Catalytic reactor and process

FIELD: chemical engineering.

SUBSTANCE: invention relates to chemical process and catalytic reactors suitable for carrying out the process. In particular, Fischer-Tropsch synthesis is described involving compact block of catalytic reactor (10) forming passages wherein gas-permeable catalyst structure (16) is present, said passages extending between manifolds (18). Synthesis is performed in at least two steps since reactor block provides at least two consecutive passages (14, 14a) for Fischer-Tropsch synthesis process interconnected through manifold wherein gas flow velocity in the first passages is high enough to limit conversion of carbon monoxide to 65%. Gases are cooled in manifold between two steps so as to condense water steam and then passes through the second passage at flow velocity high enough to limit conversion of the rest of carbon monoxide to 65%.

EFFECT: reduced partial pressure of water steam and suppressed oxidation of catalyst.

17 cl, 3 dwg

 

This invention relates to a chemical process and catalytic reactors suitable for use in the process.

In WO 01/51195 (Accentus plc) describes the way in which the methane reacts with steam, forming carbon monoxide and hydrogen in a first catalytic reactor; the resulting gas mixture is then used for performing Fischer-Tropsch synthesis in the second catalytic reactor. The overall result is the conversion of methane to hydrocarbons of higher molecular weight, which are usually liquid or solid at ambient conditions. Two stage process, the reforming steam/methane and Fischer-Tropsch synthesis, require different catalysts, and for each stage described catalytic reactors. Catalytic reactors allow heat to be transmitted to the reaction gases or from them, according to, is the reaction endothermic or exothermic; the heat required for reforming steam/methane, is provided by burning gas. Known catalyst for Fischer-Tropsch synthesis uses small particles of cobalt on the ceramic carrier, but it was found that this catalyst can undergo oxidation or irreversible reaction with the ceramic media in the presence of water vapor with a decrease in the result of this activity. Now found uluchsheniya implementation of this process.

According to the present invention, a method for implementation of the Fischer-Tropsch synthesis using the at least one compact unit catalytic reactor, forming channels for the reaction of the Fischer-Tropsch synthesis, in which there is permeable to gas, the structure of the catalyst, inside of which contains carbon monoxide gas is subjected to Fischer-Tropsch synthesis into at least two successive stages, and the velocity of gas flow in the first stage is high enough to ensure that no more than 70% of carbon monoxide were subjected to the synthesis reaction in the first stage, and the gases are cooled between successive stages so that condensed water vapor, and the flow rate gas in the second stage high enough to ensure that no more than 70% of the remaining carbon monoxide were subjected to the synthesis reaction in the second stage.

Preferably the first and in the second stage, the volumetric rate is above 1000 h-1but preferably not higher than 15000 h-1. Preferably the process is carried out so that the proportion of water vapor in the gas mixture in the reactor did not exceed 20 mol.%. Preferably at each stage of conversion being no more than 65% carbon monoxide.

The volumetric rate in this description, is defined as the volumetric flow rate of gases supplied to the reactor (measured at normalnyh temperature and pressure), divided by the free volume of the reactor. Thus, if the reactor is at 210°and a pressure of 2.5 MPa, a space velocity of 5000 h-1corresponds to the gas flow (under operating conditions) at about 354 free volume of the reactor per hour and, therefore, the residence time is about 10 seconds

Accordingly, the invention also provides a method for making the Fischer-Tropsch synthesis gas containing hydrogen and carbon monoxide, using at least one compact unit catalytic reactor, forming channels for the reaction of the Fischer-Tropsch synthesis, in which there is permeable to gas, the structure of the catalyst, in which the reaction is carried out in at least two successive stages at a sufficiently high velocity gas flow to the proportion of water vapor in the gas mixture in the reactor did not exceed 20 mol.% and that between successive stages of the gases are cooled to condense the water vapor.

The invention relates also to a device for carrying out such a Fischer-Tropsch synthesis. This can be a compact unit of a catalytic reactor containing collectors that connect the sequential flow channels, where the reservoir includes means for condensing water vapor and removing the condensed liquid from the collector. Catalytically the reactor unit preferably includes a number of metal plates, placed in a package and connected together so as to form channels for the Fischer-Tropsch synthesis, alternating with channels for the heat exchange medium. Preferably the temperature in the channels of the synthesis of the above 190°With, for example 200°C. Wavy or lunata foil, metal mesh or wavy or corrugated sheets of metal felt can be used as a substrate for catalyst structure within the channels in order to improve heat transfer and to increase the surface area of the catalyst.

Preferably, each successive stage is carried out in the respective multiple channels, and the total cross-sectional area of the second set of channels less than the total area of the multiple first channels.

It should be clear that the materials from which to fabricate the reactor are exposed to when using the corrosive environment. The reactor may be made of such metal as containing aluminum ferritic steel, for example, it may contain iron to 15% chromium, 4% aluminum and 0.3% yttrium (for example, FecralloyTM). When such a metal is heated in air, it forms adhering oxide coating of aluminum, which protects the alloy from further oxidation; this oxide layer also protects the alloy against corrosion. Is that where this metal is used in quality the ve of the catalyst substrate and the cover ceramic layer, which introduced the material of the catalyst layer of aluminum oxide on the metal associated with the oxide coating, thereby ensuring that the catalytic material is stuck to the metal substrate. Can be used also other stainless steel. Alternative plate separating the channels may be made of aluminum.

The invention will now be described additionally and more specifically, for example only and with reference to the accompanying drawings, on which:

figure 1 shows the cross-section of a reactor suitable for performing the Fischer-Tropsch synthesis, showing the plate in the plan;

figure 2 shows a modification of the reactor 1.

The invention relates to a Fischer-Tropsch synthesis, which may be part of the process of conversion of methane into hydrocarbons with a longer chain. The Fischer-Tropsch synthesis is a reaction between carbon monoxide and hydrogen, this gas mixture may, for example, be generated by the reforming water vapor/methane. When the Fischer-Tropsch synthesis gases react to form hydrocarbons with longer chains, that is,

nCO+2nH2→(CH2)n+nH2About

This reaction is exothermic, which takes place at elevated temperatures, typically between 190 and 350°With, for example, when 210°and high pressure, typically between 2 MPa and 4 MPa, for example at 2.5 MPa, in the presence of a catalyst, Taco is about as iron, cobalt or fused magnetite with the promoter. The exact nature of the organic compounds formed during the reaction depends on temperature, pressure and catalyst, and the ratio of carbon monoxide and hydrogen.

The preferred catalyst comprises a coating of gamma alumina with a specific surface area of 140-450 m2/g with about 10-40% by weight by weight aluminum oxide) cobalt and promoter ruthenium/platinum, and the promoter is between 0.01% to 10% by weight of cobalt. There may also be an alkaline promoter, such as gadolinium oxide. The activity and selectivity of the catalyst depends on the degree of dispersion of cobalt metal on the carrier, and the optimal level of dispersion of cobalt is usually in the range from 0.1 to 0.2, so that between 10 and 20 percent of the people of atoms of cobalt metal are on the surface. It is clear that the greater the degree of dispersion, the smaller should be the size of the crystallite of cobalt metal, and it is usually in the range of 5-10 nm. The cobalt particles of this size provide a high level of catalytic activity, but can be oxidized in the presence of water vapor, and this leads to a sudden and significant decrease in their catalytic activity. The degree of oxidation depends on the share of hydrogen and water in the vicinity of the catalyst particles, and the e on their temperature, moreover, a higher proportion of water vapor, and higher temperatures increase the depth of oxidation.

Referring now to figure 1, the reactor 10 for Fischer-Tropsch synthesis includes plate pack of 12 of Fecralloy steel, where each plate is generally rectangular with a length of 450 mm, a width of 150 mm and a thickness of 6 mm, and these dimensions are for example only. On the upper surface of each plate 12 has a rectangular grooves 14 a depth of 5 mm, separated by edges 15 (shown eight such grooves), but there are three different locations of the slots 14. In plate 12, shown in the drawing, the grooves 14 are diagonally at an angle of 45° to the longitudinal axis of the plate 12 from the top left to the bottom right, as shown. In the second type of plate 12 grooves 14a (indicated by dashed lines) follow the scheme mirroring, passing diagonally at an angle of 45° bottom from left up to right, as shown. In the third type of plate 12 grooves 14b (dotted lines) are parallel to the longitudinal axis.

The plate 12 is assembled in a package, where each of the plates 12 of the third type (with longitudinal grooves 14b) is located between plate with diagonal grooves 14 and plate mirrored diagonal grooves 14a, and after Assembly of many plates 12 package complete blank rectangular plate. The plate 12 is pressed together and the machining is to provide a heat treatment, to perform diffusion bonding, or spaivayut together so that they were bound to each other. Corrugated foil of alloy Fecralloy 16 (shown only one) with a thickness of 50 microns, coated with a ceramic coating, impregnated with a catalytic material, the appropriate form with the corrugations with a height of 5 mm, can be inserted in each diagonal groove 14 or 14a.

More preferably, a pair of corrugated coated catalyst sheets of foil 16 with a corrugation height of about 2.4 mm collected in the package and with the flat-coated catalyst sheets of foil between them and fasten together by spot welding before inserting them into the slots 14 or 14a.

The collector chamber 18 are welded to the package along each side, where each collector comprises three compartments with two ribs 20, which are also welded to the package. Ribs 20 are located at one-third the way along the length of the package on each side, and coincide with the edge 15 (or with a part of the plate without slots) in each plate 12 with diagonal grooves 14 or 14a. Collectors refrigerant 22 in the form of a rectangular caps welded on the package at each end and connected with longitudinal grooves 14b. In a modification (not shown) instead of each collector 18 with three compartments can be three adjacent collector chambers, each of which is a rectangular cap that is similar to the manifold 22. Within each of the main compartments of the reservoir 18 has cooling tubes 25, which extend the full height of the package. At the base of each of these Central compartments is output fitting (not shown), through which may enter the liquid condensing on the tube 25. To use the reactor 10 equipped with plates 12 in almost horizontal planes, so that the cooling pipes 25 are almost vertical.

When using the reactor 10 a mixture of carbon monoxide and hydrogen are served in both compartments of the reservoir 18 at one end (the left end as shown) of the package, and thus the gases formed during the Fischer-Tropsch synthesis, go through both compartments of the reservoir 18 to the right as shown. The flow path for the mixture supplied to the upper left compartment of the manifold (as shown), passes through, for example, diagonal grooves 14 in the lower middle compartment of the reservoir and then flows through the diagonal slots 14a in the other plates of package in top right compartment of the reservoir. The refrigerant is fed to the collector 22 at the same end of the package to maintain the temperature in the reactor 10 at a level of about 210°so that the refrigerant was at its lowest temperature in the area where the heat has its maximum during the first stage. Therefore, the reacting gas flows, and a refrigerant is Vlada, at least partially, in parallel. The goal is to achieve isothermal conditions throughout the reactor 10; this is the advantage of minimizing the risk of any blocking waxes (i.e. hydrocarbons with very long hydrocarbon chain) flow channels towards the exit reaction channels, if the local temperature drops below approximately 190°C. If is the deposition of paraffins, they can be removed by lifting the refrigerant temperature at between 5 and 15°and a feed rich in hydrogen tail gas through the reactor. Flow rate (space velocity) of the reaction gases is in the range of 1000-1500 h-1so, to be sure that the conversion of carbon monoxide was only about 60% or less for the time the gases reach the middle compartments of the reservoir 18.

The refrigerant tube 25 is supplied with refrigerant temperature so that they were colder, for example, at 150°With (which is below the boiling point of water at the pressure in the reactor). In the water vapor (and part of the hydrocarbons with longer chain) is condensed on the outer surface of the cooling tubes 25 and flows through these tubes 25 to exit through an outlet fitting (not shown) at the bottom of the package. This significantly reduces the partial pressure of water vapor in the gas mixture, which comes next, set the diagonal grooves 14 or 14a. The result is that the Fischer-Tropsch synthesis occurs in two successive stages, where in the first stage, the gas flows from the input compartments of the reservoir 18 in the middle compartments, and in the second stage, the gas flows from the middle compartments in the weekend compartments, and at least part of the water vapor formed in the first stage, remove from the gas stream before it enters the second stage.

It should be clear that the reactor 10 may be modified in various ways and that, in particular, the plate 12 can be of varying thickness. For example, plate 12, forming a diagonal grooves, or channels, 14 and 14a, in which the Fischer-Tropsch synthesis may be a thickness of 10 mm at the depth of the groove, or channel, 9 mm, while the plate 12 with longitudinal grooves or channels, 14b for the refrigerant can be of a thickness of only 4 mm, the depth of the groove, or channel, 3 mm. In this case, the corrugated foil 16 may be replaced by a package of, say, three or four sheets of corrugated foil, which can be fastened together by spot welding so that the total height was 9 mm. Such deeper grooves give the advantage, if there is some kind of waxy material, as they are less susceptible to clogging. Channels with a depth of more than about 2 mm improve bulk transport properties of corrugated catalytic vstavki; in the case of the Fischer-Tropsch synthesis this allows for effective drainage and removal of liquid products, and the reaction gas transport to the catalyst surface. Step or arrangement of corrugated sheets of foil 16 may vary along the reaction channel 14 or 14a to regulate the catalytic activity and, therefore, provide an opportunity to regulate the temperature or the reaction rate at different points of the reactor 10. In addition, the diagonal grooves may be reduced in width and possibly also in depth along their length so as to vary the flow conditions of the environment and the coefficients of heat or mass transfer.

During the synthesis reaction volume of gas decreases and by narrowing the channels 14, the velocity of the gas can be maintained as the reaction to maintain the target conversion. An alternative means of maintaining the gas velocity is to reduce the number of flow channels, as shown in figure 2, in which reference is made. Fig. 2 shows a view corresponding to that of figure 1. The only difference is that the diagonal channels 14 (and 14a), forming the second stage Fischer-Tropsch synthesis, in other words, the channels 14 (and 14a) between the middle compartment and a right compartment collectors 18 are separated by a wider edges 30 so that there were only three such Cana is in each plate 12.

It should be also clear that the modified reactor can provide more stages, for example, be a three-stage reactor Fischer-Tropsch process, where the reservoir 18 is formed by four successive compartment on each side of the reactor, condenser tubes 25 in each of the two middle compartments. The overall conversion can be almost the same, for example, two stages with a conversion of 60% and three stages with a conversion of 50% each to ensure total conversion above 80%.

Removal of water vapor and low-boiling hydrocarbons in the tubes of the condenser 25 not only reduces the partial pressure of water vapor and thus suppresses the oxidation of the catalyst, but also gives the added benefit of removing at least part of those hydrocarbons, which may form a layer of fluid on the structure of the catalyst. Any such liquid layer inhibits the contact of the gas mixture with the catalyst particles and slows down the diffusion of the produced hydrocarbons from the catalyst particles, so that the removal of hydrocarbon fluid minimizes such diffusion resistance.

Figure 1 and 2 shows only four tubes of the condenser 25 in each compartment, but it should be clear that there can be a different number of tubes, for example ten or more. To improve the heat transfer of each tube 25 may be provided with ribs, which are preferably located the military longitudinally to the flow of the condensed liquid in the tube 25 is not difficult. On the tubes not only condenses the water vapor, but also any liquid droplets carried by the gas stream tend to collide with the surface of the tubes 25 and thus removed from the gas stream. Alternatively, the tubes of the heat exchanger 25 or other heat exchange surfaces may be prompted spray condenser system in the middle compartments of the reservoir 18, which can be used as a coolant recirculating the products of the Fischer-Tropsch synthesis at about 150°C. This can be particularly beneficial if there is a risk of paraffin deposits which contaminate the surface of the heat exchange.

Alternatively, the cooling and condensation may be carried out separately and outside of the reactor. For example, three reactor 10A, similar to the one shown in figure 1, but without cooling tube 25 within the manifold can be configured to pass gas flows in parallel, and the conversion FROM kept below 65% of the control reaction temperature and flow rate (figure 3). Emerging from the three reactors 10A gases are connected through a manifold condenser installation 35 (same as 25), in which condensed water vapor and liquid hydrocarbon product. The remaining gases with reduced partial pressure of water can be is then filed in the same individual reactor 10A (again not containing the inside of the cooling tubes 35), again, about 60% of residual unreacted suffered FROM the synthesis reaction. The decrease of the gas between the first stage and the second stage due to the fact that most of the gas was subjected to synthesis and formed a fluid, consistent with the decrease in the number of reactor units from three to one to maintain a high flow velocity.

Additional advantages of high speed gas flow is to reduce the temperature variations along the length of the reactor channels by promoting the redistribution of heat exothermic reactions on the catalyst surface into the gas phase. It also promotes the entrainment of liquid reaction products in the gas stream and to maintain the catalyst surface, free from paraffin deposits.

1. Method for making Fischer-Tropsch synthesis using the at least one compact unit catalytic reactor (10), forming channels (14, 14a) for the reaction of the Fischer-Tropsch synthesis, in which there is permeable to gas, the structure of the catalyst (16), characterized in that it contains carbon monoxide gas is subjected to Fischer-Tropsch synthesis into at least two successive stages, and the velocity of gas flow in the first stage is high enough to ensure that no more than 70% of carbon monoxide were subjected to the synthesis reaction in the first stage, and between the using serial stages gases are cooled in the capacitor system (25) or inside the reservoir (18) of the reactor (10), or separately outside of the reactor to condense water vapor, and the velocity of gas flow in the second stage high enough to ensure that no more than 70% of the remaining carbon monoxide were subjected to the synthesis reaction in the second stage.

2. The method according to claim 1, carried out with the use of a single reactor unit (10), in which each stage of the synthesis reaction occurs in multiple channels (14, 14a) inside the reactor building and the gases are cooled in condenser system (25) in the reservoir (18) between consecutive stages.

3. The method according to claim 1, wherein the stream containing carbon monoxide gas flows through many parallel first channels (14, 14a) of the first stage and then through the set of second parallel channels (14, 14a) of the second stage, and the cross-sectional area of the second set of channels (14, 14a) is less than that for many the first channels (14, 14a).

4. The method according to claim 2, in which the stream containing carbon monoxide gas flows through many parallel first channels (14, 14a) of the first stage and then through the set of second parallel channels (14, 14a) of the second stage, the total cross-sectional area of the second set of channels (14, 14a) is less than that for many the first channels (14, 14a).

5. The method according to claim 3, in which the number of second channels (14, 14a) is less than the first number of channels (14, 14a).

6. The method according to claim 4, in cat the rum the number of second channels (14, 14a) is less than the first number of channels (14, 14a).

7. The method according to any of the preceding paragraphs, in which the first and at the second stage, the volumetric rate is above 1000 h-1.

8. The method according to claim 7, in which the first and in the second stage, the volumetric rate is not above 15000 h-1.

9. The method according to any of the preceding claims 1 to 6, in which water vapor does not exceed 20 mol.%.

10. The method according to any one of claims 1 to 6, in which the rate of gas flow through the first and through the second stage high enough to ensure that no more than 65% of the carbon monoxide was subjected to the synthesis reaction.

11. Method for making Fischer-Tropsch synthesis gas containing hydrogen and carbon monoxide, using at least one compact unit catalytic reactor (10), forming channels (14, 14a) for Fischer-Tropsch synthesis, in which there is permeable to gas, the structure of the catalyst (16), where the synthesis is carried out in at least two successive stages at a sufficiently high rate of flow of gas to water vapor does not exceed 20 mol.%, and that between successive stages of the gases were cooled in a condenser system (25) or inside the reservoir (18) of the reactor (10), or separately outside of the reactor to condense water vapor.

12. The device for performing the Fischer-Tropsch synthesis according to any one of the preceding is unstow, including at least one compact unit catalytic reactor (10), forming channels (14, 14a) for the reaction of the Fischer-Tropsch synthesis, in which are permeable to gas, the structure of the catalyst (16), connecting means (18), providing a link between successive sets of channels (14, 14a), and a cooling condenser system (25) inside connecting means for condensing water vapor and remove the condensed liquid from the gas stream.

13. The device according to item 12, in which successive sets of channels (14, 14a) are in the same reactor unit (10) and connecting means (18) is the header.

14. The device according to item 12, in which the cross-sectional area of flow channels (14, 14a), the transport stream of the connecting means (18), is less than the cross-sectional area of flow channels (14, 14a), the transport flow in the connecting means (18).

15. The device according to item 13, in which the cross-sectional area of flow channels (14, 14a), the transport stream of the connecting means (18), is less than the total cross-sectional area of flow channels (14, 14a), the transport flow in the connecting means (18).

16. Device according to any one of p-15, in which the number of flow channels (14, 14a), the transport stream of the connecting means (18), less than the number of flow channels (14, 14a), the protractor is affected flow in the connecting means (18).

17. The device according to item 12, also comprising means (14b) to ensure that the temperature in the channels of the synthesis (14, 14a) does not exceed 210°C.



 

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1 cl, 15 tbl

FIELD: disproportionation reaction catalysts.

SUBSTANCE: invention relates to Fischer-Tropsch catalyst containing cobalt and zinc, to a method for preparation thereof, and to Fischer-Tropsch process. Catalyst according to invention containing co-precipitated cobalt and zinc particles, which are characterized by volume-average size below 150 μm and particle size distribution wherein at least 90% of the catalyst particle volume is occupied by particles having size between 0.4 and 2.5 times that of the average particle size and wherein zinc/cobalt atomic ratio within a range of 40 to 0.1. Catalyst is prepared by introducing acid solution containing zinc and cobalt ions at summary concentration 0.1 to 5 mole/L and alkali solution to reactor containing aqueous medium wherein acid solution and alkali solution come into contact with each other in aqueous medium at pH 4-9 (deviating by at most 0.2 pH units) at stirring with a speed determined by supplied power between 1 and 300 kW/L aqueous medium and temperature from 15 to 75°C. Resulting cobalt and zinc-including precipitate separated from aqueous medium, dried, and further treated to produce desired catalyst. Employment of catalyst in Fischer-Tropsch process is likewise described.

EFFECT: enhanced strength and separation properties suitable for Fischer-Tropsch process.

13 cl, 2 dwg, 1 tbl, 5 ex

FIELD: production of pigments and catalysts based on titanium dioxide, in particular, process for treatment of titanium dioxide for removal of sulfur, in particular sulfates.

SUBSTANCE: method involves treating calcined titanium dioxide at elevated temperatures using aqueous solution containing one or more ammonium compounds; separating titanium dioxide from aqueous solution and drying titanium dioxide. Ammonium compounds preferably used in treatment process are ammonium acetate or ammonium chloride.

EFFECT: increased efficiency in cleaning of titanium dioxide from sulfur, in particular sulfates.

9 cl, 5 tbl, 5 ex

FIELD: petrochemical process catalyst.

SUBSTANCE: invention relates to a method of preparing catalyst for use in Fischer-Tropsch process and to catalyst obtained according present invention. Preparation of catalyst suitable for conversion at least one synthesis gas component comprises: providing aqueous solution of organic acid; adding iron metal to acid solution; passing oxidant through the solution until iron metal is consumed and iron-containing slurry formed; grinding resulting slurry to achieve average particle size less than about 2 μm; adding at least one promoter to ground iron-containing slurry to form product suspension, concentration of said promoter being such as to obtain said product suspension containing solid phase constituting from about 10 to about 40% of the weight of suspension, including said promoter; performing spray drying of suspension to obtain particles; and calcining these particles to obtain desired catalyst.

EFFECT: optimized catalyst preparation procedure.

23 cl, 2 dwg, 1 tbl, 12 ex

FIELD: alternate fuel production.

SUBSTANCE: invention relates to synthesis of hydrocarbons from CO and H2, in particular to catalysts and methods for preparation thereof in order to carrying out synthesis of hydrocarbons C5 and higher according to Fischer-Tropsch reaction. Method resides in that non-calcined zeolite ZSM-12 in tetraethylammonium-sodium form is subjected to decationation at pH 5-9, after which decationized zeolite (30-70 wt %) is mixed with alumina binder while simultaneously adding cobalt (7.5-11.5 wt %) as active component and modifier, in particular boron oxide (3-5 wt %). Proposed method allows catalyst preparation time to be significantly reduced owing to combining support preparation and deposition of active component and modifier in one stage with required catalytic characteristics preserved. In addition, method is environmentally safe because of lack of waste waters, which are commonly present when active components are deposited using impregnation, coprecipitation, and ion exchange techniques.

EFFECT: reduced catalyst preparation time and improved environmental condition.

1 tbl, 10 ex

FIELD: petrochemical processes.

SUBSTANCE: synthesis gas is subjected to conversion to produce liquid hydrocarbons in sequentially connected reactors containing catalytic slurry of at least one solid catalyst in a liquid phase. Reactors are triphase bubble column-type reactors provided with virtually full stirring characterized by liquid Peclet number below 8, gas Peclet number below 0.2, and diameter larger than 6 m. Last reactor at least partially receives at least part of at least one of the gas fractions collected at the outlet of at least one of other reactors. At least one reactor is supplied with stream of catalytic slurry coming directly out of another reactor, and at least one stream of catalytic slurry coming out of reactor is at least partially separated so as to receive liquid product substantially free of catalyst and catalyst-rich catalytic slurry, which is then recycled.

EFFECT: improved process technology.

10 cl, 8 dwg, 7 ex

FIELD: organic synthesis catalysts.

SUBSTANCE: invention provides fischer-tropsch process catalyst comprising at least one metal suitably absorbing carbon monoxide and at least one promoter, said metal and said promoter being dispersed on a substrate to form catalytic particle having BET surface area between 100 and 250 m2/g so that size of metal oxide crystallites ranges from 40 to 200 while said metal and said promoter are different compound and said particle has predominantly smooth and uniform morphology of surface. substrate is characterized by particle size between 60 and 150 μm, surface area 90 to 210 m2/g, pore volume 0.35 to 0.50 mL/g, and pore diameter 8 to 20 nm. Described are also catalyst and a method of preparing catalyst including cobalt dispersed onto substrate to form catalyst particle.

EFFECT: increased surface of catalyst, improved uniformity in distribution of metal, and reduced size of metal crystallites.

33 cl, 9 dwg, 1 tbl, 10 ex

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to a method for synthesis of alcohol comprising synthesis of olefins by the Fischer-Tropsch process followed by the hydroformylation reaction and isolation of mixture of alcohols. Hydrocarbon fraction with the content of linear olefins 10-45 wt-% is separated from products reaction synthesized by the Fischer-Tropsch process with using cobalt catalyst by distillation followed by its hydroformylation with carbon monoxide and hydrogen taken in the molar ratio hydrogen to carbon monoxide = 1.0-5.0. The reaction of synthesis is carried out in the presence of cobalt-base catalyst and a substituted or unsubstituted monophosphocycloalkane ligand followed by steps of hydrogenation and distillation. Invention provides preparing a composition with the content of linear (C7-C12)-alcohols 60 wt.-%, not less, high rate of reaction and high selectivity of the process.

EFFECT: improved method of synthesis.

8 cl, 3 tbl, 4 ex

FIELD: method for separating at least a fraction of non-acidic chemical products from at least a fraction of raw gaseous product received in Fischer-Tropsch reaction, or from condensate of said product.

SUBSTANCE: in accordance to method at least a fraction of raw gaseous product or its condensate is fed into feeding plate of distillation column, liquid flow is drained from aforementioned column from plate, positioned above feeding plate of the column. Received liquid flow is divided on water phase and saturated non-acidic chemical product phase and water phase is returned to distillation column onto plate positioned below plate from which liquid flow is drained.

EFFECT: increased efficiency of cleaning method.

23 cl, 1 dwg

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

FIELD: chemical industry; petrochemical industry; methods of production of the catalysts and hydrocarbons with their use.

SUBSTANCE: the invention is pertaining to the method of production of the catalyst for production of hydrocarbons and to the method for production of hydrocarbons at the presence of the catalyst on the basis of the metal of VIII group on the carrier - the refractory oxide. The presented method of production of the catalyst for production of hydrocarbons on the basis of the metal of VIII group on the carrier - the refractory oxide provides for mixing of the refractory oxide with the surface area of no less than 0.5 m2 /g with the solution of the precursor of this refractory oxide and with the metal or with the precursor of this metal till production of the suspension, drying of the suspension and its calcination. The invention also presents the method of production of the hydrocarbons providing for contacting of the mixture of the hydrocarbon monoxide with hydrogen at the heightened temperature and pressure at presence of the catalyst produced by the method described above. The technical result is production of the catalyst with higher activity in the synthesis of the hydrocarbons at conservation of high selectivity.

EFFECT: the invention ensures production of the catalyst with the higher activity in the synthesis of the hydrocarbons at conservation of the high selectivity.

8 cl, 1 tbl, 1 ex

FIELD: gas treatment.

SUBSTANCE: invention relates to improved method for removing acetylene compounds from hydrocarbon streams, which method comprises bringing hydrocarbon stream containing a first concentration of acetylene compounds and olefins with catalyst being consisted either of supported non-sulfided metallic nickel or the same modified with metals such as Mo, Re, Bi, or mixture thereof, said non-sulfided nickel being present on support in quantity by at least 5% superior to quantity required for selective hydrogenation of acetylenics. Hydrogenation is carried out in first reaction zone at temperature and pressure as well as hydrogen concentration favoring hydrogenation of acetylenics, after which hydrocarbon material is discharged containing second concentration of acetylenics inferior to its first concentration.

EFFECT: improved acetylenics removal selectivity and increased yield of target olefin compounds.

20 cl, 10 dwg, 1 tbl, 6 ex

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