Synthesis gas producing method and device

FIELD: gas.

SUBSTANCE: synthesis gas producing method includes partial oxidation of the first portion of hydrocarbon in partial oxidation reactor, wherein the first flow leaving the reactor is obtained, cooled up to the temperature of 650° to 1000°C, and supplied to the reforming heat-exchanger. Then the second portion of hydrocarbon with steam passes through catalyst space in the reforming heat-exchanger, and the second flow leaving the reactor is generated, discharged from catalyst space, and mixed with the first flow leaving the reactor. Mixture passes through catalyst space in indirect heat exchange therewith, and mixture is cooled and catalyst space is heated, and after that the cooled mixture is taken from the reforming heat-exchanger. Modernising procedure of synthesis gas producing method includes partial oxidation reaction stage, whereat the first hydrocarbon flow is turned into the first flow leaving the reactor, heat recovery stage, whereat the first flow leaving the reactor is cooled, and steam is generated with the help of recovered heat, and outlet flow treatment stage, at which cooled flow leaving the reactor is received, and synthesis gas is produced with increased hydrogen content. It also includes the cooling stage of the first flow leaving the reactor up to the temperature of 650° to 1000°C, the stage at which the first cooled flow leaving the reactor is discharged into the reforming heat-exchanger, stage at which the second portion of hydrocarbon with steam passes through catalyst space in the reforming heat-exchanger, and the second flow leaving the reactor is generated, stage at which the second flow leaving the reactor is discharged from catalyst space and mixes with the first flow leaving the reactor, stage at which mixture passes through catalyst space in indirect heat exchange therewith, and mixture is cooled and catalyst space is heated, and stage at which cooled mixture is supplied from the reforming heat-exchanger to heat recovering stage.

EFFECT: allow to increase in capacity as to hydrogen.

21 cl, 2 dwg, 1 tbl

 

The level of technology

This invention relates to the production of synthesis gas (syngas) using a partial oxidation reactor (CHO) and heat exchanger reformer.

The reforming of hydrocarbons is a standard method for the production containing hydrogen synthesis gas used, for example, to produce ammonia or methanol. Traditional reactors CHO are not having nozzles non-pressure non-catalytic gas generators, which serves heated gaseous hydrocarbon and oxygen, optionally with a temperature controller. The flow resulting from the partial oxidation reactor, then abruptly or gradually cooled, usually 200-300°not necessarily cleaned to remove soot, and, as a rule, then subjected to transformation in CO-converters with high and low temperature, in which pairs and interact with the formation of additional hydrogen and CO2. Synthesis gas with high hydrogen content are especially necessary for ammonia synthesis or by other processes where hydrogen is the main reagent from synthesis gas. The weight ratio of steam to hydrocarbon in the feed to the reactor CHO is generally from 0.1 to 5 atomic ratio of oxygen to carbon in the hydrocarbon is in the range from 0.6 to 1.6, and the reaction times vary from 1 to 10 seconds.

The reaction is ora CHO described, for example, in U.S. patents 2,896,927; 3,920,717; 3,929,429 and 4,081,253, which are incorporated here by reference in full.

Reactors CHO produce a flowing stream of synthesis gas at a very high temperature before the sudden cooling, for example, from 1100° up to 1650°C. This means that a large part of the supplied hydrocarbon must actually be used as a fairly expensive fuel in order to heat the raw materials and to produce pairs of high or medium pressure. However, the production of steam is usually much more than is required for installation, and therefore it must be allocated and for sale pair often have little opportunity or it does not.

In the art a need for a way to improve the effectiveness of systems for the production of hydrogen, using reactors CHO, and reduction or elimination of steam extraction. Also, it is often desirable to maximize or increase the production of hydrogen at existing facilities for the production of hydrogen; however, the reactor CHO is often the mode of operation, limiting performance. Reactors CHO cannot be easily increased in volume to improve performance.

The present invention is directed to meeting these needs by feeding the partially cooled stream flowing from the reactor CHO, side shell is of Teploobmennik reformer, to provide heat to produce additional synthesis gas. The reforming exchangers used with the reforming-installations with autopedigree known, for example, from U.S. patent 5,011,625 and 5,122,299 in the name of LeBlanc and 5,362,454 name Cizmer and others, which are all incorporated here by reference in full. These reforming exchangers are commercially available under the trademark KRES or Kellogg Reforming Exchanger System.

The invention

The present invention uses a heat exchanger reformer in parallel with the reactor, a partial oxidation (CHO) in a new installation for hydrogen production with improved efficiency and reduced exhaust steam, or in an existing installation for the production of hydrogen. In one embodiment the performance of hydrogen can be increased by 20-30 percent while reducing steam extraction from plants for the production of hydrogen. The process has a very low energy consumption.

The present invention provides a method for synthesis gas production. The method includes: (a) partial oxidation of the first part of the hydrocarbon with oxygen in the partial oxidation reactor, obtaining a first stream flowing from the reactor; (b) cooling the first stream flowing from the reactor to a temperature of from 650° 1000°With; (C) feeding the first stream flowing from the reactor, at Teploobmennik is to the reformer; (d) passing the second portion of the hydrocarbon with steam through the zone of the catalyst in the heat exchanger reformer, with the formation of the second stream flowing from the reactor; (e) the release of the second stream flowing from the reactor, the catalyst with the formation of the mixture with the first stream flowing from the reactor; (f) passing the mixture through a zone of catalyst in indirect heat exchange with cooling the mixture, and the heating zone of the catalyst; and (g) collecting the cooled mixture from the heat exchanger reformer.

The cooling may include the introduction of water in the first stream flowing from the reactor, as a fluid medium for rapid cooling, indirect heat exchange, or a combination of sharp cooling water and indirect heat exchange. Indirect heat exchange may be used for heating the second portion of the hydrocarbon in the cross heat exchanger. Area of the catalyst may include catalytic tube. The method may also include applying the second part of the hydrocarbon from the tubes of the heat exchanger reformer and its transmission through the catalytic tube, and feeding the cooled first stream flowing from the reactor on the input side of the shell of the heat exchanger reformer. Entrance from the side shell may be adjacent to the outlet end of the catalyst tubes. The method may further include applying the first and second parts of the carbohydrate is kind of in a weight ratio of from 40:60 to 95:5. More preferably, the first and second parts of the hydrocarbon could be served in a weight ratio of from 40:60 to 60:40 (for more efficient hydrogen production), or from 80:20 to 95:5 (if you want more).

The present invention also provides a device for the production of synthesis gas. The device includes: (a) means in the form of a partial oxidation reactor for partial oxidation of the first part of the hydrocarbon with oxygen, with the formation of the first stream flowing from the reactor; (b) a means for cooling the first stream flowing from the reactor to a temperature of from 650° 1000°With; (C) means for feeding the first stream flowing from the reactor, the heat exchanger reformer; (d) means for passing a second portion of the hydrocarbon with steam through the zone of the catalyst in the heat exchanger reformer, with the formation of the second flow arising from reactor; (e) means to produce a second stream flowing from the reactor, the catalyst with the formation of the mixture with the first stream flowing from the reactor; (f) means for passing the mixture through a zone of catalyst in indirect heat exchange with cooling the mixture, and the heating zone of the catalyst; and (g) means for collecting the cooled mixture from the heat exchanger reformer.

The present method further provides a method of upgrading method of obtaining Sint the C-gas, includes step of the reaction of partial oxidation, which makes the first hydrocarbon stream into a first stream flowing from the reactor stage heat recovery, which is cooled first stream flowing from the reactor, and producing steam using recovered heat, and the stage of processing of the output stream, which take the cooled stream flowing from the reactor, and produce synthesis gas with high hydrogen content. Modernization includes: (a) the stage at which the partially cooled first stream flowing from the reactor to a temperature of from 650° 1000°With; (b) the stage at which divert partially cooled first stream flowing from the reactor, the heat exchanger reformer; (C) the stage at which miss the second part of the hydrocarbon with steam through the zone of the catalyst in the heat exchanger reformer, with the formation of the second stream flowing from the reactor; (d) the stage at which release a second stream flowing from the reactor, from the zone of the catalyst with the formation of the mixture with the first stream flowing from the reactor; (e) the stage at which pass the mixture through a zone of catalyst in indirect heat exchange with cooling the mixture, and the heating zone of the catalyst; and (f) stage, which serves a mixture of a heat exchanger reformer stage heat recovery.

Brief description of drawings

1 before the hat is a simplified process diagram for the traditional process CHO, known from the prior art, which can be upgraded in accordance with one of the embodiments of the present invention.

Figure 2 is a simplified process diagram for production of synthesis gas from the reactor CHO and heat exchanger reformer integrated in accordance with one of the embodiments of the invention.

Detailed description of the invention

The proposed upgraded installation of the present invention have the General configuration shown in figure 1. Desulfuromonas natural gas or another hydrocarbon, supplied from line 2, mixed with process steam from the pipe 4, and the mixture is heated in the heat exchanger of the heating of the substrate (not shown). The heated mixture of steam-hydrocarbon is fed through line 6 to the reactor CHO 8 (or multiple reactors CHO) with oxygen 10, and the resulting stream is collected in the pipe 12, abruptly cooled by water injected through the pipe 14, and then fed to the processing of 15 of the output stream, which may include conversion section (CO-converters with high temperature, medium temperature and/or low temperature), heat recovery, removal of CO2(for example, the absorbance at a pressure difference or PSA), and the like. Is rich in hydrogen flow synthesis gas 17.

The installation of figure 1 upgraded, or new installation from what is given in accordance with one of the embodiments of the present invention, as shown in figure 2. The reactor(s) CHO 8 and the pipes 2, 4, 6, 10 are conventional, as described with reference to figure 1. The resulting process flow in the pipe 12 from the reactor(s) CHO 8 sharply cooled water through the pipe 14 to 700°-1100°With, preferably 750°-1000°and the mixture is fed through line 16 to the input side of the shell of the heat exchanger reformer 18. The heat exchanger 15 can be used in addition or instead of the pipeline sharp cooling 14. The heat exchanger 15 can be used to preheat the flow of raw material 19.

Heated the mixture in the pipe 19 from the steam and hydrocarbon, which may be the same or different from the hydrocarbon in the pipe 2, is fed to the inlet side of the tubes of the heat exchanger reformer 18. The mixture passes through the catalyst tube 20, with the formation of additional gas containing hydrogen. The gas reformer of the output apertures of the catalytic tubes 20 is mixed with the flowing stream from the reformer installation CHO, and the mixture passes through the outer side of the catalytic tubes 20 on the output side of the shell, where it is collected in the pipe 22 in the traditional way. The combined synthesis gas in line 22 is then fed to the traditional processing of the output stream 24, as in figure 2, which may include CO-Converter, heat exchanger Assembly for regenerat and heat, and additional cleaning of producing purified molecular hydrogen. In the modernized application processing units of the output stream can be modified or augmented in volume, as needed, to handle the additional synthesis gas supplied through the pipe 22, which is obtained by adding a heat exchanger reformer 18.

The need for heat for heat exchanger reformer 18 is satisfied by the quantity and temperature of the stream flowing from the reactor CHO. Usually, the larger the supply of raw materials in the pipe 19 into the heat exchanger reformer 18, the more heat is required from the stream 16 flowing from the reactor CHO to support, generally, the endothermic reforming reaction in the catalytic tubes 20. It is desirable that the temperature of the gas resulting from the catalytic reforming tubes-installation was so high, as will the materials of construction of the heat exchanger reformer 18, for example, from 750° 1000°With standard unit KRES. If the temperature is too low, the heat exchanger reformer 18 may be insufficient reforming process, whereas if the temperature is too high, metallurgical calculations can be problematic. It is also necessary to take measures to ensure that the temperature is chosen so that the minimi is activated dust metal.

The ratio of hydrocarbon feed to the reactor(s) CHO 8 may be in the range from 40 to 95 percent of the total, whereas the ratio of feed to the heat exchanger reformer 18 may be from 5 to 60 percent of the total hydrocarbon feed. It is desirable that the ratio of feed between the reactor(s) CHO 8 and heat exchanger reformer 18 was such that the reactor(s) CHO 8 could(if) to produce the appropriate amount of hot flowing stream to provide heat requirements of the heat exchanger reformer 18. The ratio of feed to the reactor(s) CHO 8 from 40 to 60 percent of the total number is beneficial for improved energy return and maximize the performance of hydrogen, while supply from 80 to 95 percent of the total hydrocarbon feed to the reactor(s) CHO 8 is advantageous to obtain a larger amount of CO in the synthesis gas.

The present invention is illustrated by way of example. Preliminary project settings process for the integrated Assembly of the heat exchanger CHO-reformer shown in figure 2, were developed on the basis of modernization of typical CHO process of figure 1 with part of the flow and the flow through the pipeline 16, indicated in the table below. The compositions, properties, and costs for selected streams in the process, modified in accordance with the configuration according to Fig., also shown in the table.

The configuration of the reactor CHO - exchanger reformer
Stream ID:Stemming the flow CHO pipeline 16Catalytic tubes 20 InputCatalytic tubes 20 OutputThe output from shell Pipeline 22
ComponentThe composition of the flow, the final molar percent
H262,351,8073,7964,21
N20,661,800,470,63
CH40,6694,403.04 from1,05
Ar0,110,000,000,09
COof 33.260,1016,5230,54
CO22,960,206,173,49
C2H60,001,200,000,00
With3H80,000,300,000,00
i-C40,000,100,000,00
i-C50,0 0,100,000,00
The total flow KMOL/h636,232,1123,5759,7
H2O, KMOL/h153,285,850,3203,5
The total flow KMOL/h789,4117,9173,8963,1
The total flow, kg/h10,5282,0732,07312,601
Pressure (bar(absolute))32,435,532,432,1
Temperature (°C)999,7308,8938,1702,3

In the main event, only with the reactor CHO, synthesis gas produced in the reforming process of the installation, you will have the composition and the flow rate flowing out of the reactor CHO, in the pipeline 16. Using the heat exchanger reformer in parallel with the reactor CHO in accordance with this embodiment of the invention, the resulting flow in the pipe 16 is mixed with the gas discharged from the catalytic tubes 20, to obtain a synthesis gas having a composition in the pipe 22. This example shows that the integrated process of CHO-exchanger reformer can be used for regeneration of waste heat in the heat exchanger reformer and increasing productivity is eljnosti hydrogen from 20 to 25 percent. Using a heat process for additional production of hydrogen, thereby achieving a corresponding reduction in steam extraction.

The invention is described above with reference to non-limiting examples provided for illustrative purposes only. Various modifications and changes will become obvious to a person skilled in this technical field from this point of view. It is assumed that all such changes and modifications within the scope and essence of the attached claims will be included in the scope of the invention.

1. Method for production of synthesis gas, including

partial oxidation of the first part of the hydrocarbon with oxygen in the partial oxidation reactor, obtaining a first stream flowing from the reactor;

cooling the first stream flowing from the reactor to a temperature of from 650 to 1000°C;

feeding the first stream flowing from the reactor, the heat exchanger reformer;

the transmission of the second part of the hydrocarbon with steam through the zone of the catalyst in the heat exchanger reformer, with the formation of the second stream flowing from the reactor;

the release of the second stream flowing from the reactor, the catalyst with the formation of the mixture with the first stream flowing from the reactor;

passing the mixture through a zone of catalyst in indirect heat exchange with ohlord the of the mixture, and the heating zone of the catalyst;

collecting the cooled mixture from the heat exchanger reformer.

2. The method according to claim 1, in which the water is introduced into a first stream flowing from the reactor, as the fluid for rapid cooling.

3. The method according to claim 2, which further includes cooling by indirect heat exchange.

4. The method according to claim 3, in which indirect heat exchange involves the heating of the second part of the hydrocarbon in the cross heat exchange.

5. The method according to claim 1, wherein the cooling includes heat transfer.

6. The method according to claim 5, in which indirect heat exchange involves the heating of the second part of the hydrocarbon in the cross heat exchanger.

7. The method according to claim 1, in which the area of the catalyst includes a catalytic tube.

8. The method according to claim 5, in which the second part of the hydrocarbon served with side tubes of the heat exchanger reformer and passed through the catalyst tubes.

9. The method according to claim 5, in which the cooled first stream flowing from the reactor is fed to the input side of the shell of the heat exchanger reformer.

10. The method according to claim 7, in which the entrance-side membrane is adjacent to the outlet end of the catalyst tubes.

11. The method according to claim 1, wherein the first and second parts of hydrocarbon served in a weight ratio of from 40:60 to 95:5.

12. The method according to claim 1, wherein the first and second parts of hydrocarbon served in a weight ratio of from 40:60 to 60:40.

13. The method according to claim 1, in which p is pout and a second portion of the hydrocarbon served in a weight ratio of from 95:5 to 80:20.

14. Device for the production of synthesis gas, containing

means in the form of a partial oxidation reactor for partial oxidation of the first part of the hydrocarbon with oxygen with the formation of the first stream flowing from the reactor;

means for cooling the first stream flowing from the reactor to a temperature of from 650 to 1000°C;

means for feeding the first stream flowing from the reactor, the heat exchanger reformer;

means for passing a second portion of the hydrocarbon with steam through the zone of the catalyst in the heat exchanger reformer, with the formation of the second stream flowing from the reactor;

means to produce a second stream flowing from the reactor from the catalyst, forming a mixture with the first stream flowing from the reactor;

means for passing the mixture through a zone of catalyst in indirect heat exchange with cooling the mixture, and the heating zone of the catalyst;

means for collecting the cooled mixture from the heat exchanger reformer.

15. Upgrade method of producing synthesis gas comprising step of the reaction of partial oxidation, which makes the first hydrocarbon stream into a first stream flowing from the reactor stage heat recovery, which is cooled first stream flowing from the reactor, and produce vapor when help is regenerated heat and the stage of processing of the output stream, which take the cooled stream flowing from the reactor, and produce synthesis gas with a high hydrogen content, including

the stage at which it is cooled first stream flowing from the reactor to a temperature of from 650 to 1000°C;

the stage at which divert the cooled first stream flowing from the reactor, the heat exchanger reformer;

the stage at which miss the second part of the hydrocarbon with steam through the zone of the catalyst in the heat exchanger reformer, with the formation of the second stream flowing from the reactor;

the stage at which release a second stream flowing from the reactor, the catalyst with the formation of the mixture with the first stream flowing from the reactor;

the stage at which the mixture is passed through a zone of catalyst in indirect heat exchange with cooling the mixture, and the heating zone of the catalyst;

stage, which is served chilled mixture from the heat exchanger reformer stage heat recovery.

16. The method according to item 15, in which water is injected into a first stream flowing from the reactor, as the fluid for rapid cooling.

17. The method according to claim 11, in which the first stream flowing from the reactor, cooled by indirect heat exchange.

18. The method according to 17, in which the second part of the hydrocarbon is heated is by indirect heat exchange before as served at the heat exchanger reformer.

19. The method according to 17, in which water is injected into a first stream flowing from the reactor.

20. The method according to claim 11, in which the area of the catalyst additionally contains a catalytic tube.

21. The method according to p, in which the second part of the hydrocarbon fed to the inlet side of the tubes of the heat exchanger reformer.



 

Same patents:

FIELD: chemistry.

SUBSTANCE: hydroreactive mixture contains industrial aluminium ACD-1 powder and aluminium nanopowder with particle size of 70÷120 nm, as well as an activating additive in form of granular sodium hydroxide with the following ratio of components, in wt %: industrial ACD-1 powder 67÷79, aluminium nanopowder 30÷14, sodium hydroxide 3÷7.

EFFECT: faster heat release.

1 tbl

FIELD: chemistry.

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13 cl, 14 dwg, 7 tbl, 4 ex

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5 cl, 6 ex

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17 cl, 2 tbl, 24 ex

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FIELD: chemistry.

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EFFECT: invention makes it possible to improve industrial and economic characteristics.

18 cl, 5 dwg, 3 tbl

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EFFECT: invention makes it possible to improve industrial and economic characteristics.

18 cl, 5 dwg, 3 tbl

FIELD: chemistry.

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129 cl, 13 tbl, 13 ex

FIELD: chemistry.

SUBSTANCE: invention relates to dehydrogenation or reforming of alcohols, in particular to a method of dehydrogenation of the primary alcohol, such as methanol or ethanol, for obtaining hydrogen, in particular for use in a fuel element with the purpose of obtaining electrical energy. In the method of dehydrogenation a catalyst containing copper is used, which includes a metallic carrier. To solve the given challenge the method includes bringing to contact of the initial raw mixture of the gases containing alcohol, with the catalyst of reforming in order to obtain a mixture of products of reforming, containing hydrogen, and the catalyst for reforming the contains a metallic spongy carrier and a coating on copper, at least, partially covering surface of the given metal spongy carrier where the given metal spongy carrier is obtained by means of the method including the leaching of aluminium from an alloy, containing aluminium and the main metal.

EFFECT: increased activity in the gas-phase reforming of primary spirits and increased stability.

129 cl, 13 tbl, 13 ex

FIELD: chemistry.

SUBSTANCE: invention pertains to the method of obtaining porous substances on a substrate for catalytic applications, to the method of obtaining porous catalysts for decomposition of N2O and their use in decomposing N2O, oxidising ammonia and reforming methane with water vapour. Description is given of the method of obtaining porous substances on a substrate for catalytic applications, in which one or more soluble precursor(s) metal of the active phase is added to a suspension, consisting of an insoluble phase of a substrate in water or an organic solvent. The suspension undergoes wet grinding so as to reduce the size of the particles of the substrate phase to less than 50 mcm. The additive is added, which promotes treatment before or after grinding. A pore-forming substance is added and the suspension, viscosity of which is maintained at 100-5000 cP, undergoes spray drying, is pressed and undergoes thermal treatment so as to remove the pore-forming substance, and is then baked. Description is also given of the method of obtaining porous catalysts on a substrate for decomposing N2O, in which a soluble cobalt precursor is added to a suspension of cerium oxide and an additive, promoting treatment, in water. The suspension is ground to particle size of less than 10 mcm. A pore-forming substance, viscosity of which is regulated to approximately 1000 cP, is added before the suspension undergoes spray drying with subsequent pressing. The pore-forming substance is removed and the product is baked. Description is given of the use of the substances obtained above as catalysts for decomposition of N2O, oxidation of ammonia and reforming of methane with water vapour.

EFFECT: obtaining catalysts with homogenous distribution of active phases and uniform and regulated porosity for optimisation of characteristics in catalytic applications.

FIELD: hydrocarbon conversion catalysts.

SUBSTANCE: catalyst for generation of synthesis gas via catalytic conversion of hydrocarbons is a complex composite composed of ceramic matrix and, dispersed throughout the matrix, coarse particles of a material and their aggregates in amounts from 0.5 to 70% by weight. Catalyst comprises system of parallel and/or crossing channels. Dispersed material is selected from rare-earth and transition metal oxides, and mixtures thereof, metals and alloys thereof, period 4 metal carbides, and mixtures thereof, which differ from the matrix in what concerns both composition and structure. Preparation procedure comprises providing homogenous mass containing caking-able ceramic matrix material and material to be dispersed, appropriately shaping the mass, and heat treatment. Material to be dispersed are powders containing metallic aluminum. Homogenous mass is used for impregnation of fibrous and/or woven materials forming on caking system of parallel and/or perpendicularly crossing channels. Before heat treatment, shaped mass is preliminarily treated under hydrothermal conditions.

EFFECT: increased resistance of catalyst to thermal impacts with sufficiently high specific surface and activity retained.

4 cl, 1 tbl, 8 ex

FIELD: power engineering.

SUBSTANCE: method includes searching for continental or oceanic rift generation zones, supported by abnormal mantle with output of substance branches to earth crust. Drilling of wells by turbodrills into mantle substance. After well enters mantle substance a reaction hollow is formed in it by putting together force and product wells or by expanding force and/or product wells. Water is pumped into force well and gas-like hydrogen is outputted to surface through product well forming during reaction of inter-metallic substances fro mantle substance to water. Water is fed in amount, adjusting output of hydrogen, while reaction surface of reaction hollow is periodically regenerated, for example, by high pressure water flow, supplied through jets in reaction hollow, on remotely controlled manipulators. Expansion of well may be performed via explosions of explosive substances charges, and it is possible to separate forming gaseous hydrogen and water steam by separator mounted therein.

EFFECT: higher effectiveness of hydrogen production.

9 cl

FIELD: alternative fuel production and catalysts.

SUBSTANCE: invention relates to (i) generation of synthesis gas useful in large-scale chemical processes via catalytic conversion of hydrocarbons in presence of oxygen-containing components and to (ii) catalysts used in this process. Catalyst represents composite including mixed oxide, simple oxide, transition element and/or precious element, carrier composed of alumina-based ceramic matrix, and a material consisting of coarse particles or aggregates of particles dispersed throughout the matrix. Catalyst has system of parallel and/or crossing channels. Catalyst preparation method and synthesis gas generation method utilizing indicated catalyst are as well described.

EFFECT: enabled preparation of cellular-structure catalyst with high specific surface area, which is effective at small contact times in reaction of selective catalytic oxidation of hydrocarbons.

6 cl, 2 tbl, 16 ex

FIELD: autothermal catalytic reforming of hydrocarbon feed stream.

SUBSTANCE: method relates to method for reforming of hydrocarbon feed stream with water steam at elevated temperature to produce gas enriched with hydrogen and/or carbon oxide. Hydrocarbon stream is passed through water steam reforming catalyst bed wherein oxygen is fed through oxygen-permeable membrane followed by removing of finished product from this bed. Said catalyst bed contains in input region catalyst with reduced or without water steam reforming activity, but having hydrocarbon feed oxidation activity.

EFFECT: process with improved characteristics due to temperature controlling in reactor.

3 cl, 1 dwg

FIELD: alternate fuel manufacture catalysts.

SUBSTANCE: invention relates to generation of synthesis gas employed in large-scale chemical processes such as synthesis of ammonia, methanol, higher alcohols and aldehydes, in Fischer-Tropsch process, and the like, as reducing gas in ferrous and nonferrous metallurgy, metalworking, and on gas emission detoxification plants. Synthesis gas is obtained via catalytic conversion of mixture containing hydrocarbon or hydrocarbon mixture and oxygen-containing component. Catalyst is a complex composite containing mixed oxide, simple oxide, transition and/or precious element. Catalyst comprises metal-based carrier representing either layered ceramics-metal material containing nonporous or low-porosity oxide coating, ratio of thickness of metallic base to that of above-mentioned oxide coating ranging from 10:1 to 1:5, or ceramics-metal material containing nonporous or low-porosity oxide coating and high-porosity oxide layer, ratio of thickness of metallic base to that of nonporous or low-porosity oxide coating ranging from 10:1 to 1:5 and ratio of metallic base thickness to that of high-porosity oxide layer from 1:10 to 1:5. Catalyst is prepared by applying active components onto carrier followed by drying and calcination.

EFFECT: increased heat resistance and efficiency of catalyst at short contact thereof with reaction mixture.

13 cl, 2 tbl, 17 ex

FIELD: electric power and chemical industries; methods of production of the electric power and liquid synthetic fuel.

SUBSTANCE: the invention presents a combined method of production of the electric power and liquid synthetic fuel with use of the gas turbine and steam-gaseous installations and is dealt with the field of electric power and chemical industries. The method provides for the partial oxidation of hydrocarbon fuel in a stream of the compressed air taken from the high-pressure compressor of the gas turbine installation with its consequent additional compression, production of a synthesis gas, its cooling and ecological purification, feeding of the produced synthesis gas in a single-pass reactor of a synthesis of a liquid synthetic fuel with the partial transformation of the synthesis gas into a liquid fuel. The power gas left in the reactor of synthesis of liquid synthetic fuel is removed into the combustion chamber of the gas-turbine installation. At that the degree of conversion of the synthesis gas is chosen from the condition of maintenance of the working medium temperature at the inlet of the gas turbine depending on the type of the gas-turbine installation used for production of the electric power, and the consequent additional compression of the air taken from the high-pressure compressor of the gas-turbine installation is realized with the help of the gas-expansion machine powered by a power gas heated at the expense of the synthesis gas cooling before the reactor of synthesis. The invention allows simultaneously produce electric power and synthetic liquid fuels.

EFFECT: the invention ensures simultaneous production of electric power and synthetic liquid fuels.

2 cl, 2 dwg

FIELD: petrochemical industry.

SUBSTANCE: the invention is dealt with petrochemical industry, in particular with a method of catalytic preliminary reforming of the hydrocarbon raw materials containing higher hydrocarbons. The method provides for the indicated hydrocarbon raw materials gating through a zone of a catalyst representing a fixed layer containing a noble metal on magnesia oxide (MgO) and-or spinel oxide (MgAl2O4) at presence of oxygen and water steam. The technical result is a decrease of a carbon share on the catalyst.

EFFECT: the invention allows to decrease a carbon share on the catalyst.

3 cl, 2 tbl, 2 ex

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: methods of production a synthesis gas.

SUBSTANCE: the invention is pertaining to the process of production of hydrogen and carbon oxide, which mixture is used to be called a synthesis gas, by a selective catalytic oxidation of the hydrocarbonaceous (organic) raw material in presence of the oxygen-containing gases. The method of production of the synthesis gas includes a contacting with a catalyst at a gas hourly volumetric speed equal to 10000-10000000 h-1, a mixture containing organic raw material and oxygen or an oxygen-containing gas in amounts ensuring the ratio of oxygen and carbon of no less than 0.3. At that the process is conducted at a linear speed of the gas mixture of no less than 2.2 · 10-11 · (T1 + 273)4 / (500-T2) nanometer / s, where: T1 - a maximum temperature of the catalyst, T2 - a temperature of the gas mixture fed to the contacting. The linear speed of the gas mixture is, preferably, in the interval of 0.2-7 m\s. The temperature of the gas mixture fed to the contacting is within the interval of 100-450°C. The maximum temperature of the catalyst is within the interval of 650-1500°C. The technical effect is a safe realization of the process.

EFFECT: the invention ensures a safe realization of the process.

10 cl, 5 ex

FIELD: chemical industry; petrochemical industry; oil refining industry and other industries; methods of production a synthesis gas.

SUBSTANCE: the invention is pertaining to the field of the methods of production of a synthesis of gas and may be used in chemical, petrochemical, oil refining and other industries. The method of production of synthesis gas using a vapor or a vapor-carbon dioxide conversion of a hydrocarbonaceous raw material provides for purification of the hydrocarbonaceous raw material from sulfuric compounds, its commixing with steam or with steam and carbon dioxide with formation of a steam-gas mixture. The catalytic conversion of the steam-gas mixture is conducted in a reactor of a radially-spiral type, in which in the ring-shaped space filled with a nickel catalyst with a size of granules of 0.2-7 mm there are the hollow spiral-shaped walls forming the spiral-shaped channels having a constant cross section for conveyance of a stream of the steam-gaseous blend in an axial or in a radially-spiral direction. At that into the cavities of the walls feed a heat-transfer agent to supply a heat into the zone of reaction. The invention ensures intensification the process.

EFFECT: invention ensures intensification the process.

4 cl, 4 dwg, 2 tbl, 3 ex

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