Technological scheme of new reactor of dehydrogenation of propane to propylene

FIELD: chemistry.

SUBSTANCE: invention relates to a method of propane dehydrogenation, which includes passing of a preliminarily heated initial propane flow into a dehydrogenation reactor, mixing and interaction of the initial propane flow with a non-metallic fluidised catalyst, which contains zirconium oxide, in the dehydrogenation reactor, which represents a reactor of fast fluidisation with formation of a flow of a propylene-containing product. The catalyst is in the reactor with the average time of presence from 15 to 45 minutes; passing of a waste catalyst into a catalyst regeneration unit with formation of a flow of a regenerated catalyst; and passing the flow of the regenerated catalyst into the dehydrogenation reactor.

EFFECT: application of the claimed method makes it possible to increase the passing capability of the system.

8 cl, 1 dwg

 

This patent application claims the priority based on patent application U.S. No. 12/728,543, which was filed on March 22, 2010.

The technical field to which the invention relates.

The present invention relates to the production of light olefins from paraffins. Particularly the present invention relates to the dehydrogenation of propane in obtaining propylene.

The level of technology

In the petrochemical industry develop a catalyst for continuous conversion. The cracking of hydrocarbons in a fluidized bed with a catalyst is an important method of obtaining light hydrocarbons, ethylene and propylene. In the method of fluidized catalytic cracking constantly fluidized catalyst is continuously circulated between the reactor and regenerator.

Another option for obtaining propylene can be carried out by propane dehydrogenation by catalytic dehydrogenation. The dehydrogenation catalysts contain mostly catalysts of noble metals on acidic substrates, such as alumina, aluminosilicate or zeolite materials. However, this reaction is strongly endothermic, and is at a sufficient speed requires a high temperature. At the same time, these reactions must be controlled to limit the decomposition of propane education is ETANA and ethylene, and ethylene can be gidrirovanii hydrogen released by dehydrogenation of propane. This method also leads to zakochani catalyst and deactivates it. Therefore, the catalyst must constantly regenerate after relatively short periods of operation, or stay in the dehydrogenation reactor.

The invention

The present invention relates to a method for dehydrogenation of paraffins. In particular, the invention relates to a method for the dehydrogenation of propane to obtain propylene. The method includes passing the pre-heated source of a stream of propane in the dehydrogenation reactor. The reactor to operate under conditions of mixing and contact of propane with a fluidized bed of a catalyst for the formation of a product stream containing propylene. In the reactor provide a constant supply and removal of the catalyst from the dehydrogenation reactor at a speed that provides the residence time of the catalyst in the reactor from 15 to 45 minutes. This reactor is a reactor fast fluidization to ensure the entire reactor is well mixed reagents and flow of the initial reagents, as well as a uniform temperature. The stream flowing from the reactor is separated into a stream of spent catalyst and a product stream containing propylene. Otra is otany the catalyst is sent to the regeneration unit of catalyst, thereby forming a stream of regenerated catalyst. The catalyst is treated in the regeneration unit when the restriction condition of the average residence time in the regeneration unit to 30 minutes or less. The regenerated catalyst is sent to the dehydrogenation reactor.

High cyclic rate of passage of the catalyst through the reactor and the regenerator provides for an increase of the total flow using the reagents and performance of the dehydrogenation reactor.

Additional tasks, ways of implementation and details of the present invention can be obtained of the following drawings and detailed description of the present invention.

Brief description of drawings

The figure presents a diagram of the process of dehydrogenation of hydrocarbons using the fast reactor fluidization.

The implementation of the invention

Dehydrogenation of hydrocarbons is an important process for olefin production. Olefins are required for different products, such as polymer plastics, or the olefins used in the formation of compounds of alkylaryl. The method relates to the dehydrogenation of propane. This method involves passing a preheated original flow of propane to the dehydrogenation reactor. The flow of the source reagent is put into communication with a fluidized bed of catalyst in the reactor de is gidrirovaniya, thereby forming a product stream containing propylene. This reactor is a fast fluidization, and the reactor is controlled in the flow regime to the turbulent mixing of catalyst and the flow of the source reagent. The flow of catalyst and the product passes through the reactor, and its share in the partition of separation, resulting in a product stream containing propylene, is removed from the reactor. The spent catalyst is sent to the regeneration unit catalyst for regeneration of the catalyst and return it to the dehydrogenation reactor.

The operation of the fast reactor fluidization control under conditions of back mixing of the catalyst and reagents. Mixing constrains the temperature to maintain a more uniform during the reaction, whereas the limit local temperature decreases, which adversely affects the reaction rate. Conditions for the reaction include the operation of the reactor at a temperature of from 600°C to 700°C. Mixing is needed to create a more uniform temperature, and preferably enough to mix the catalyst and the source reagent for operation at a temperature of 630°C. to 650°C.

Reaction conditions include a pressure at the outlet of the reactor in the range from 108 kPa to 170 kPa (1 to 10 lbs/inch2). Preferred conditions controls the outlet pressure of the reactor in the range is the area from 122 to 136 kPa kPa (3 to 5 lb/inch). This reaction takes place in an atmosphere containing hydrogen, in addition to the formed hydrogen. The reactor includes a molar ratio of hydrogen to hydrocarbons at the inlet to the reactor in the range from 0.2 to 1, with the preferred molar ratio of hydrogen to hydrocarbon of 0.6. Stream source of hydrogen and hydrocarbon is preheated to ensure a certain amount of heat required for the endothermic reaction. The hydrogen formed in the course of the method of dehydrogenation, remove and reuse in the original thread. Hydrogen is used again to maintain the level of hydrogen in all zones of the reactor.

The method uses a relatively short residence time for the catalyst, and also the rapid recovery of the catalyst. This method allows the average residence time of catalyst in the reactor from 15 to 45 minutes, with a preferred average residence time of from 15 to 30 minutes. The short cycle allows you to maintain a more uniform temperature in the cross section of the reactor to achieve the best conversion and selectivity. New catalysts used in the present method include non-metallic catalysts. The term non-metallic catalysts relates to catalysts that do not contain the metal in its ground state, but implies the catalysts containing the oxides of the metals, such as zirconium and chromium.

To some extent the flow of the catalyst during the regeneration process limit the average residence time of less than 30 minutes. The regeneration unit is preferably Elevator-reactor, which allows you to mix the catalyst during the regeneration process. The regeneration process is usually carried out under conditions of burning part of the carbon that has accumulated on the catalyst. Additional fuel is sent to a regeneration unit for combustion and heating of the catalyst. Burning zajigaet carbon that has accumulated on the catalyst during the dehydrogenation process.

This method is presented in the figure. Thread 10 of the original hydrocarbon flow with a stream of hydrogen for 12 joint supply heat exchanger 20, thus forming a pre-heated mixed stream 22 of the original product. Mixed flow 22 of the original product is additionally heated in the heater 30 to the state of the thread 32 of the original product heated to the temperature at the inlet to the reactor 40. This thread 32 of the original product passes through the reactor 40 and forms a stream 42 product containing dehydrogenated hydrocarbons. Thread 42 product is used for pre-heating of hydrogen 12 and the thread 10 of the original hydrocarbon. In the present invention the preferred source reagent is propane, which money is dirout to the formation of the thread 42 of propylene. The catalyst in the reactor flows upward through the reactor 40, and the reactor 40 is controlled to ensure that the average residence time of the catalyst from 15 to 45 minutes. The catalyst produced from the reactor 44 in the regenerator 50. Fuel 46 is added to the regenerator 50 to provide energy for the combustion of carbon on the catalyst and to heat the catalyst. The 48 air is compressed and heated before mixing with the fuel 46, and then through the regenerator 50. The regenerator 50 runs for re-heating of the catalyst and passing the catalyst through the regenerator 50 with the average residence time of less than 30 minutes. Hot regenerated catalyst 52 is passed into the reactor 40 dehydrogenation.

The catalyst circulates through the loop at high speed between the reactor 40 and the regenerator 50. High speed cyclization catalyst provides the heated catalyst to maintain the endothermic reaction. With the rapid cyclization produces low levels of coke on the catalyst and coke quickly and easily removed during the recovery stage. Additionally, excess heat, leaving the regenerator in the flue gas can be returned to the stream 60 recovery.

Estimated real technological scheme will increase the receipt of propylene with higher bandwidth. The current receiving item is cut in the reactor system is limited to a value of about 500 hundred metric tons per year (CMTA). In the new technological scheme suggest an increase in flow rate of about 1,000 CMTA. I think that for such systems the catalyst circulates with a speed in the range of 10 to 12 million kg/hour.

Although the present invention is described in preferred embodiments, one should understand that it is not limited to the disclosed variants, but covers various modifications and equivalent implementation is included in the scope of the attached claims.

1. The method of dehydrogenation of propane, including:
passing the preheated original thread propane dehydrogenation reactor;
the mixing and interaction of the original stream of propane with a fluidized bed of non-metallic catalyst containing zirconium oxide, in the dehydrogenation reactor, which is a fast reactor fluidization with the formation of the product stream containing propylene and the catalyst is in the reactor with an average residence time of from 15 to 45 minutes;
passing spent catalyst in the regeneration unit of the catalyst with a stream of regenerated catalyst; and
the transmission of a stream of regenerated catalyst in the dehydrogenation reactor.

2. The method according to claim 1, in which reactor the fast fluidization control under conditions of reverse Pach the project catalyst and reagents.

3. The method according to claim 1, wherein the reaction conditions include a temperature from 600°C to 700°C.

4. The method according to claim 1, wherein the reaction conditions include a pressure at the outlet of the reactor in the range from 108 kPa to 170 kPa.

5. The method according to claim 1, in which the molar ratio of hydrogen to hydrocarbon in the feed is from 0.2 to 1.

6. The method according to claim 1, wherein the regeneration unit is an Elevator-reactor and the catalyst is passed through the regenerator with an average residence time of less than 30 minutes.

7. The method according to claim 1, which further comprises passing the fuel in the regeneration unit for combustion and heating of the catalyst.

8. The method according to claim 1, which further comprises passing the product stream in the heat exchanger combined raw materials for pre-heating of the source streams of propane and hydrogen.



 

Same patents:

FIELD: chemistry.

SUBSTANCE: present invention relates to a mesoporous carbon-supported copper-based catalyst, a method for production and use thereof in catalytic dehydrogenation of a compound with a C2-C12 alkyl chain to convert said compound to a compound with a corresponding alkenyl chain. The catalyst contains mesoporous carbon, a copper component and an auxiliary element supported on said mesoporous carbon. One or more auxiliary elements (in form of oxides) are selected from a group consisting of V2O5, Li2O, MgO, CaO, Ga2O3, ZnO, Al2O3, CeO2, La2O3, SnO2 and K2O. The amount of the copper component (calculated as CuO) is 2-20 wt % based on the total weight of the catalyst. The amount of the auxiliary element (calculated as said oxide) is 0-3 wt %. The amount of the mesoporous carbon is 77.1-98 wt % based on the total weight of the catalyst. The method of producing the catalyst involves: (1) a step of contacting a copper component precursor, auxiliary element precursor and mesoporous carbon in a given ratio to form an intermediate product and (2) a step of calcining the intermediate product to obtain the mesoporous carbon-supported copper-based catalyst.

EFFECT: catalyst is cheap, environmentally safe and has high thermal stability and caking resistance with considerably high and relatively stable catalytic activity.

19 cl, 47 ex

FIELD: chemistry.

SUBSTANCE: described is a method of producing C3-C5 olefin hydrocarbons via dehydrogenation of corresponding C3-C5 paraffin hydrocarbons or mixtures thereof in the presence of a catalyst which contains chromium oxide, zinc oxide, aluminium oxide and additionally a aluminium-magnesium spinel and at least tin oxide in amount of 0.1-3.0 wt %. Before the regeneration step, reaction products are removed from the catalyst by first passing C1-C5 hydrocarbons or mixtures thereof and then nitrogen through the catalyst. The catalyst contains chromium oxide, zinc oxide, aluminium oxide, aluminium-magnesium spinel and tin oxide, with the following ratio of components in terms of oxides, wt %: Cr2O3 - 10.0-30.0, ZnO - 10.0-40.0, SnO2 - 0.1-3.0, MgO - 1.0-25.0, Al2O3 - the balance. The catalyst can further contain a manganese compound in amount of 0.05-5.0 wt %.

EFFECT: high efficiency of the process of producing olefin hydrocarbons.

3 cl, 1 tbl, 11 ex

FIELD: chemistry.

SUBSTANCE: method is characterised by contacting a gas stream containing at least one of said hydrocarbons with a dehydrogenation catalyst containing gallium and platinum and deposited on a support made of aluminium oxide or aluminium oxide and silicon dioxide, at reaction temperature in a direct-flow, upward stream with weight ratio of catalyst to hydrocarbon of 5 to 100 in a dehydrogenation reactor, wherein the average contact time of the hydrocarbon with the catalyst in the zone of the dehydrogenation reactor ranges from 1 s to 4 s, and temperature and pressure in the dehydrogenation reactor range from 570 to 750°C and from 41.4 (6.0) to 308 (44.7) kPa (psia); and moving the hydrocarbon and the catalyst from the dehydrogenation reactor into a separation device, wherein the average contact time of the hydrocarbon with the catalyst at reaction temperature in the separation device is less than 5 s, and the full average contact time between the hydrocarbon, catalyst and the formed hydrocarbons is less than 10 s; and moving the catalyst from the separation device into a regenerator, where the catalyst is brought into contact with an oxygen-containing regenerating stream and additional fuel.

EFFECT: method has short contact time between the hydrocarbon and the catalyst.

7 cl, 5 dwg

FIELD: chemistry.

SUBSTANCE: disclosed is a method of determining resistance of an alkyl aromatic hydrocarbon dehydrogenation catalyst to catalyst poisons, said catalyst containing an alkali metal, the method involving treating the catalyst with a mixture which contains an alkyl aromatic hydrocarbon and 1-10% aqueous hydrochloric acid solution in ratio of 1:2…1:3, at temperature of 550-650°C, holding the sample for 3 hours; in order to dehydrogenate the alkyl aromatic hydrocarbons, the dealkylisation degree is determined using the formula: α=n(Me+)inn(Me+)recn(Me+)in, where α is the dealkylisation degree; n(Me+) is the amount of the alkaline promoter, mol. The method enables to predict loss of an alkaline promoter when using the catalyst at a formulation adjustment step without conducting long-term tests.

EFFECT: method for rapid determination of resistance of an alkyl aromatic hydrocarbon dehydrogenation catalyst, which contains an alkali metal, to catalytic poisons.

1 tbl, 5 ex

FIELD: chemistry.

SUBSTANCE: initial hydrocarbon raw material is initially separated and first part of initial raw material is introduced into first zone of dehydration reaction, which functions without oxidation re-heating, and obtained as a result output flow is introduced into second zone of dehydration reaction, which functions without oxidation re-heating. Obtained as a result output flow from second zone of dehydration reaction, together with second part of initial raw material is introduced into third zone of dehydration reaction, which functions with oxidation re-heating.

EFFECT: increased method productivity.

10 cl, 1 dwg

FIELD: chemistry.

SUBSTANCE: present invention relates to a catalyst and a method for continuous oxidative dehydrogenation of paraffins to corresponding olefins, specifically ethane to ethylene. Described is a catalyst for continuous oxidative dehydrogenation of ethane to ethylene, which contains a mixed oxide catalyst phase which contains ions of metals such as vanadium, molybdenum, niobium, tellurium or antimony, deposited on a support in form of an inert gas-permeable porous ceramic membrane with a deposited mixed oxide catalyst phase on the outer side of the membrane surface. Described also is a method for continuous oxidative dehydrogenation of ethane to ethylene in the presence of the disclosed catalyst by feeding an ethane-containing gas onto the outer side of the membrane surface coated with catalyst, and an oxygen-containing gas is fed onto the inner side of the membrane surface which is not coated with catalyst at temperature of 300°C-550°C, pressure ranging from atmospheric pressure to 10 MPa and volume rate of feeding material of 500-2000 h-1.

EFFECT: increase in ethylene selectivity to 98% and output of the process from 800 to 1400-2240 g/h per kg catalyst, high process safety since it enables to separate the hydrocarbon stream from the stream of oxygen-containing gas, thereby minimising the probability of their mixing, thus preventing formation of explosive mixtures.

4 cl, 1 tbl, 8 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of controlling activity of a catalyst for dehydrogenation of higher n-paraffins. The method involves controlling catalyst activity by increasing the rate of feeding water into a reactor and is characterised by that, the flow rate of water is further adjusted depending on the type of catalyst, wherein the ratio of the equilibrium constant when varying the process temperature to the equilibrium constant at the initial temperature must equal to one: Ki+1Ki=(nCO(i+1)*nCO(1)*)63(n1H2O+nCO(1)*nH2O(i+1)+nCO(i+1)*)28(n1H2O+nH2(1)*nH2O(i+1)+nH2(i+1)*)28=1, where Ki+1, K1 denote the equilibrium constant at Ti+1 and T1, Pa21; nH2O(i+1),n1H2O is the initial amount of H2O at Ti+1 and T1, mole; n*CO(i+1), n*CO(1) is the equilibrium amount of CO at Ti+1 and T1, mole; nH2(i+1)*,nH2(1)* is the equilibrium amount of H2 at Ti+1 and T1, mole.

EFFECT: high efficiency of the process.

2 cl, 1 tbl, 3 ex, 2 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a material which is suitable as a support for an alkane dehydrogenation catalyst, a method of producing said material and a method for catalytic dehydrogenation of alkane-containing gas mixtures. Described is a material for catalytic dehydrogenation of gas mixtures which contain C2-C6 alkanes and may contain hydrogen, water vapour, oxygen or any mixture of said gases, wherein primarily alkenes and hydrogen, and additionally water vapour, can be obtained, which: a) consists of ceramic foam obtained from oxide or non-oxide ceramic materials or a mixture of oxide and non-oxide ceramic materials, b) wherein the oxide ceramic materials used are calcium aluminate, silicon dioxide, tin dioxide or zinc aluminate or a mixture of said substances, c) to provide catalytic activity, the material is saturated with at least one catalytically active substance and d) the catalytically active material contains platinum, tin or chromium or mixtures thereof. Described is a method of producing said material by applying a starting ceramic substance, mixed during production with a suitable additive as an auxiliary agent, in form of a suspension onto a prepared starting polyurethane material, after which the obtained material is sintered and saturated with catalytically active material. Described is a method of dehydrogenating alkane-containing gas mixtures (versions) using the disclosed material.

EFFECT: considerable reduction in hydraulic resistance of the catalyst, significant improvement in availability of catalytically active material, increase in thermal and mechanical stability of the material.

14 cl

FIELD: chemistry.

SUBSTANCE: invention relates to a method of dehydrogenating alkanes, according to which a mixture containing hydrocarbons, particularly alkanes, which can contain water vapour, is continuously fed through a catalyst bed at ordinary dehydrogenation conditions. The many-hours-long dehydrogenation step is followed by a step with bleeding of oxygen-free gas through a reactor layer in order to blow and remove reaction gas from the reactor layer, and this is followed by a step for bleeding oxygen-containing regeneration gas in order to remove deposits on the catalyst formed during the dehydrogenation reaction. This is followed by a step for bleeding oxygen-free gas in order to blow and remove regeneration gas from the reactor. Duration of bleeding oxygen-containing gas during catalyst regeneration is equal to or less than 70% of the total duration of regeneration, total regeneration time is equal to 1 hour and regeneration starts after a seven-hour step of obtaining the product. The method is characterised by that regeneration starts with a five-minute blowing step, followed by a step for regeneration with a gas which contains oxygen and water vapour for 20 minutes, followed by an additional blowing step.

EFFECT: method enables to preserve catalyst activity and selectivity with respect to the desired process and after many regeneration cycles.

12 cl, 5 ex, 4 tbl

FIELD: chemistry.

SUBSTANCE: invention relates to dehydrogenation catalysts. Described is a dehydrogenation catalyst for dehydrogenating gaseous hydrocarbons, which contains platinum, one or more auxiliary metals selected from a group consisting of tin, germanium, gallium, indium, zinc and manganese, an alkali metal or an alkali-earth metal and a halogen component, which are deposited on a support consisting of aluminium oxide having theta-crystallinity of 90% or higher, said support having 5-100 nm mesopores and 0.1-20 mcm macropores, and platinum density per unit surface area of the catalyst is equal to 0.001-0.009 wt %/m2.

EFFECT: high catalyst activity.

8 cl, 3 tbl, 3 dwg, 3 ex

FIELD: chemistry.

SUBSTANCE: pyrolysis of methylene chloride is carried out on a catalyst with a carbonisation degree in the range of 2.6-5.2 wt %, which is obtained during 60-150 minutes of a reactor work, after which in order to support the obtained degree of carbonisation a catalyst is constantly discharged into a regenerator, excessive carbon is removed by burning with air at a temperature of 550°C. After that it is returned into the reactor, providing constant circulation of the carbonised catalyst from the reactor of pyrolysis into the regenerator and back.

EFFECT: application of the method makes it possible to increase selectivity of the process of obtaining lower olefins due to increase of the catalyst selectivity, applied in the process of methylene chloride pyrolysis.

2 ex, 2 tbl

FIELD: chemistry.

SUBSTANCE: invention relates to a method of catalytic methane oxychlorination in a deck-type adiabatic reactor under pressure of 1-10 atm in presence of a catalyst, which contains on a porous carrier with a specific surface of 1-60 m2/g a mixture of copper, potassium and lanthanum chlorides in a molar ratio of 1:1:0.3 in an amount of 3-30 wt % of the carrier weight and distributed on each reactor deck by 30% higher than the previous one. The two-layered catalyst in the form of equal in volume layers is loaded into the deck-type adiabatic reactor by a flow of reaction gas on each deck of the adiabatic reactor, the first layer of the catalyst contains a mixture of copper, potassium and lanthanum chlorides in a molar ratio of 1:1:0.3, and the second layer of the catalyst - a mixture of copper and potassium chlorides in a molar ratio of 1:1.

EFFECT: conversion of hydrogen chloride remains stable when the claimed method is applied.

1 ex, 1 tbl

FIELD: chemistry.

SUBSTANCE: method is characterised by contacting a gas stream containing at least one of said hydrocarbons with a dehydrogenation catalyst containing gallium and platinum and deposited on a support made of aluminium oxide or aluminium oxide and silicon dioxide, at reaction temperature in a direct-flow, upward stream with weight ratio of catalyst to hydrocarbon of 5 to 100 in a dehydrogenation reactor, wherein the average contact time of the hydrocarbon with the catalyst in the zone of the dehydrogenation reactor ranges from 1 s to 4 s, and temperature and pressure in the dehydrogenation reactor range from 570 to 750°C and from 41.4 (6.0) to 308 (44.7) kPa (psia); and moving the hydrocarbon and the catalyst from the dehydrogenation reactor into a separation device, wherein the average contact time of the hydrocarbon with the catalyst at reaction temperature in the separation device is less than 5 s, and the full average contact time between the hydrocarbon, catalyst and the formed hydrocarbons is less than 10 s; and moving the catalyst from the separation device into a regenerator, where the catalyst is brought into contact with an oxygen-containing regenerating stream and additional fuel.

EFFECT: method has short contact time between the hydrocarbon and the catalyst.

7 cl, 5 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a method for combined production of petrol and propylene from heavy hydrocarbon material with initial boiling point of 340°C on a catalytic cracking apparatus (FCC), downstream of which there is an oligomerisation apparatus, capable of operating in two modes designated as "maximum propylene" and "maximum petrol", wherein for the "maximum propylene" mode, material fed into the oligomerisation apparatus consists of a C4 or C4/C5 olefin fraction, for the "maximum petrol" mode, material fed into the oligomerisation apparatus consists of a C3/C4 olefin fraction; catalytic cracking is carried out in a single reactor or in two different reactors, each reactor capable of operating in an ascending stream. The invention also relates to a method where catalytic cracking is carried out in a single reactor or in two different reactors, each reactor capable of operating in a descending stream.

EFFECT: improved flexibility of the method with respect to production of propylene and petrol.

6 cl, 2 dwg, 3 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of converting methanol material to olefins. The method involves: reacting the methanol material in a first conversion zone with a catalyst in reaction conditions effective to produce a first reaction zone effluent containing dimethyl ether (DME), unreacted methanol and water; cooling the first reaction zone effluent to separate DME as a first gaseous product from the first reaction zone effluent and to form a first aqueous stream containing water, unreacted methanol, soluble DME and oxygenates; further reacting the first gaseous product in a second conversion zone with a catalyst in reaction conditions effective to produce a second reaction zone effluent containing light olefins, unreacted DME, water and oxygenates; cooling the second reaction zone effluent to separate the light olefins and the unreacted DME as a second gaseous product from the second reaction zone effluent and to form a second aqueous stream containing water, soluble DME and oxygenates; compressing the unreacted DME and the light olefins; separating DME from the light olefins with an aqueous absorbing liquid to produce virtually DME free olefin product and a third aqueous stream containing the absorbing liquid, absorbed DME, soluble oxygenates and hydrocarbons; feeding at least a portion of the first, second and/or third aqueous streams into a stripper of a fractionation tower and stripping and recovering the methanol, DME, soluble oxygenates and hydrocarbons as an overhead gaseous product and a fourth aqueous stream containing substantially clean water as a bottom liquid product; and recycling at least a portion of the overhead gaseous product to the first conversion zone and/or to the second conversion zone.

EFFECT: use of the present method enables to minimise formation of reaction by-products which cannot be recycled or used in other processes.

10 cl, 1 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a method of dehydrogenating alkanes, according to which a mixture containing hydrocarbons, particularly alkanes, which can contain water vapour, is continuously fed through a catalyst bed at ordinary dehydrogenation conditions. The many-hours-long dehydrogenation step is followed by a step with bleeding of oxygen-free gas through a reactor layer in order to blow and remove reaction gas from the reactor layer, and this is followed by a step for bleeding oxygen-containing regeneration gas in order to remove deposits on the catalyst formed during the dehydrogenation reaction. This is followed by a step for bleeding oxygen-free gas in order to blow and remove regeneration gas from the reactor. Duration of bleeding oxygen-containing gas during catalyst regeneration is equal to or less than 70% of the total duration of regeneration, total regeneration time is equal to 1 hour and regeneration starts after a seven-hour step of obtaining the product. The method is characterised by that regeneration starts with a five-minute blowing step, followed by a step for regeneration with a gas which contains oxygen and water vapour for 20 minutes, followed by an additional blowing step.

EFFECT: method enables to preserve catalyst activity and selectivity with respect to the desired process and after many regeneration cycles.

12 cl, 5 ex, 4 tbl

FIELD: process engineering.

SUBSTANCE: invention relates to catalyst for catalytic cracking, to its production and use. Proposed catalyst comprises substrate including aluminium oxide and molecular sieve with the following distribution of pores: 5-70% of pores are sized to <2 nm, 5-70% of pores are sized to 2-4 nm, 0-10% of pores are sized to 4-6 nm, 20-80% of pores are sized to 6-20 nm, and 0-40% of pores are sized to 20-100 nm, proceeding from volume of pores sized to not over 100 nm. Proposed method comprises the following stages: mixing substrate including aluminium oxide or its precursors with molecular sieve, suspending and drying said mix by spray drying. Note here that in mixing, pore expander is introduced. Note also that said expander is selected from the group including boric acid and salts of alkaline metals. Note that expander-to-substrate weight ratio makes 0.1:100-15:100 in terms of substrate weight.

EFFECT: great volume of catalyst's pores, high capability of cracking heavy oil products and high stability of coving.

25 cl, 4 tbl, 11 ex, 1 dwg

FIELD: chemistry.

SUBSTANCE: one of the versions involves reaction of ketone and hydrogen at reaction temperature ranging from 150°C to 250°C in the presence of a Cu-containing hydrogenation catalyst and a metal oxide type solid acid, where the Cu-containing hydrogenation catalyst additionally contains at least one element from group IIIA, group IIB and group VIB of the periodic table of elements, and where the metal oxide type solid acid is β-zeolite.

EFFECT: use of the present invention enables to obtain olefins with high selectivity.

5 cl, 8 ex, 4 tbl

FIELD: oil and gas industry.

SUBSTANCE: invention refers to the method for obtaining lower olefinic hydrocarbons and includes pyrolysis of hydrocarbon raw material in presence of metallic catalyst applied to the carrier located inside the reactor. The method is characterised by the fact that propane-butane hydrocarbon mixture is used as hydrocarbon raw material, and nanostructure particles of metals formed on inner carrier surface are used as catalyst.

EFFECT: use of the present invention allows increasing ethylene and propylene output and excluding the coke formation.

7 cl, 4 dwg

FIELD: chemistry.

SUBSTANCE: system comprises a first a first reactor (14) an inlet, an outlet and a reaction zone, where the first reactor is capable of receiving a stream (12) of material containing oxygenates and hydrocarbons, converting a portion of the oxygenates to light olefins and alkylating aromatic compounds. The light olefins and the alkyl aromatic compounds are included in a first effluent stream (15). A separator system (18) in fluid connection with the outlet of the first reactor (14) for obtaining the first effluent stream (15) of the first reactor (14) and for forming a first product stream (20) containing a C3 olefin, a second stream (24) containing C7 aromatic compounds and a third stream (26) containing C8 aromatic compounds. The system further includes a first line connecting the separator (18) to the inlet of the first reactor (14) for conveying the second stream (24) to the first reactor (14). The system includes a second line in fluid connection with the separator system (18) for conveying the C3 olefin to a propylene recovery unit (56). The system includes a third line in fluid connection with the separator system (18) for conveying the C8 aromatic compounds to a xylene separating unit (30) and a second reactor (40) for obtaining a stream (28 and 29) of material containing C6+ aromatic hydrocarbons form the separator system (18) and subjecting the streams (28, 29) of material to conditions for transalkylating the C6+ aromatic hydrocarbons to form an effluent stream (46) rich in C8 hydrocarbons.

EFFECT: use of the present method enables to obtain xylenes together with propylene from methanol.

7 cl, 2 ex, 1 dwg

FIELD: process engineering.

SUBSTANCE: device (1) for processing of loose material ply (2) supported by aerating bottom (3) and subjected to cooling by gas fed towards said bottom (3) and extending upward through said bottom (3) and material ply (2) from underlying compartment (4) having sidewalls (5), end walls (6) and base (7). It differs from known designs in that it comprises a set of inspection channels (8) extending into compartment (4) from sidewalls (5), end walls (6) or base (7) and equipped with a set of inspection holes (9). Inspection channels allow the control over equipment at invisible sections of the compartment.

EFFECT: possibility of control over equipment at remote section of the compartment.

3 cl, 1 dwg

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