Section of plant and method of separation and cleaning of synthesis-gas

FIELD: separation and cleaning of synthesis-gas.

SUBSTANCE: proposed section consists of device for partial condensation of synthesis-gas including the following components: heat exchanger A for cooling the synthesis-gas fed to section, separator B connected with heat exchanger A and intended for separation of synthesis-gas into gas fraction consisting mainly of hydrogen and carbon monoxide and liquid fraction consisting mainly of carbon monoxide and methane, evaporator C for further separation of gas fraction fed from separator B into gas fraction consisting mainly of hydrogen and liquid fraction consisting mainly of carbon monoxide, evaporator D where hydrogen absorbed in liquid and remaining liquid containing mainly carbon monoxide are evaporated; this liquid may be directed to distilling tower; section is also provided with one more evaporator E where hydrogen absorbed in liquid fraction of separator B is removed through evaporation; this liquid contains mainly carbon monoxide and methane; liquid may be directed to distilling tower F for separation of gaseous carbon monoxide and obtaining methane from lower part of column. Section is also provided with unit for washing with nitrogen which includes washing column G for separation of admixtures by action of nitrogen from gas fraction of evaporator C and recovery of admixtures as fuel gas. Nitrogen washing unit adjoins the partial condensation device.

EFFECT: enhanced heat exchange; low cost of process.

13 cl, 1 dwg, 1 tbl

 

The present invention relates to the section installation and method for the separation and purification of synthesis gas, which allows for a two stage process in one section of the installation. In particular, the method allows a single section installation partial condensation synthesis gas and scrubbed synthesis gas with liquid nitrogen and get a few of the cleaned gases or gas mixtures that are directly suitable for further chemical syntheses.

It is known that for the separation and purification of the synthesis gas used production plant, in which, as a rule, can be allocated to only one component of the synthesis gas obtained by partial oxidation of natural gas. In these known methods, the carbon monoxide will be allocated using methods of refrigeration equipment in the unit sections, which is known as a device for the partial condensation of the gas ("Gas Production", Ullmann''s Encyclopedia of Industrial Chemistry, vol. A12, VCH Verlagsgesellschaft mbH (1989)). Methods of refrigeration equipment are also needed for the production of ammonia synthesis gas, and the used section of the installation, which is known as "a device for flushing with nitrogen (see above link). Both sections of the units are completely different. Common to both methods related to the field of refrigeration technology, is the only application mnogo the stock plate heat exchanger for cooling, and for re-heating gas flows.

Further known method of purification of the converted gas, in which washing is performed with liquid nitrogen (SU 179413, 08.04.1966 year).

Each of these methods requires a device for cooling, in section partial condensation in General can be achieved by increasing carbon monoxide or hydrogen, while section nitrogen leaching requires liquid nitrogen.

The objective of the proposed invention is to eliminate the above described disadvantages.

The problem is solved proposed section installation for the separation and purification of synthesis gas, the difference of which is that it consists of a device for the partial condensation synthesis gas, including:

- heat exchanger for cooling is supplied to the section installation synthesis gas;

- connected with the heat exchanger And a separator for separating a synthesis gas 2 gas fraction 4, consisting mainly of hydrogen and carbon monoxide, and the liquid fraction 5, consisting mainly of carbon monoxide and methane;

- evaporating device With further dividing supplied from the separator To the gas fraction 4 on the gas fraction 6, consisting mainly of hydrogen, and the liquid fraction 7, consisting mainly of carbon monoxide;

- evaporating device D, which evaporates absorb the Bank incorporated in the liquid 7 is hydrogen and the remaining containing mainly carbon monoxide liquid 8 may be directed to a distillation column F;

another evaporating device E, which is still absorbed in the liquid fraction 5 of the separator In the hydrogen is removed by evaporation and containing mainly carbon monoxide and methane liquid 9 may be directed to a distillation column F;

- distillation column F for the separation of gaseous carbon monoxide and produce methane gas from the exhaust from the lower part of the column of liquid;

and device for flushing with nitrogen, including:

- wash column G for separating liquid nitrogen impurities from containing mainly hydrogen gas fraction 6 evaporator With and utilization of impurities in the fuel gas 12,

moreover, the device for nitrogen leaching is adjacent to the device for partial condensation.

The preferred embodiment is that the heat exchanger And can take a lot of the allocated gas and liquid flows and to cool or to heat them to a predetermined temperature, and evaporators C, D and E are the evaporators flash evaporation, which can be removed dissolved in the liquid gas.

It is also desirable to distillation column F had the heat exchanger, through which is passed a synthesis gas of any composition, or made at the bottom of this column removal for accumulating the liquid, which after por the transmission through the heat exchanger And can be returned to the distillation column F.

It is preferable to wash the column G had lead pipes for gaseous or liquid nitrogen.

The task is also solved by the proposed method of separation and purification of the synthesis gas in the above-described section of the installation according to the invention, the difference of which is that, first conduct a partial condensation synthesis gas and then washing with liquid nitrogen.

The preferred implementation of the method according to the invention is that the separator To carry out the separation of the synthesis gas 2 gas fraction 4, consisting mainly of hydrogen and carbon monoxide, and the liquid fraction 5, consisting mainly of carbon monoxide and methane at a pressure of approximately 78 bar and a temperature of minus 171±10°and evaporating apparatus To carry out the separation gas fraction 4 consisting mainly of hydrogen gas fraction 6 and consisting mainly of carbon monoxide liquid 7 at a pressure of approximately 78 bar and a temperature of minus 195±10°C.

Preferably, the evaporating apparatus D to evaporate absorbed in the liquid 7 hydrogen at a pressure of 6 bar and a temperature of minus 195±10°With, in the evaporating apparatus E to evaporate absorbed in the liquid 5 hydrogen at a pressure of 6 bar and a temperature of minus 171±10°and in the distillation column F separation of carbon monoxide to hold p and a pressure of about 5 bar and the temperature in the upper part of the column of about minus 175° C and the temperature in the lower part of the column of about minus 155°C.

In the wash column G is desirable separation of impurities from consisting mainly of hydrogen gas fractions 6 to hold liquid nitrogen at a pressure of about 77 bar and a temperature of minus 185±10°C.

Preferably, the molar ratio of hydrogen to nitrogen in the exhaust from the top of the wash column G of the gas mixture to set to a value of about 3:1.

In the present invention two stage cleaning combined with each other in a single process, and the crude synthesis gas is cooled to cryogenic temperatures at which carbon monoxide can be separated from the synthesis gas. The remaining hydrogen is cleaned by flushing with nitrogen washing column G and then, if necessary mixed with another stream of nitrogen, used for synthesis of ammonia.

The proposed section of the setup is shown schematically in figure 1.

The list of items

A - heat exchanger;

In the separator;

With - evaporating device;

D - evaporating device;

E - evaporating device;

F - distillation column;

G - wash column;

1 - nitrogen under high pressure;

2 - synthesis gas;

3 - liquid nitrogen;

4 - gas fraction comprising hydrogen, carbon monoxide and traces of methane;

5 is a liquid fraction consisting of carbon monoxide, methane and odor is Yes;

6 - gas fraction comprising hydrogen and small amounts of carbon monoxide;

7 is a liquid fraction consisting of carbon monoxide, small amounts of methane and traces of hydrogen;

8 is a liquid fraction consisting of carbon monoxide, small amounts of methane and traces of hydrogen;

9 is a liquid fraction consisting of carbon monoxide and methane;

10 is a liquid fraction comprising methane and small amounts of carbon monoxide;

11 - liquid nitrogen;

12 is a liquid fraction consisting of carbon monoxide, nitrogen, hydrogen and small amounts of traces of argon;

13 is a gaseous fraction comprising carbon monoxide, small amounts of hydrogen and small amounts of methane;

14 is a gaseous fraction comprising carbon monoxide;

15 is a gaseous fraction comprising carbon monoxide, nitrogen, hydrogen, methane and traces of argon;

16 - gas fraction comprising hydrogen and nitrogen.

The composition shows the material flow is shown in table 1.

The heat exchanger But is preferably a multi-pass heat exchanger, in which heat transfer plate, usually made of aluminum. The heat exchanger And can take a lot of the allocated gas and liquid flows and to cool or to heat them to a predetermined temperature.

Synthesis gas 2 is fed through the heat exchanger And in section of the installation according to the invention, is separated in the separator In the gas fraction 4, rich in hydrogen and containing carbon monoxide, and the liquid fraction 5, rich in carbon monoxide and methane. This separation is carried out at a pressure of about 78 bar and a temperature of minus 171±10°C. the Gas fraction 4 further cooled in the heat exchanger and then sent to an evaporation apparatus C. the Liquid 5 will descomprimir to a pressure of about 6 bar and sent to an evaporation apparatus that is

Evaporator device is a device in which there is a further separation of hydrogen-enriched gas 4 is supplied from the separator, namely, gas 6, which consists mainly of hydrogen, and the liquid 7, which consists mainly of carbon monoxide. This separation is carried out at a pressure of about 78 bar and a temperature of minus 195±10°C. Gas 6, still contaminated with carbon monoxide, is introduced into the lower part of the wash column G. the Liquid 7 is divided into two streams, one for further purification, and the other with excess carbon monoxide, containing a little hydrogen. It can be used as a synthesis gas for the formation of products such as methanol, which are derived from carbon monoxide and hydrogen.

Carbon monoxide is 7 provided for the La further purification, will descomprimir to a pressure of about 6 bar and injected into the evaporating device D.

In the evaporation apparatus D in the process of the instant evaporation the evaporation of hydrogen absorbed in the carbon monoxide. The carbon monoxide can then, after passing through the heat exchanger And to be used as fuel gas 15. The flash evaporation process is carried out at a pressure of about 6 bar and a temperature of minus 195±10°C. the liquid 8 is sent to a distillation column F.

Obtained in the separator In the liquid 5 is sent to an evaporation apparatus, and the hydrogen absorbed in the liquid carbon monoxide, evaporated, and then he can be abstracted through a heat exchanger and used as fuel gas. It's an instant evaporation is carried out at a pressure of about 6 bar and a temperature of minus 171±10°C. Obtained in the evaporation apparatus E liquid 9 is sent to a distillation column F.

The distillation column F is used to obtain high-purity carbon monoxide with purity above 98% (by vol.). The distillation column F is under pressure of about 5 bar and has a top temperature of about minus 175°and in the lower part of about minus 155°C. In the distillation column F serves a mixture of carbon monoxide and methane from the evaporator E (9) and consisting mainly of carbon monoxide is idcast of the evaporator D. Distillation in the distillation column F is carried out by heating via a heat exchanger, through which is passed a synthesis gas of any composition, or by the discharge of fluid through at the bottom part of the distillation column F the outlet for collecting the liquid after passing through the heat exchanger And can be returned to the distillation column F (figure 1 not shown). Taken from the top of distillation column F the gas is almost completely pure carbon monoxide and sent back to the heat exchanger A. then it can be used for syntheses that require high-purity carbon monoxide.

Coming from the bottom of distillation column F the fluid is almost pure liquid methane, which descomprimir to a pressure of about 1.3 bar and which, after passing through the heat exchanger And can be used as fuel gas.

Wash column G is used for hydrogen purification by liquid nitrogen and simultaneously for hydrogen-nitrogen mixture. Wash column G is under pressure of about 77 bar and has a temperature of about minus 185±10°C. In the lower part of the wash column G by pipeline from evaporating apparatus is introduced almost pure hydrogen gas 6. In the wash column G's liquid nitrogen, with che is the washing column G is formed a mixture of hydrogen and nitrogen, which has a residual concentration of carbon monoxide and argon is less than 5 parts per million, respectively, less than 150 parts per million Selected from the top of the wash column G of the product then can be mixed with other streams of gaseous nitrogen, to set the molar ratio of hydrogen to nitrogen of about 3:1, in General, the molar ratio 2,995, and after passing through the heat exchanger And to use as a synthesis gas for ammonia synthesis. In the lower part of the wash column G is formed a mixture of liquid carbon monoxide, argon and nitrogen, the pressure is dropped to a value of 1.3 bar, and which, after passing through the heat exchanger And used as fuel gas.

Used washing column G liquid nitrogen with a purity of 99,995% liquefied in the heat exchanger and is supplied in a pressurised gaseous nitrogen leaching column G. This stream of nitrogen may also consist of several nitrogen flow introduced into the wash column G at different pressures. Then the pressure of the mixture of different nitrogen flows can be installed on required to process the value.

The use of liquid nitrogen has the purpose of cooling under low pressure liquid flows in the lower part of the wash column G.

Proposed in the invention section of the installation is the Central components is that the setup for the decomposition of the synthesis gas, described in the simultaneously filed application to the German patent DE 10226209 A1. It describes the whole process of separation of the synthesis gas. In this first allocate contained in the synthesis gas carbon monoxide. The remaining gas mixture consisting mainly of carbon monoxide and hydrogen, forms a stream of synthesis gas 2, while in the above-mentioned application describes the division exactly synthesis gas 2 using the proposed in the present invention partitions the installation.

The advantages offered by the invention section of the installation and the method of separation and purification of the synthesis gas prior to prior art lies primarily in the fact that:

a) provides a much more efficient heat transfer in plate heat exchangers;

b) does not require special cooling system in the form extender for purification of carbon monoxide, so the security of the whole system improves;

c) improving the reliability of gas supply due to the fact that in case of reduction needs either carbon monoxide or ammonia synthesis gas section of the installation according to the invention can be maintained in a cold condition, continuing the cleanup of the other synthesis gas, and very quickly again to return to full productivity for both synthesis gas;

d) proposed in the invention section of the installation can be built over conomice in comparison with two separate cryogenic systems.

Table 1
The gas flow12345678
Composition, % (vol.)
Methane2,591,0023,040,036,347,22
Carbon monoxide19,9416,4664,164,8182,0491,43
Argon0,100,070,420,010,400,45
Hydrogen77,3882,49KZT 12.3995,1511,220,90
Nitrogen99,9999,99
The pace. (°)4036-195-171-171-195-195-193
Pressure(bar abs.)772777777775,8
Steam share11010100
Flow rate (t/h)142149611832516741

Table 1 (continued)
The gas flow910111213141516
Composition, % (vol.)
Methane29,8091,690,416,340,7016,97
Carbon monoxide69,237,6669,0082,0498,1446,89to 2.57 ppm
Argon0,480,650,190,400,410,25
Hydrogen0,4813,31 11,220,7516,6974,97
Nitrogen99,9917,0819,2025,03
The pace. (°)-178to 143-185-19631313131
Pressure (bar abs.)5,85,8777676501,275
Steam share00001111
Flow rate (t/h)276,23926632543166

1. Section installation for the separation and purification of synthesis gas, characterized in that it consists of a device for the partial condensation synthesis gas, including

a heat exchanger for cooling is supplied to the section installation synthesis gas;

coupled with a heat exchanger And a separator for separating a synthesis gas 2 gas fraction 4, consisting mainly of hydrogen and carbon monoxide, and the liquid fraction 5, consisting basically in the from of carbon monoxide and methane;

evaporating apparatus further dividing supplied from the separator To the gas fraction 4 on the gas fraction 6, consisting mainly of hydrogen, and the liquid fraction 7, consisting mainly of carbon monoxide;

evaporating device D, which evaporates absorbed in the liquid 7 is hydrogen, and the remaining, containing mainly carbon monoxide liquid 8 may be directed to a distillation column F;

another evaporating device E, which is still absorbed in the liquid fraction 5 of the separator In the hydrogen is removed by evaporation and containing mainly carbon monoxide and methane liquid 9 may be directed to a distillation column F;

the distillation column F for the separation of gaseous carbon monoxide and produce methane gas from the exhaust from the lower part of the column of liquid;

and device for flushing with nitrogen, including

leaching column G for separating liquid nitrogen impurities from containing mainly hydrogen gas fraction 6 evaporator With and utilization of impurities in the fuel gas 12,

moreover, the device for nitrogen leaching is adjacent to the device for partial condensation.

2. Section installation according to claim 1, characterized in that the heat exchanger And can take a lot of the allocated gas and liquid flow is in and to cool or to heat them to a predetermined temperature.

3. Section installation according to claim 1, characterized in that the evaporators C, D and E are evaporators flash evaporation, which can be removed dissolved in the liquid gas.

4. Section installation according to claim 1, characterized in that the distillation column F has a heat exchanger, through which is passed a synthesis gas of any composition, or made at the bottom of this column removal for accumulating the liquid, which, after passing through the heat exchanger And can be returned to the distillation column F.

5. Section installation according to claim 1, characterized in that the wash column G has the inlet piping for gaseous and liquid nitrogen.

6. The method of separation and purification of the synthesis gas section of the installation according to one of claims 1 to 5, characterized in that the first conducting partial condensation synthesis gas and then washing with liquid nitrogen.

7. The method according to claim 6, characterized in that the separator To carry out the separation of the synthesis gas 2 gas fraction 4, consisting mainly of hydrogen and carbon monoxide, and the liquid fraction 5, consisting mainly of carbon monoxide and methane at a pressure of approximately 78 bar and a temperature of minus (171±10)°C.

8. The method according to claim 6 or 7, characterized in that the evaporating apparatus To carry out the separation gas fraction 4 consisting mainly of hydrogen, g is the gas fraction 6 and consisting mainly of carbon monoxide liquid 7 at a pressure of approximately 78 bar and a temperature of minus (195± 10)°C.

9. The method according to claim 6, characterized in that the evaporating apparatus D vapor absorbed in the liquid 7 hydrogen at a pressure of 6 bar and a temperature of minus (195±10)°C.

10. The method according to claim 6, characterized in that the evaporating apparatus E vapor absorbed in the liquid 5 hydrogen at a pressure of 6 bar and a temperature of minus (171±10)°C.

11. The method according to claim 6, characterized in that the distillation column F separation of carbon monoxide is carried out at a pressure of about 5 bar and the temperature in the upper part of the column of about minus 175°and the temperature in the lower part of the column of about minus 155°C.

12. The method according to claim 6, characterized in that the washing column G the separation of impurities from consisting mainly of hydrogen gas fraction 6 hold liquid nitrogen at a pressure of about 77 bar and a temperature of minus (185±10)°C.

13. The method according to claim 6, characterized in that the molar ratio of hydrogen to nitrogen in the exhaust from the top of the wash column G of the gas mixture set to a value of about 3:1.



 

Same patents:

The invention relates to a method of purification of coke oven gas from ammonia (NH3) and can be used in the coking industry

The invention relates to gas industry and can be used in schemes for the installations of regeneration of saturated solutions of glycols and other absorbents contaminated with mineral salts

The invention relates to gas industry and can be used on installations of gas transport, as well as during regeneration of absorbents contaminated with mineral salts
The invention relates to the technology of purification of coke oven gas from naphthalene and can be used in the manufacture of coke

The invention relates to methods coke gas purification from hydrogen sulfide leaching alkaline absorbent and can be used in coking plants

Catalytic reactor // 2296003

FIELD: chemical industry; production of the catalytic reactors.

SUBSTANCE: the invention is pertaining to the chemical industry, in particular, the catalytic reactor, which contains a set of the sheets forming the channels of the streams between them. In each channel of a stream there is the wavy material foils, which surfaces are coated with the catalytic material, except for the places where they contact to the sheets. On each end of the reactor there are the gas-collecting mains for the gaseous mixtures feeding in the channels of the streams. At that the gas-collecting mains are communicating with the adjacent channels separately. The reactor realizes feeding of the various gaseous mixtures in the adjacent channels , which may be under the different pressures, and the corresponding chemical reactions in them are also different. When one of the reactions is endothermic reaction, then the other reaction is exothermal; the heat is transmitted through the sheets separating the adjacent channels from the exothermic reaction to the endothermal reaction. The reactor may be used in the compact-type installation for realization of conversion of the methane with the steam, for production of the necessary heat at the methane catalytic combustion, and also Fisher-Tropsh synthesis, so this general method includes conversion of the methane in the long-chain hydrocarbons. The technical result of the invention is realization of the gaseous phases reactions at the increased pressures and especially for realization of the highly exothermal and endothermal reactions.

EFFECT: the invention ensures realization of the gaseous phases reactions at the heightened pressures and especially for realization of the highly exothermal and endothermal reactions.

9 cl, 6 dwg

FIELD: disproportionation process catalysts.

SUBSTANCE: invention relates to generation of hydrogen through steam conversion of carbon monoxide and development of catalyst for indicated process. Invention provides carbon monoxide conversion catalyst showing high catalytic activity and heat-conductivity and a process of steam conversion of carbon monoxide using indicated catalyst. Catalyst is characterized by heat-conductivity at least 1 W(mK)-1, which enables performing process with low temperature gradient in direction transversal to gas stream direction.

EFFECT: increased catalytic activity and heat-conductivity.

7 cl, 4 dwg, 3 tbl, 10 ex

FIELD: petroleum processing and petrochemistry.

SUBSTANCE: process comprises contacting hydrocarbon blend with solid porous phase, namely with methanol decomposition catalyst or methanol-to-hydrocarbons and water conversion catalyst. Contact is conducted such that at least part of hydrocarbon blend comes into contact with catalyst under suitable conditions for conversion of at least part of methanol at volumetric feed flow rate 3-15 h-1.

EFFECT: enabled removal of methanol without disturbing composition of hydrocarbon blend.

4 cl, 7 ex

FIELD: alternate fuels.

SUBSTANCE: invention relates to production of synthetic gas via catalytic hydrocarbon conversion in presence of oxygen-containing gases and/or water steam as well as to catalysts suitable for this process. Invention provides catalyst, which is complex composite constituted by supported precious element, or supported mixed oxide, simple oxide, transition element, wherein support is a metallic carrier made from metallic chromium and/or chromium/aluminum alloy coated with chromium and aluminum oxides or coated with oxides of chromium, aluminum, or mixtures thereof. Catalyst preparation procedure and synthetic gas production process are also described.

EFFECT: increased conversion of hydrocarbons, selectivity regarding synthetic gas, and heat resistance of catalyst at lack of carbonization thereof.

4 cl, 3 tbl, 9 ex

FIELD: hydrogen production processes.

SUBSTANCE: invention relates to catalytic processes of hydrogen production from hydrocarbon-containing gases. Method of invention comprises elevated-pressure catalytic decomposition of methane and/or natural gas into hydrogen and carbon followed by gasification of the latter with the aid of gasification reagent in several in parallel installed interconnected reactors, each of them accommodating preliminarily reduced catalyst bed. When one of reactors is run in methane and/or natural gas decomposition mode, the other gasifies carbon, the both operation modes being regularly switched. Operation period in one of the modes ranges from 0.5 to 10 h. Carbon gasification reagent is, in particular, carbon dioxide and catalyst utilized is reduced ferromagnetic thermally stabilized product consisting of iron oxides (30-80 wt %) and aluminum, silicon, magnesium, and titanium oxides. Methane and/or natural gas is decomposed at 625-1000°C and overpressure 1 to 40 atm.

EFFECT: ensured environmental safety and increased productivity of process.

3 cl, 1 dwg, 8 ex

FIELD: petrochemical industry; integral reactors and the methods of realization of exothermal and endothermic reactions.

SUBSTANCE: the invention is pertaining to the integral reactors of combustion (IRC), intended for realization of the exothermal and endothermic reactions. The IRC contains the exothermal reaction chamber (12) with the catalytic agents of the exothermic reaction (14,16), the endothermic reaction chamber (15) with the catalytic agent of the endothermic reaction (17), the open channels (18,19) for free flow of the of the medium stream through the chamber and the heat-conducting partition separating the chambers. It is preferable, that the exothermal or endothermic chambers would have the width (the minimum size in a direction perpendicular to the stream) - 2 mm or less. The invention also describes the separate models of the reactors and the methods of realization of the reactions in them. The invention ensures the safe work with the fuel, realization of the vapor reforming during the short time of the contact, the increased productivity per the unit of the volume of the reactor, extinguishing/inhibition of the gaseous-phase reactions.

EFFECT: The invention ensures the safe work with the fuel, realization of the vapor reforming during the short time of the contact, the increased productivity per the unit of the volume of the reactor, extinguishing/inhibition of the gaseous-phase reactions.

12 cl, 9 tbl, 27 dwg

FIELD: composition and structure of composite metal semiconductor meso-porous materials; titanium-dioxide-based catalyst for photo-chemical reactions.

SUBSTANCE: proposed catalyst is meso-porous titanium-dioxide-based material containing crystalline phase of anatase in the amount no less than 30 mass-% and nickel in the amount no less than 2 mass-%; material has porous structure at average diameter of pores from 2 to 16 nm and specific surface no less than 70 m2/g; as catalyst of photo-chemical reaction of liberation of hydrogen from aqua-alcohol mixtures, it ensures quantum reaction yield from 0.09 to 0.13. Method of production of such catalyst includes introduction of precursor - titanium tetraalkoxyde and template of organic nature, holding reagent mixture till final molding of three-dimensional structure from it at successive stages of forming sol, then gel, separation of reaction product and treatment of this product till removal of template; process is carried out in aqua-alcohol solvent containing no more than 7 mass-% of water; at least one of ligands is introduced into solvent as template; ligand is selected from group of macro-cyclic compounds containing no less than four atoms of oxygen and/or from complexes of said macro-cyclic compounds with ions of metals selected from alkaline or alkaline-earth metals or F-metals containing lithium, potassium, sodium, rubidium, cesium, magnesium, calcium, strontium, barium, lanthanum and cerium; mixture is stirred before forming of sol maintaining its temperature not above 35°C till final molding of three-dimensional structure from reagent mixture; mixture is held in open reservoir at the same temperature at free access of water vapor; after removal of template from three-dimensional structure, mixture is first treated with nickel salt solution during period of time sufficient for withdrawal of nickel ions from solution by pores of structure, after which is it kept in hydrogen-containing medium during period of time sufficient for reduction of nickel ions in pores of structure to metallic nickel.

EFFECT: enhanced sorption and photo-catalytic parameters; reproducibility of catalyst properties.

7 cl, 68 ex

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

FIELD: power engineering, in particular, hydrogen and oxygen production system.

SUBSTANCE: hydrogen and oxygen production system has electric plasmochemical reactor made in the form of high-pressure cylinder with spherical bottoms provided at its ends, said bottoms being equipped with screens, through which superhigh-frequency radiation waveguides are inserted. Waveguides are separated from internal volume of reactor by metal diaphragms with supporting grids and are provided with nozzles for supplying of carbonic acid and water steam, and hollow perforated electrodes of different poles for producing and separating of hydrogen and oxygen, with internal volumes of said electrodes being connected with driers, molecular sieves for separation of hydrogen, oxygen and carbonic acid, output refrigerators, gas holder and receiver.

EFFECT: increased energy efficiency owing to reduced consumption of power, consumption of hydrogen from storages in gas-and-steam units of auxiliary electric stations at night time.

2 dwg

FIELD: chemical industry; devices for production of the synthesis gas.

SUBSTANCE: the invention is pertaining to the radial type device for realization of oxidation of the gaseous hydrocarbon fuels with the help of the catalytic agent and may be used for production of the synthesis gas. The radial type device for production synthesis gas contains the gas-distribution perforated tube 3 and the catalytic agent 4. The catalytic agent is made in the form of the annular heat-conducting dispensing catalytic plates and the heat-conducting separators with the grooves alternating among themselves with formation of channels for the gaseous streams running and connected among themselves. On the both sides of the separator 6 there are grooves 7 made in the form of the evolvent from the center to the periphery. The annular plates of the catalytic agent are mounted perpendicularly to the axis of the shafts of the gas-distribution perforated tube 3. Inside of the gas-distribution perforated tube 3 there is the starting system, which consists of the mixer 1 with the ignition plug 2 or the electric heating component. The invention presents the compact and effective device.

EFFECT: the invention presents the compact and effective radial type device used for realization of oxidation of the gaseous hydrocarbon fuels with the help of the catalytic agent and for production of the synthesis gas.

6 cl, 3 dwg

Catalytic reactor // 2296003

FIELD: chemical industry; production of the catalytic reactors.

SUBSTANCE: the invention is pertaining to the chemical industry, in particular, the catalytic reactor, which contains a set of the sheets forming the channels of the streams between them. In each channel of a stream there is the wavy material foils, which surfaces are coated with the catalytic material, except for the places where they contact to the sheets. On each end of the reactor there are the gas-collecting mains for the gaseous mixtures feeding in the channels of the streams. At that the gas-collecting mains are communicating with the adjacent channels separately. The reactor realizes feeding of the various gaseous mixtures in the adjacent channels , which may be under the different pressures, and the corresponding chemical reactions in them are also different. When one of the reactions is endothermic reaction, then the other reaction is exothermal; the heat is transmitted through the sheets separating the adjacent channels from the exothermic reaction to the endothermal reaction. The reactor may be used in the compact-type installation for realization of conversion of the methane with the steam, for production of the necessary heat at the methane catalytic combustion, and also Fisher-Tropsh synthesis, so this general method includes conversion of the methane in the long-chain hydrocarbons. The technical result of the invention is realization of the gaseous phases reactions at the increased pressures and especially for realization of the highly exothermal and endothermal reactions.

EFFECT: the invention ensures realization of the gaseous phases reactions at the heightened pressures and especially for realization of the highly exothermal and endothermal reactions.

9 cl, 6 dwg

FIELD: disproportionation process catalysts.

SUBSTANCE: invention relates to generation of hydrogen through steam conversion of carbon monoxide and development of catalyst for indicated process. Invention provides carbon monoxide conversion catalyst showing high catalytic activity and heat-conductivity and a process of steam conversion of carbon monoxide using indicated catalyst. Catalyst is characterized by heat-conductivity at least 1 W(mK)-1, which enables performing process with low temperature gradient in direction transversal to gas stream direction.

EFFECT: increased catalytic activity and heat-conductivity.

7 cl, 4 dwg, 3 tbl, 10 ex

FIELD: petroleum processing and petrochemistry.

SUBSTANCE: process comprises contacting hydrocarbon blend with solid porous phase, namely with methanol decomposition catalyst or methanol-to-hydrocarbons and water conversion catalyst. Contact is conducted such that at least part of hydrocarbon blend comes into contact with catalyst under suitable conditions for conversion of at least part of methanol at volumetric feed flow rate 3-15 h-1.

EFFECT: enabled removal of methanol without disturbing composition of hydrocarbon blend.

4 cl, 7 ex

FIELD: alternate fuels.

SUBSTANCE: invention relates to production of synthetic gas via catalytic hydrocarbon conversion in presence of oxygen-containing gases and/or water steam as well as to catalysts suitable for this process. Invention provides catalyst, which is complex composite constituted by supported precious element, or supported mixed oxide, simple oxide, transition element, wherein support is a metallic carrier made from metallic chromium and/or chromium/aluminum alloy coated with chromium and aluminum oxides or coated with oxides of chromium, aluminum, or mixtures thereof. Catalyst preparation procedure and synthetic gas production process are also described.

EFFECT: increased conversion of hydrocarbons, selectivity regarding synthetic gas, and heat resistance of catalyst at lack of carbonization thereof.

4 cl, 3 tbl, 9 ex

FIELD: hydrogen production processes.

SUBSTANCE: invention relates to catalytic processes of hydrogen production from hydrocarbon-containing gases. Method of invention comprises elevated-pressure catalytic decomposition of methane and/or natural gas into hydrogen and carbon followed by gasification of the latter with the aid of gasification reagent in several in parallel installed interconnected reactors, each of them accommodating preliminarily reduced catalyst bed. When one of reactors is run in methane and/or natural gas decomposition mode, the other gasifies carbon, the both operation modes being regularly switched. Operation period in one of the modes ranges from 0.5 to 10 h. Carbon gasification reagent is, in particular, carbon dioxide and catalyst utilized is reduced ferromagnetic thermally stabilized product consisting of iron oxides (30-80 wt %) and aluminum, silicon, magnesium, and titanium oxides. Methane and/or natural gas is decomposed at 625-1000°C and overpressure 1 to 40 atm.

EFFECT: ensured environmental safety and increased productivity of process.

3 cl, 1 dwg, 8 ex

Up!