Method for preparing motor fuels

FIELD: petroleum chemistry.

SUBSTANCE: method involves preparing synthesis gas, catalytic conversion of synthesis gas in reactor for synthesis of dimethyl ether (DME) at enhanced temperature and pressure wherein synthesis gas is contacted with catalyst followed by cooling the gaseous mixture and its separation for liquid and gaseous phases. Dimethyl ether is isolated from the liquid phase that is fed into catalytic reactor for synthesis of gasoline and the gaseous phase containing unreacted components of synthesis gas is fed to repeated catalytic conversion into additional reactor for synthesis of DME being without the parent synthesis gas. Residue of gaseous phase containing components of synthesis gas not reacted to DME after repeated catalytic conversion in additional reactor for synthesis of DME are oxidized in reactor for synthesis of carbon dioxide. Then carbon dioxide is separated and mixed its with natural gas at increased temperature and pressure that results to preparing synthesis gas that is fed to the catalytic conversion into reactor for synthesis of DME. Invention provides increasing yield of gasoline fraction and decrease of carbon dioxide waste in atmosphere.

EFFECT: improved method of synthesis.

4 cl, 1 tbl, 1 dwg, 1 ex

 

The invention relates to the field of hydrocarbon processing, and in particular to methods of production of synthetic motor fuels and, in particular, to a method for producing dimethyl ether (DME) and synthetic gasoline by catalytic conversion of synthesis gas (SG).

A known method of producing hydrocarbons developed by Haldor Topsoe AS, in the processing of synthesis gas containing hydrogen and carbon monoxide and having a molar ratio of CO/H2above 1, and provided that the synthesis gas supplied to the conversion, has a molar ratio CO/CO2from 5 to 20 for U.S. patent No. 4481305, class C 07 C 1/04, 1/20, 1984. According to the similar process is carried out in two sequential reactors at a pressure of 0.5 to 10.0 MPa without intermediate selection of products after the first reactor. In the first reactor synthesis gas in contact with one or more catalysts, leading the transformation of synthesis gas at a temperature of 150-400°in methanol and then in the same reactor in DME. Then the gas mixture is directed to the second reactor, where in the presence of a zeolite catalyst at a temperature of 150-600°DME convert mostly in liquid under normal conditions hydrocarbons.

The main disadvantages of the method according to U.S. patent No. 4481305 are emitted into the atmosphere neprivrednih components of the synthesis gas after the second reactor, and neither the cue output gasoline fraction in relation to the submitted feedstock carbon (29 wt.%).

A known process for producing gasoline from synthesis gas, in which synthesis gas is converted into gas through liquid-phase process of dimethyl ether as an intermediate product for U.S. patent No. 5459166, class C 07 C 001/04,1995. Dimethyl ether is converted into gasoline over a zeolite catalyst ZSM-5 at temperatures 340-540°C.

The disadvantage of this process is the emission of unreacted components of synthesis gas, reducing the yield of liquid hydrocarbons.

Also known a method of producing motor fuels from carbonaceous raw materials by RF patent No. 2143417, class C 07 C 1/04, 41/06, 1999. A method of producing motor fuels includes a first stage contacting of the feedstock, a synthesis gas (mixture of CO, CO2and H2with a catalyst comprising zeolite ZSM-5 and metal oxide component containing (wt.%): CuO 38-64, ZnO 24-34, Cr2About30-22, Al2About36-9, mixed in a mass ratio of 20-50/80-50, the gas flow after the first stage reactor is cooled and separated into a liquid fraction and a gas phase containing neprevyshenie components of synthesis gas and dimethyl ether, and the liquid fraction is further isolated DME, and the gas phase is divided into two streams - one is mixed with the synthesis gas and is fed into the same reactor of the first stage. The second gas stream is directed to the second stage, the DG is in contact with the catalyst, consisting of zeolite ZSM-5 and metal oxide component containing (wt.%): ZnO 65-70, Cr2About329-34, W2O51, mixed in a mass ratio of 30-99/70-1, is the conversion of DME and components of synthesis gas into gasoline fraction, gaseous hydrocarbons and water fraction.

The main disadvantage of this method of producing motor fuels from carbonaceous raw materials by RF patent No. 2143417 is the output of the gas flow of the circulation circuit, which reduces the yield of DME, and hence the gasoline fraction in calculation to the feed oxides of carbon.

There is also known a method of producing motor fuels from natural gas by RF patent No. 2226524, class C 07 C 1/04, 41/06, 43/04, With 10 G 3/00, 2004, adopted as the closest analogue (prototype) of the proposed method. A method of producing motor fuels includes obtaining synthesis gas non-catalytic gas-phase oxidative conversion of natural gas with oxygen at a temperature of 800-1500°and a pressure of 1-10 MPa. This is followed by catalytic conversion of synthesis gas in the synthesis reactor, dimethyl ether, followed by cooling the product gas mixture, and the division into liquid and gas phase. Thus from the gas phase produce DME, which is sent to the catalytic reactor synthesis gas, and a gas phase containing neprevyshenie component is s synthesis gas, sent for re-catalytic conversion in additional synthesis reactor DME without mixing with the original synthesis gas. The gas flow after additional catalytic synthesis reactor DME cooled and share the gas flow on the liquid and gas phase from the gas stream condense liquid products - water and dimethyl ether, and the gas phase, representing the remains unreacted components of synthesis gas, is removed from the process. To obtain a gasoline fraction DME sent to the catalytic reactor synthesis gas, in which DME is injected into contact with a catalyst consisting of a high-silica zeolite and metal oxide components such as ZnO, Na2O, oxides of rare earth metals, and turn the DME to gasoline fraction, gaseous hydrocarbons and water fraction, followed by separation of the gasoline fraction.

The main disadvantage of this method of producing motor fuels from natural gas is neprivrednih components of the synthesis gas from the process, which reduces the yield of DME, and hence the gasoline fraction in calculation to the feed oxides of carbon. Another disadvantage of this method is the emission of environmentally harmful carbon dioxide contained in the remainder of the synthesis gas.

The objective of the proposed method the floor with the help of motor fuels is to increase the yield of dimethyl ether and accordingly, the gasoline fraction in the calculation of the recycled carbon dioxide by utilizing neprivrednih components of synthesis gas, as well as reducing emissions of carbon dioxide into the atmosphere.

The task in the invention is solved by a method for producing motor fuels from natural gas includes obtaining synthesis gas, the catalytic conversion of synthesis gas in the reactor for the synthesis of dimethyl ether (DME) at elevated temperature and pressure at which the synthesis gas is introduced into contact with the catalyst with subsequent cooling of the gas mixture and the division into liquid and gas phase from the liquid phase produce dimethyl ether, which is sent to the catalytic reactor synthesis gas, and a gas phase containing neprevyshenie components of synthesis gas, is directed to re-catalytic conversion in additional synthesis reactor DME without adding a source of synthesis gas, while the remainder of the gas phase containing neprevyshenie in DME components of the synthesis gas after the second catalytic conversion in the secondary reactor for the synthesis of dimethyl ether, are oxidized in the reactor for the synthesis of carbon dioxide, then separate the carbon dioxide and mix it with natural gas at elevated temperature and pressure, resulting in receiving the synthesis gas which is sent n the catalytic conversion of the synthesis reactor DME.

Oxidation of the residue gas phase, including neprevyshenie components of synthesis gas, namely carbon monoxide, carbon dioxide, hydrogen and nitrogen, can be produced by atmospheric oxygen at a temperature of 400-700°obtaining a hot gas mixture containing carbon dioxide, nitrogen and water vapor.

Separation of carbon dioxide from nitrogen and water vapor can be produced by cooling the hot gas mixture in the heat exchanger-the heat exchanger, then cooled gas mixture may be directed into the lower part of the absorber of carbon dioxide, in which it is brought into countercurrent contact with a cold poor absorbent solution, with saturated solution of absorbent carbon dioxide, then the solution of absorbent material saturated with carbon dioxide, is heated in the heat exchanger-the heat exchanger and serves in desorber-regenerator, in which the absorbent solution is separated into a stream of hot poor solution of an absorbent and a stream of carbon dioxide.

The resulting carbon dioxide can be mixed with natural gas at a temperature of 700-1300°and a pressure of 0.5 to 5.0 MPa, thus receive the synthesis gas, which serves to catalytic conversion in the reactor for the synthesis of dimethyl ether.

Thanks to the present method obtained the technical result, namely increased yield of DME and, accordingly, the gasoline fraction due to increased the I degree of conversion of carbon oxides in DME by recycling neprivrednih monoxide synthesis gas. In addition, reduced emissions of carbon dioxide into the atmosphere, which is consistent with the requirements of the Kyoto Protocol.

The drawing shows a process flow diagram for the production of motor fuels.

According to the claimed method of producing motor fuels in high temperature reactor (TUE) 1 serving of natural gas and air, where at elevated temperatures 800-1500°and a pressure of 1-10 MPa by direct non-catalytic gas-phase oxidation conversion gain synthesis gas (mixture of CO, H2, CO2and N2), which is sent to the heat exchanger, and then to the catalytic reactor 2 synthesis of dimethyl ether, where the synthesis gas at a temperature of 220-240°To enter into contact with a catalyst composed of metal oxide components, such as CuO, ZnO, Cr2About3and Al2About3.

The gas flow after the catalytic reactor 2 synthesis of dimethyl ether is cooled and subjected to absorption in countercurrent flow with a liquid methanol scrubber 3, separating the gas stream into liquid and gas phase from the gas stream secrete water and dimethyl ether. The gas phase, representing neprevyshenie components of synthesis gas, is fed into an additional catalytic reactor 4 synthesis of DME without mixing with the original synthesis gas at a temperature of 220-240°where these neprevyshenie components of the synthesis gas is introduced into contact with the catalyst, the state is representative of the metal oxide components.

The gas flow after additional catalytic reactor 4 synthesis of dimethyl ether is cooled and subjected to absorption in countercurrent flow with a liquid methanol in the scrubber 5, separating the gas stream into liquid and gas phase from the gas stream condense liquid products - water and dimethyl ether, and the gas phase, representing the remains unreacted components of the synthesis gas, are not taken from the process and sent to the reactor 6 synthesis of carbon dioxide.

The high solubility of DME, methanol and water contributes to its extraction from the gas stream. Next, the liquid phase, representing enriched dimethyl ether methanol scrubber 3 and 5 is sent to distillation column 7, where separating dimethyl ether from methanol and water at a pressure of 1.2 MPa, which allows to obtain DME as the target product. In this case, after distillation column 7 DME serves in the memory 8, and the methanol is returned to the process.

Neprevyshenie components of synthesis gas (CO, H2, CO2and others) in the reactor 6 synthesis of carbon dioxide mixed with air and oxidize at a temperature of 400-700°obtaining a stream of hot gas containing mainly nitrogen, water vapor and carbon dioxide. The stream of hot gas is directed into the heat exchanger-the heat exchanger 9, where take away from it the heat is on and receive a stream of cold gas, which is directed to the bottom of the absorber 10 of carbon dioxide. In absorber 10 of the carbon dioxide stream of cold gas is brought into contact with a stream of cold poor absorbent solution fed to the upper part of the absorber 10 carbon dioxide countercurrent to the flow of cold gas, and absorb carbon dioxide from the cold gas absorption with receiving threads of waste gas, which is removed from the upper part of the absorber 10, carbon dioxide, and a stream rich in carbon dioxide absorbent that is directed to the heat exchanger-the heat exchanger 9. In the heat exchanger-the heat exchanger 9, the flow of the saturated absorbent is heated by the removal of heat from the hot gas stream and serves obtained hot stream of saturated absorbent in the middle part of desorber-regenerator 11. In desorber-regenerator 11, the flow of hot saturated absorbent share by heating the adsorbent in the lower part of desorber-regenerator 11 to the flow of hot poor absorbent withdrawn from the lower part of desorber-regenerator 11, and the flow of carbon dioxide, which is removed from the upper part of desorber-regenerator 11 and sent for recycling in the high temperature reactor 1, where carbon dioxide is mixed with methane at a temperature of 700-1300°and a pressure of 0.5 to 5.0 MPa and receive the synthesis gas, which is cooled and sent to a catalytic conversion the synthesis reactor DME 2. The flow of hot poor absorbent is sent to the refrigerator 12, where dissipate heat from the obtaining of the flow of cold poor absorbent, who served in the upper part of the absorber 10.

To obtain a gasoline fraction of dimethyl ether (DME) from distillation column 7 is sent to the catalytic reactor 13 synthesis gas, in which DME at a temperature of 380-420°To enter into contact with a catalyst consisting of a high-silica zeolite and metal oxide components such as ZnO, Na2O, oxides of rare earth metals, and turn the DME to gasoline fraction, gaseous hydrocarbons and water fraction, followed by separation of the gasoline fraction.

The following is an example illustrating the applicability of the proposed method.

Example

Description of raw material:

The composition of the air, vol.%: nitrogen 78,09; oxygen 20,95; argon 0,93; undefined gases else.

The natural gas composition, vol.%: methane 97%; ethane, 2%; unspecified gases else.

The composition of the flow of carbon dioxide sent for recycling, vol.%: carbon dioxide 99%; unspecified gases else.

In the head part of the high-temperature reactor (TUE) 1 serving of natural gas and air and at a temperature of 1600°and the pressure of 5.00 MPa and direct non-catalytic gas-phase oxidation conversion receive the synthesis gas composition (in terms of dry ha is)

Hydrogen3,2
Carbon monoxide14,5
Carbon dioxide2,1
Methane0,56
NitrogenRest

Conversion of the carbon source of hydrocarbons to carbon monoxide 89%.

Recycled carbon dioxide is mixed with additional natural gas and served in the middle part of the high temperature reactor 1, where by mixing with the previously produced synthesis gas to produce a synthesis of additional synthesis gas by nakateleeli carbon dioxide reforming of natural gas at a temperature of 1100°and the pressure of 5.00 MPa with the final composition (in terms of dry gas)

Hydrogen34,2
Carbon monoxide20,5
Carbon dioxide3,6
Methane0,8
NitrogenRest

Conversion of the recycled carbon dioxide and additional natural gas carbon monoxide is 80%.

Due to this, prevent the emission of carbon dioxide, which improves the environmental performance of the method of receipt.

The resulting synthesis gas e.g. the keys in the catalytic reactor 2 synthesis of dimethyl ether, where the synthesis gas is introduced into contact with a catalyst composed of metal oxide components, such as

CuO 21-50 wt.%, ZnO 20-30 wt.%, Cr2About315-25 wt.% and Al2About35-40 wt.%, if the initial temperature 220°C, end 260°and receive gas composition (vol.%):

ComponentBeginning synthesisThe end of synthesisAfter removing DME
Hydrogen34,226,127,5
Carbon monoxide20,510,010,5
Carbon dioxide3,69,19,6
Methane0,80,961,00
Nitrogenof 40.948,951,4
DME04,8Less than 0.1
Methanol00,25Less than 0.1

Conversion of the source of carbon monoxide in DME 58,3%.

Conversion of the source of carbon monoxide in methanol 1%.

The resulting mixture is cooled to 50°With and separated into liquid and gas phase in countercurrent flow with a liquid methanol scrubber 3 at a pressure of 5.1 MPa, enriched dimethyl ether methanol directed to the Department is giving DME in a distillation column 7 when the pressure in the helmet 1.2 MPa and a temperature of 60° With, then DME serves in the drive, and the methanol is returned to the process.

Containing neprevyshenie components of the synthesis gas is heated to 220°With, sent for re-catalytic conversion in the reactor 4 is in contact with a catalyst of the same composition at a pressure of 5 MPa and a final temperature of 250°C.

The resulting composition has,%:

ComponentBeginning synthesisThe end of synthesisAfter extraction, the
DME
Hydrogen27,523,924,4
Carbon monoxide10,56,26,4
Carbon dioxide9,611,7to 12.0
Methane1,001,11,1
Nitrogen51,455,056,1
DMELess than 0.11,5Less than 0.1
MethanolLess than 0.10,5Less than 0.1

Additional conversion in the DME: 50,6%

Additional conversion in the ethanol: 5,1%

Full conversion to the desired products from the carbon source natural gas: 96,3%

The resulting mixture is cooled to 50°With and separated into liquid and gas phases in countercurrent flow with a liquid methanol in the scrubber 5 at a pressure of 4.9 MPa, enriched dimethyl ether methanol is directed to the separation of dimethyl ether in the same distillation column 7 when the pressure in the helmet 1.2 MPa and a temperature of 60°C, after which the DME is served in the drive, and the methanol is returned to the process.

Remaining after the extraction of DME synthesis gas containing carbon dioxide, the remainder of the carbon monoxide, the remainder of the hydrogen, methane and nitrogen, is directed into the reactor 6 synthesis of carbon dioxide which oxidizes the residual synthesis gas is air at a temperature of 550°to provide hot gas, containing nitrogen, argon, water vapor, carbon dioxide.

The composition of the gas obtained in the reactor 6,%:

Nitrogen74,6
Argon0,6
Carbon dioxidethe 10.1
Water vapors14,7

The content of environmentally harmful carbon monoxide, nitrogen oxides and ammonia does not exceed MPC.

To separate carbon dioxide from nitrogen and water vapor obtained in the reactor 6 hot gas napravlyayut the heat exchanger-the heat exchanger 9, where it is cooled to 50°and the resulting cold gas is directed into the lower part of the absorber 10 of carbon dioxide, which lead him into countercurrent contact with a cold poor absorbent (water solution of monoethanolamine) and receive a stream of saturated carbon dioxide absorbent and a discharge gas containing nitrogen 98 vol.%, argon of 1.3 vol.%, carbon dioxide else.

Saturated with carbon dioxide absorbent is fed into the heat exchanger-the heat exchanger 9, is heated by heat from the hot gas from the reactor 6 and send desorber-regenerator 11, which is shared by desorption on the recirculating carbon dioxide and hot poor absorbent. Hot poor absorbent is cooled in the refrigerator 12 and received poor cold absorbent is directed to the absorption of carbon dioxide in the absorber 10. The recirculating carbon dioxide is directed to a mixture of natural gas and fed into the reactor TUE 1 for receiving the synthesis gas.

The gasoline fraction produced by directing DME in the catalytic reactor 13 synthesis of gasoline at 2 MPa, in which DME is injected into contact with a catalyst consisting of a high-silica zeolite WHC produced by THE 38.401528-85 and the ratio of SiO2/Al2O3= 42 (70%) and metal oxide components such as ZnO (2%), Na2O (0,05-0,1%), oxides of rare earth metals (1%), and convert the dimethyl ether in petrol FR is the Ktsia at a temperature of 320-360° With, gaseous hydrocarbons and water fraction, followed by separation of the gasoline fraction. The yield of gasoline fraction 90% carbon DME. The composition of the gasoline fraction is given in table:

Name of the componentThe content of components in the gasoline fraction,%
Paraffins40,07
Paraffins50,67
Paraffins63,57
Paraffins77,26
Paraffins C86,84
Paraffins94,69
Naphthenes With60,25
Naphthenes With70,27
Naphthenes, C83,86
Naphthenes With92,98
Naphthenes With1012,80
Naphthenes, C10-C1125,83
Aromatic hydrocarbon, C813,03
Aromatic hydrocarbons With917,88
Total100

The resulting composition of the hydrocarbon components of gasoline fraction corresponds to motor fuels with an octane number is om AI-92.

The technical result

- Due to the recycling of carbon dioxide the carbon dioxide emission is reduced more than 100 times.

- Due to the recycling of carbon dioxide increased the degree of conversion of the original natural gas gasoline fraction to 95%.

- Due to the oxidation of the residual synthesis gas with air at a temperature of 550°With a reduced content of carbon monoxide, nitrogen oxides and ammonia in the gas emissions below the exposure limits.

The inventive method of producing motor fuels from natural gas has increased the yield of DME and, consequently, gasoline fractions by increasing the degree of conversion of carbon oxides by utilizing neprivrednih monoxide synthesis gas to DME, and also reduced the emissions of environmentally harmful carbon dioxide.

1. A method of producing motor fuels from natural gas, including the production of synthesis gas, the catalytic conversion of synthesis gas in the reactor for the synthesis of dimethyl ether (DME) at elevated temperature and pressure at which the synthesis gas is introduced into contact with the catalyst with subsequent cooling of the gas mixture and the division into liquid and gas phase from the liquid phase produce dimethyl ether, which is sent to the catalytic reactor synthesis gas, and a gas phase containing neprevyshenie components of synthesis gas, is directed to p is repeated catalytic conversion in additional synthesis reactor DME without adding the source synthesis gas, characterized in that the remainder of the gas phase, containing not converted into DME components of the synthesis gas after the second catalytic conversion in the secondary reactor for the synthesis of dimethyl ether, are oxidized in the reactor for the synthesis of carbon dioxide, then separate the carbon dioxide and mix it with natural gas at elevated temperature and pressure, resulting in a gain synthesis gas, which is directed to catalytic conversion in the reactor for the synthesis of dimethyl ether.

2. The method according to claim 1, characterized in that the oxidation residue gas phase, including neprevyshenie components of synthesis gas, namely carbon monoxide, carbon dioxide, hydrogen and nitrogen, to produce air at a temperature of 400-700°obtaining a hot gas mixture containing carbon dioxide, nitrogen and water vapor.

3. The method according to claim 1, characterized in that the separation of carbon dioxide from nitrogen and water vapor carried out by cooling the hot gas mixture in the heat exchanger-the heat exchanger, then cooled gas mixture is sent to the bottom of the absorber of carbon dioxide, in which it is brought into countercurrent contact with a cold poor absorbent solution, with saturated solution of absorbent carbon dioxide, then the solution of absorbent material saturated with carbon dioxide, is heated in the heat exchanger-the heat exchanger and serves in desorber-regenerator, in which process the absorbent is separated into a stream of hot poor solution of an absorbent and a stream of carbon dioxide.

4. The method according to claim 1, characterized in that the carbon dioxide is mixed with natural gas at a temperature of 700-1300°and a pressure of 0.5 to 5.0 MPa, thus receive the synthesis gas.



 

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8 cl, 1 tbl, 1 ex

FIELD: alternate fuel production and catalysts.

SUBSTANCE: synthesis gas containing H2, CO, and CO2 is brought into contact, in first reaction zone, with bifunctional catalyst consisting of (i) metal oxide component containing 65-70% ZnO, 29-34%, Cr2O3, and up to 1% W2O5 and (ii) acid component comprised of zeolite ZSM-5 or ZSM-11, beta-type zeolite or crystalline silica-alumino-phosphate having structure SAPO-5 at silica-to-alumina molar ratio no higher than 200, whereas, in second reaction zone, multifunctional acid catalyst is used containing zeolite ZSM-5 or ZSM-11 and having silica-to-alumina molar ratio no higher than 200.

EFFECT: increased selectivity with regard to C5+-hydrocarbons and increased yield of C5+-hydrocarbons based on synthesis gas supplied.

7 cl, 2 tbl, 15 ex

FIELD: engineering of Fischer-Tropsch catalysts, technology for producing these and method for producing hydrocarbons using said catalyst.

SUBSTANCE: catalyst includes cobalt in amount ranging from 5 to 20 percents of mass of whole catalyst on argil substrate. Aforementioned substrate has specific surface area ranging from 5 to 50 m2/g. Catalyst is produced by thermal processing of argil particles at temperature ranging from 700 to 1300°C during period of time from 1 to 15 hours and by saturating thermally processed particles with cobalt. Method for producing hydrocarbon is realized accordingly to Fischer-Tropsch method in presence of proposed catalyst.

EFFECT: possible achievement of high selectivity relatively to C5+ at low values of diffusion resistance inside particles.

3 cl, 9 ex, 9 dwg

FIELD: organic chemistry.

SUBSTANCE: claimed method includes a) reaction of carbon monoxide and hydrogen in presence of effective amount of Fischer-Tropsch catalyst; b) separation of at least one hydrocarbon cut containing 95 % of C15+-hydrocarbons from obtained hydrocarbon mixture; c) contacting separated cut with hydrogen in presence of effective amount of hydration catalyst under hydration conditions; d) treatment of hydrated hydrocarbon cut by medium thermal cracking; and e) separation of mixture, including linear C5+-olefins from obtained cracking-product. Method for production of linear alcohols by oxidative synthesis of abovementioned olefins also is disclosed.

EFFECT: improved method for production of linear olefins.

12 cl, 3 tbl, 1 dwg, 2 ex

FIELD: organic synthesis catalysts.

SUBSTANCE: invention relates to methods for preparing catalyst precursors and group VIII metal-based catalysts on carrier, and to a process of producing hydrocarbons from synthesis gas using catalyst of invention. Preparation of precursor of group VIII metal-based catalyst comprises: (i) imposing mechanical energy to mixture containing refractory oxide, combining catalyst precursor with water to form paste comprising at least 60 wt % of solids, wherein ratio of size of particles present in system in the end of stage (i) to that in the beginning of stage (i) ranges from 0.02 to 0.5; (ii) mixing above prepared paste with water to form suspension containing no more than 55% solids; (iii) formation and drying of suspension from stage (ii); and (iv) calcination. Described are also method of preparing group VIII metal-based catalyst using catalyst precursor involving reduction reaction and process for production of hydrocarbons by bringing carbon monoxide into contact with hydrogen are elevated temperature and pressure in presence of above-prepared catalyst.

EFFECT: increased catalytic activity and selectivity.

12 cl, 1 tbl, 3 ex

FIELD: petrochemical process catalysts.

SUBSTANCE: invention relates to synthesis of C5-C100-hydrocarbons from CO and H2, which catalyst contains carrier based on alumina prepared from gibbsite-structure aluminum hydroxide and cobalt in concentration of 15 to 50%. Carrier is prepared by mixing dry cobalt compound with dry gibbsite-structure aluminum hydroxide at cobalt-to aluminum molar ratio between 1:1 and 1:30, followed by calcination, impregnation (in two or more steps) with aqueous cobalt salt solution, and heat treatment. Invention also discloses process of producing C5-C100-hydrocarbons using above catalyst.

EFFECT: increased selectivity of catalyst regarding production of high-molecular hydrocarbons at reduced yield of methane.

7 cl, 1 tbl, 10 ex

FIELD: catalyst preparation methods.

SUBSTANCE: invention provides Fischer-Tropsch catalyst, which consists essentially of cobalt oxide deposited on inert carrier essentially composed of alumina, said cobalt oxide being consisted essentially of crystals with average particle size between 20 and 80 Å. Catalyst preparation procedure comprises following stages: (i) preparing alumina-supported intermediate compound having general formula I: [Co2+1-xAl+3x(OH)2]x+[An-x/n]·mH2O (I), wherein x ranges from 0.2 to 0.4, preferably from 0.25 to 0.35; A represents anion; x/n number of anions required to neutralize positive charge; and m ranges from 0 to 6 and preferably is equal to 4; (ii) calcining intermediate compound I to form crystalline cobalt oxide. Invention also described a Fischer-Tropsch process for production of paraffin hydrocarbons in presence of above-defined catalyst.

EFFECT: optimized catalyst composition.

16 cl, 12 tbl, 2 ex

FIELD: petroleum chemistry, chemical technology.

SUBSTANCE: method involves carrying out the preparing synthesis gas by the gaseous oxidative conversion of natural gas with air oxygen, catalytic conversion of synthesis gas to a catalyzate followed by its cooling and separating and feeding a liquid phase into reactor for synthesis of gasoline. For aim reducing the cost of manufacturing catalytic preparing methanol is carried out in the synthesis reactor wherein methanol is fed into reactor for preparing high-octane components of gasoline that are stabilized and separated for liquid components and fatty gas that is fed into reactor for preparing oligomer-gasoline. Then liquid components from reactors wherein high-octane components of gasoline and oligomer-gasoline are prepared and then combined, and the mixture is stabilized. Water formed in all synthesis reactions after separating is removed separately, combined and fed to the fresh water preparing block and formed nitrogen is fed for storage with partial using in technological cycle and in storage of synthetic fuel. The unreacted depleted synthesis gas from block wherein methanol is prepared is used for feeding methanol into reactor sprayers for preparing high-octane component of gasoline, and unreacted gases from reactor for preparing oligomer-gasoline are fed into generator for synthesis gas. Also, invention claims the device for realization of the method. The device consists of blocks for preparing synthesis gas, catalytic conversion of synthesis gas to catalyzate and preparing gasoline and made of two separate reactors for preparing high-octane additive of gasoline and oligomer-gasoline. The device is fitted additionally by block for preparing fresh water and nitrogen collector. The reactor sprayers are connected with intermediate capacity for collection of methanol and with reactor for synthesis of methanol and block for preparing methanol, and reactor for preparing oligomer-gasoline is connected pneumatically with block for preparing synthesis gas. Invention provides the development of method for the combined preparing the fuel and fresh water.

EFFECT: improved preparing method.

2 cl, 6 dwg, 2 ex

FIELD: petrochemical process catalysts.

SUBSTANCE: preparation of crusted metallic catalyst comprises: (i) applying suspension containing diluent, catalytically active metal selected from cobalt and ruthenium groups, and optionally first refractory element (atomic number at least 20) oxide onto surface of carrier particles to form wet coating and (ii) removing at least part of diluent from wet coating, said suspension containing at least 5% by weight of catalytically active metal based on the weight of calcination residue, which would result after drying and calcination of suspension. Crusted metallic catalyst itself and hydrocarbon production process are also described.

EFFECT: simplified catalyst preparation technology, improved physicochemical properties of catalyst as well as selectivity thereof, and increased productivity of hydrocarbon production process.

10 cl, 1 tbl, 3 ex

FIELD: industrial inorganic synthesis and catalysts.

SUBSTANCE: invention provides ammonia synthesis catalyst containing VII group and group VIB metal compound nitrides. Ammonia is produced from ammonia synthesis gas by bringing the latter into contact with proposed catalyst under conditions favoring formation of ammonia.

EFFECT: increased ammonia synthesis productivity.

8 cl, 2 tbl, 19 ex

FIELD: hydrocarbon manufacturing.

SUBSTANCE: natural gas is brought into reaction with vapor and oxygen-containing gas in at least one reforming zone to produce syngas mainly containing hydrogen and carbon monoxide and some amount of carbon dioxide. Said gas is fed in Fisher-Tropsh synthesis reactor to obtain crude synthesis stream containing low hydrocarbons, high hydrocarbons, water, and unconverted syngas. Then said crude synthesis stream is separated in drawing zone onto crude product stream containing as main component high hydrocarbons, water stream, and exhaust gas stream, comprising mainly remained components. Further at least part of exhaust gas stream is vapor reformed in separated vapor reforming apparatus, and reformed exhaust gas is charged into gas stream before its introducing in Fisher-Tropsh synthesis reactor.

EFFECT: increased hydrocarbon yield with slight releasing of carbon dioxide.

7 cl, 3 dwg, 1 tbl, 5 ex

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