for final reforming that promotes to carry out the start of unit without trigger furnace. Water is injected in flow hydrocarbon gas directly before heat exchanger for the reaction mixture that provides excluding boiler-utilizer and trigger boiler from schedule and to solve the problem for cooling the reaction mixture in reactor for synthesis of methanol also. Based on integration of the device for preparing methanol in technological schedule with unit for complex preparing gas and significant change of the conventional schedule for preparing methanol method provides 3-fold reducing capital investment.

EFFECT: improved method for preparing methanol.

2 cl, 1 dwg

FIELD: technology for production of methanol from syngas.

SUBSTANCE: claimed method includes mixing of hydrocarbon raw material with water steam to provide syngas by steam conversion of hydrocarbon raw material and subsequent methanol synthesis therefrom. Conversion of hydrocarbon raw material and methanol synthesis are carried out under the same pressure from 4.0 to 12.0 MPa. In one embodiment hydrocarbon raw material is mixed with water steam and carbon dioxide to provide syngas by steam/carbonic acid conversion of hydrocarbon raw material in radial-helical reactor followed by methanol synthesis therefrom under the same pressure (from 4.0 to 12.0 MPa). In each embodiment methanol synthesis is carried out in isothermal catalytic radial-helical reactor using fine-grained catalyst with grain size of 1-5 mm. Methanol synthesis is preferably carried out in two steps with or without syngas circulation followed by feeding gas from the first or second step into gasmain or power plant.

EFFECT: simplified method due to process optimization.

12 cl, 3 tbl, 3 dwg

FIELD: industrial organic synthesis.

SUBSTANCE: invention relates to improved process of producing methanol from purge gas produced in basic methanol or ammonia synthesis. Process comprises dispensing compressed carbon dioxide into basic synthesis purge gas, heating resultant gas mixture to starting synthesis temperature, passing thus heated gas through methanol synthesis catalyst, cooling reacted gas, recovering condensed crude methanol, and separating non-condensed gas stream into return stream and purge stream, the former being designed for mixing with basic synthesis purge gas stream and passed to one or two circulation jet compressors. Circulation is effected by energy provide either by (i) pressure of basic synthesis purge gas, which is supplied to jet compressor and further dispensed into compressed carbon dioxide stream, or by (ii) pressure of compressed carbon dioxide, which is dispensed into jet compressor and then introduced into basic synthesis purge gas stream, or by (iii) pressure of basic synthesis purge gas and pressure of indicated compressed carbon dioxide, both being supplied to one or two jet compressors. Ammonia or methanol production purge gas is successfully used for production of methanol without utilizing additional hydrogen-containing streams.

EFFECT: reduced methanol production cost.

4 cl, 5 dwg, 1 tbl, 4 ex

FIELD: organic chemistry, chemical technology.

SUBSTANCE: method for synthesis of methanol involves the following stages: removing hydrocarbon gas to be processed, sulfur elimination, catalytic steam conversion to obtain converted gas, heat utilization with separation of water, synthesis of methanol and separation of condensed methanol. Hydrocarbon gas with unstable composition is removed under pressure 0.001 MPa, not less, and sulfur elimination of hydrocarbon gas with unstable composition is combined with stage of step-by-step stabilization of pressure to form steam-gaseous mixture. Methanol synthesis is carried out for at least two successive flow steps with reducing volume of catalyst under pressure 1.5 MPA, not less, and separation of methanol between successive stages. Method provides significant reducing cost of gas processing and service of devices and allows carrying out the processing in mobile traveling devices in field conditions. Invention can be used in processing gas with unstable composition, for example, casing-head petroleum gas in petroleum-extracting holes, in field conditions in small traveling devices.

EFFECT: improved preparing method.

2 cl, 2 dwg

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to the improved method for preparing methanol. Method involves the successive feeding hydrocarbon-containing gas, injection of chemically purified water, carrying out the preliminary steam reforming for preparing synthesis gas and carrying out the final reforming if formed gas with addition of oxygen under pressure for carrying out synthesis of methanol, heating reactor for preliminary reforming by flow of obtained synthesis gas going out from reactor for the final reforming that is fed to intertubular space of reactor for preliminary reforming followed by cooling synthesis gas obtained as result of reforming by vapor-gas mixture and carrying out synthesis of methanol in 2-step reactor. Cooling the reaction mixture for carrying out isothermal reaction for synthesis of methanol in intermediate external heat exchanger of two-step reactor is carried out with vapor-gas mixture and cooling flow going out from reactor for synthesis of methanol is carried out with vapor-gas mixture and chemically purified water. Also, invention relates to unit for preparing methanol including the source of hydrocarbon-containing gas and unit for complex preparing gas, reactor for preliminary vapor reforming heated with flow going out from reactor for final reforming, two-step reactor for synthesis of methanol, heat exchangers for cooling synthesis gas, heat exchangers for cooling flow going out from reactor for synthesis of methanol, separator for separation of reaction products and exhausting gases and crude methanol. The unit for preparing methanol is assembled with unit for complex gas preparing including block for preparing chemically purified water, block for preparing raw, additional manufacture involving torch making, cleansing constructions, sources of electric energy, air of control and measuring instruments and automatic equipment, chemical laboratory and operating block. Two-step reactor for synthesis of methanol joined with heat exchanger for cooling synthesis gas with vapor-gas mixture, intermediate external heat exchanger for cooling the reaction mixture with vapor-gas mixture is joined in-line with heat exchanger for cooling flow obtained in reactor with vapor gas mixture, heat exchanger for cooling of chemically purified water and separator for separation of reaction products. Ignition device is assembled in reactor for final reforming that promotes to carry out the start of unit without trigger furnace. Water is injected in flow hydrocarbon gas directly before heat exchanger for the reaction mixture that provides excluding boiler-utilizer and trigger boiler from schedule and to solve the problem for cooling the reaction mixture in reactor for synthesis of methanol also. Based on integration of the device for preparing methanol in technological schedule with unit for complex preparing gas and significant change of the conventional schedule for preparing methanol method provides 3-fold reducing capital investment.

EFFECT: improved method for preparing methanol.

2 cl, 1 dwg

FIELD: technology for production of methanol from syngas.

SUBSTANCE: claimed method includes mixing of hydrocarbon raw material with water steam to provide syngas by steam conversion of hydrocarbon raw material and subsequent methanol synthesis therefrom. Conversion of hydrocarbon raw material and methanol synthesis are carried out under the same pressure from 4.0 to 12.0 MPa. In one embodiment hydrocarbon raw material is mixed with water steam and carbon dioxide to provide syngas by steam/carbonic acid conversion of hydrocarbon raw material in radial-helical reactor followed by methanol synthesis therefrom under the same pressure (from 4.0 to 12.0 MPa). In each embodiment methanol synthesis is carried out in isothermal catalytic radial-helical reactor using fine-grained catalyst with grain size of 1-5 mm. Methanol synthesis is preferably carried out in two steps with or without syngas circulation followed by feeding gas from the first or second step into gasmain or power plant.

EFFECT: simplified method due to process optimization.

12 cl, 3 tbl, 3 dwg

The invention relates to a method and installation for the production of methanol by the reaction of carbon monoxide and hydrogen using biomass as raw material

The invention relates to a method of producing methanol from natural gas and "tail" of hydrocarbon gases in the chemical and petrochemical industries

The invention relates to a method and installation for the combined production of ammonia and methanol, as well as to upgrade the installation of the ammonia synthesis to ensure such co-production

The invention relates to energy-saving methods for the synthesis of methanol from synthesis gas obtained by partial oxidation of natural gas with air enriched with oxygen, air or the flow of oxygen-containing gas with a high content of nitrogen in the energy machines with electricity generation at all stages of production of methanol

The invention relates to a combined synergistic method of production of methanol and the production of tertiary butyl esters of lower Akilov partial oxidation of heavy hydrocarbon fractions

The invention relates to the field of organic synthesis, in particular to the synthesis of methanol on copper-containing catalysts at elevated temperature and pressure of a mixture of carbon oxides and hydrogen, mainly from a mixture of carbon dioxide and hydrogen

FIELD: petrochemical industry; methods of the synthesis of ammonia from the nitrogen and hydrogen mixture produced from the natural gases.

SUBSTANCE: the invention is pertaining to the field of petrochemical industry, in particular, to the method of the synthesis of ammonia from the nitrogen and hydrogen mixture produced from the natural gases. The method of the catalytic synthesis of ammonia from the mixture of nitrogen and hydrogen provides, that the natural gas together with the oxygen-enriched gas containing at least 70 % of oxygen is subjected to the autothermal reforming at temperature from 900 up to 1200°C and the pressure from 40 up to 100 bar at the presence of the catalyzer of cracking, producing the unstripped synthesis gas containing in terms of the dry state 55-75 vol.% of H2, 15-30 vol.% of C and 5-30 vol.% CO2. At that the volumetric ratio of H2: CO makes from 1.6 : 1 up to 4 : 1. The unstripped synthesis gas is removed from the furnace of the autothermal reforming, cooled and subjected to the catalytic conversion producing the converted synthesis gas containing in terms of the dry state at least 55 vol.% of H2 and no more than 8 vol.% of CO. The converted synthesis gas is subjected to the multistage treatment for extraction ofCO2, CO and CH4. At that they realize the contact of the synthesis gas with the liquid nitrogen and using at least one stage of the absorption treatment produce the mixture of nitrogen and hydrogen, which is routed to the catalytic synthesizing of ammonia. At that at least a part of the synthesized ammonia may be transformed into carbamide by interaction with carbon dioxide. The realization of the method allows to solve the problem of the ammonia synthesis efficiency.

EFFECT: the invention ensures solution of the problem of the ammonia synthesis efficiency.

8 cl, 1 ex, 2 tbl, 2 dwg

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