Improved metal passivator/trap for fcc processes
SUBSTANCE: present invention relates to a method of passivating and/or trapping at least one metal impurity from a liquid oil product in cracking apparatus on fluidised catalyst, comprising: contacting said liquid oil product, which contains at least one metal impurity, with a catalytic mixture containing 1) cracking catalyst on fluidised catalyst and 2) metal passivator/trap, which contain mixed metal oxide alloy of R, Sb, and optionally M, where R is Fe2+/3+ and M is an optional activator.
EFFECT: technical result is increased output of end products (selectivity with respect to transport fuel) due to reduced effect of catalyst deactivation by means of metal impurities in liquid oil products.
20 cl, 3 dwg, 6 tbl, 4 ex
FIELD: oil and gas industry.
SUBSTANCE: invention refers to catalytic cracking method involving mixing of recovered catalyst fed to precharge zone (VIII) with oil material, and supply of oil material to reaction zone (I) for catalytic cracking reaction; catalyst and oil gas lifting to catalyst separation zone (III) where a part of catalyst is separated and is transferred to boil-off zone for recovered catalyst (V, VII); remaining catalyst and oil gas are lifted together and then are mixed in the zone of repeated reaction (II) of oil gas with recovered catalyst fed to additional catalyst distribution zone (IV), and oil gas takes part in repeated catalytic reaction; then oil gas and catalyst in lift reactor are separated in sump (VI), recovered catalyst in the oil material reaction zone (I) and repeated oil gas reaction zone (II) are supplied to regenerator (13) after desorption processing with steam in the boil-off zone for recovered catalyst in order to be reactivated. Invention refers additionally to device for catalytic cracking.
EFFECT: improved method.
15 cl, 6 dwg
FIELD: oil and gas industry.
SUBSTANCE: invention refers to catalytic cracking of hydrocarbons. Method involves cracking reaction stage in an upflow fluidised bed reactor, stage of cracked hydrocarbon and coked catalyst separation, stage of cracked hydrocarbon fractioning, and stage of the coked catalyst recovery, where source hydrocarbon materials are fed to the upflow reactor to catalyst deactivated partially by preliminary coking of at least a part of the catalyst in the same upflow reactor so that reaction temperature for effluents discharged from the reactor varies from 470 to 600°C; such preliminary coking can be implemented by injection of at least one hydrocarbon compound with boiling point not lower than 350°C to at least a part of recovered catalyst, limited by at least one zone determined by internal device in the upflow reactor bottom part; source hydrocarbon materials for processing are supplied downstream after the top end of the internal device in the reactor if viewed against the catalyst flow in the reactor. Also, the invention refers to device for cracking method implementation.
EFFECT: maximised basic components of diesel fuel.
16 cl, 9 dwg, 4 tbl, 3 ex
SUBSTANCE: invention relates to methods of producing a catalyst for catalytic cracking, a method of catalytic cracking and the obtained catalyst application. The method contains the supply of the fresh catalyst into a fluidised bed, where it contacts with water vapour or a regenerated flue gas, and its ageing under hydrothermal conditions, including the temperature of ageing of 400-850°C, the surface linear rate of the fluidised bed of 0.1-0.6 m/s and the ageing time of 1-720 hours with the further supply of the produced catalyst into an industrial installation of catalytic cracking. The fresh catalyst contains, with respect to the total catalyst weight, 1-50% by weight of zeolite, 5-99% by weight of inorganic oxide, selected from SiO2 and/or Al2O3, and 0-70% by weight of additional clay. Clay is selected from kaolin and/or halloysite. Zeolite is selected from medium-pore zeolite ZSM or ZRP and/or large-pore zeolites, selected from a rare-earth element Y(REY), rare-earth hydrogen Y(REHYK) of ultrastable zeolite Y and high-silica zeolite Y. Another method of obtaining the catalyst contains: (1) supply of the fresh catalyst into the fluidised bed, introduction of a hot regenerated catalyst into the regenerator, with the realisation of heat exchange between the fresh catalyst and the hot regenerated catalyst in the fluidised bed; (2) realisation of contact of the product, obtained at stage (1) with vapour or with the regenerated flue gas under hydrothermal conditions, including the temperature of ageing of 400-850°C, the surface linear rate of the fluidised bed of 0.1-0.6 m/s and the time of ageing of 1-720 hours to obtain an aged catalyst, and (3) supply of the catalyst, produced at stage (2), into an industrial installation of catalytic cracking.
EFFECT: method makes it possible to regulate the catalyst activity and selectivity in an installation of catalytic cracking more evenly and considerably improves the selectivity of the catalytic cracking catalyst to considerably reduce the output of dry gas and coke, effectively use vapour and reduce energy consumption in FCC cracking.
15 cl, 4 dwg, 4 tbl, 3 ex
FIELD: oil and gas industry.
SUBSTANCE: invention is related to suppression methods of harmful effects of metals on catalytic cracking of hydrocarbon stock. This target is reached by use of metal-catching particle, which contains spray-dried mixture of kaolin, magnesium hydrate or oxide and calcium carbonate, at that the spray-dried mixture was ignited at temperature within the range from 816°C up to almost 899°C. The invention is also related to a metal passivation method, which includes: contact of hydrocarbon flow containing metal in the fluid-catalytic cracking plant with mixture of suspended cracking catalyst and granulate metal trap; at that the metal trap contains spray-dried mixture of kaolin, magnesium hydrate or oxide, and calcium carbonate, at that the spray-dried mixture subjected to ignition at temperature within the range from 816°C up to almost 899°C and the ignited metal trap contains magnesium oxide in quantity of at least 10 wt %.
EFFECT: invention is related to suppression methods of harmful effects of metals on catalytic cracking of hydrocarbon stock.
20 cl, 1 dwg, 4 ex
SUBSTANCE: invention relates to processes of paraffin dehydration. A method for the regulation of temperatures in a dehydration reactor includes the supply of a catalyst into the dehydration reactor in such a way that the catalyst flows downwards via the reactor, supply of the flow, enriched with paraffins, into the dehydration reactor in such a way that the flow passes upwards via the reactor with the formation of a technological flow, which contains the catalyst and dehydrated hydrocarbons, as well as a certain amount of non-converted paraffins, separation of a vapour phase from the technological flow with the formation of a flow of products, supplying the flow of products into a cooling unit with the formation of a cooled flow of products and the supply of a part of the cooled flow of products into the technological flow.
EFFECT: invention provides the effective and economical dehydration process with the prevention of undesirable side reactions.
10 cl, 1 dwg
FIELD: oil-and-gas industry.
SUBSTANCE: invention covers a new olefins cracking catalyst. This catalyst comprises zeolite characterised by the silicon dioxide-to-aluminium oxide ratio of 400 or more and subjected to ion exchange for the decreasing of the content of alkaline and alkaline-earth metals to below 100 ppm and, then subjected to flushing by steam and acid.
EFFECT: catalyst is characterised by better selectivity relative to the propylene yield, decreased amount of aromatic compounds and methane.
7 cl, 1 tbl
SUBSTANCE: invention relates to catalytic cracking with a fluidised bed. The invention deals with a method which includes the following stages: a) functioning of a reaction zone, which contains at least one standpipe under conditions, contributing to obtaining olefins, and into the said at least one standpipe supplied are: i) the first raw material with a boiling temperature from 180 to 800°C; ii) the second raw material, which contains one or more C4 +-olefins, containing butanes; and iii) the third raw material, containing oligomerised light olefins or a ligroin flow, which contains from 20 to 70 wt % of one or more C5-C10-olefins; b) conversion of olefins in the second raw material into propylene; c) separation of the mixture from one or more reaction products in the separation zone; and d) extraction of one or more products in the division zone.
EFFECT: increased output of light olefins, in particular propylene.
10 cl, 7 dwg, 1 ex
SUBSTANCE: present invention relates to methods (versions) and apparatus (versions) for converting olefins, mixed with paraffins, into compounds with a higher molecular weight. Heavier compounds can be fed for recirculation into a reactor for carrying out an FCC process or are fed into a separate apparatus for carrying out an FCC process. The method includes transporting C4 olefins and paraffins and C5-C7 olefins and paraffins into a conversion zone for converting C4 olefins into compounds derived from C4, having a higher molecular weight, via oligomerisation or alkylation of C4 olefins with aromatic compounds, and converting C5-C7 olefins into compounds derived from C5-C7, having a higher molecular weight, via alkylation of C5-C7 olefins with aromatic compounds; separating the compounds derived from C4 from C4 olefins and paraffins; separating the compounds derived from C5-C7 from C5-C7 olefins and paraffins; and feeding the compounds derived from C4 and compounds derived from C5-C7 into a fluid catalytic cracking (FCC) reactor. The apparatus comprises a fractionation column; an aromatic compound alkylation reactor; a second conversion zone for converting C4 olefins into compounds derived from C4, having a higher molecular weight; a stripping column for the product; and a pipe for the still residue of said stripping column for the product, which is linked to the FCC reactor.
EFFECT: easy separation of olefins from paraffins contained in a product stream.
10 cl, 5 dwg
SUBSTANCE: invention relates to catalytic conversion of biorenewable material. The method for fluid catalytic cracking (FCC) of material containing at least one source of biorenewable material comprises the following steps: contacting material containing at least one hydrocarbon fraction and at least one source of biorenewable material with a cracking catalyst in FCC conditions, where said catalyst contains zeolite, having catalytic cracking activity, a matrix and at least 1% rare-earth metal oxide per total weight of the catalyst, wherein said catalyst is characterised by the ratio of zeolite surface area to matrix surface area of at least 2.
EFFECT: obtaining a cracked hydrocarbon product.
17 cl, 6 dwg, 4 tbl, 3 ex
FIELD: oil and gas industry.
SUBSTANCE: invention is related to a combined method of conversion of oil-derived hydrocarbon fractions into high-quality hydrocarbon mixtures as fuel, which includes catalytic cracking of hydrocarbon fraction in catalyst fluidised bed with catalyst containing ERS-10 zeolite, where the specified catalyst contains at least two components, where the specified components represent: (a) a component containing one or more catalytic cracking catalysts in fluidised, and (b) a component containing ERS-10 zeolite for obtaining Light Cycle Gas Oil (LCGO), hydrotreatment of light cycle gas oil, interaction of hydrotreated light cycle gas oil obtained at the previous stage of hydrotreatment in presence of hydrogen with catalytic system. The invention also touches the method of catalytic cracking and a stage of catalytic cracking in fluidised bed.
EFFECT: production of high-quality hydrocarbons, conversion increase.
21 cl, 3 tbl, 1 ex
SUBSTANCE: described is a catalyst additive for oxidising carbon monoxide when regenerating cracking catalysts, which contains a manganese compound, aluminium oxide, natural bentonite clay and amorphous aluminosilicate, with the following content of components, wt %: manganese in terms of MnO2 10-15, bentonite clay 20-30, amorphous aluminosilicate 16-25, Al2O3 - the balance, having spherical particles with average diameter of 70-85 mcm, wear-resistance of not less than 96% and packed density of 0.68-0.76 g/cm3. Described is a method of preparing said catalyst additive.
EFFECT: high activity of oxidising CO.
2 cl, 5 ex
FIELD: oil and gas industry.
SUBSTANCE: invention is related to plant for hydrocarbon conversion including reaction zone with delivery of transported catalyst to such zone. The plant for hydrocarbon (400, 500, 600) conversion contains the following: a) vessel for regeneration; b) device with vessel for delivery that ensures delivery of catalyst from low pressure zone to high pressure zone; at that this device contains the first pipeline for catalyst transportation into the vessel for delivery and in this connection the first pipeline is connected to the first valve delivering catalyst into the vessel for delivery; the second pipeline for catalyst transportation from the vessel for delivery, at that the second pipeline is connected to the second valve in order to ensure catalyst diversion from the vessel for delivery; and the third pipeline providing passage of gas through it at pressure higher than the first pressure; this pipeline has the first section communicating with the vessel for delivery and the second section connected to the third and fourth valves. Each of the third and forth valve has the first position which is an open position and the second position, which is a closed one, and it corresponds opening and closure of the first and second valves in order to ensure passage of gas. At that the first section of the third pipeline is connected to the second section between the third and fourth valves and one end of the second section is connected to the pipeline in order to outlet gas from the vessel for storage; c) reaction zone; at that the device that ensures delivery of catalyst from low pressure zone to high pressure zone is installed vertically in essence towards the reaction zone to ensure passage of the regenerated catalyst from the above device into the reaction zone by transportation by means of gravity.
EFFECT: implementation of conversion process.
9 cl, 5 dwg
SUBSTANCE: method involves the following steps at which: initial material is processed into the ash containing the metals subject to regeneration, which have been chosen from the metals including vanadium, metals of group 8-10 and metals of group 6; the above ash is leached by leaching solution so that the first solid substance is obtained, which contains metals of group 8-10, solid carbonaceous material and supernatant fluid containing vanadium and metal of group 6; supernatant fluid is mixed with solution of ammonia sulphate and the deposit containing vanadium and additional fluid containing metal of group 6 is obtained; additional supernatant fluid is mixed with leaching solution, solution of ammonia sulphate and solution of sulphuric acid and the deposit containing metal of group 6 is obtained.
EFFECT: methods are effective for regeneration of metals without formation of other undesirable by-products.
10 cl, 9 dwg, 12 tbl, 3 ex
FIELD: technological processes.
SUBSTANCE: this invention relates to a method to regenerate a catalyst for treatment of waste gas and to a catalyst regenerated by this method. The method to regenerate a catalyst 11 is described to treat waste gas containing ash stuck on its surface. The method includes grinding stage S1, in which the catalyst 11 for waste gas treatment is ground so that from 70 to 95 wt % of the entire catalyst 11 for waste gas treatment is turned into bulk pieces 12, with size that exceeds threshold size S (any value in the range from 0.105 to 1.0 mm); separation stage S2, in which fragments produced by grinding of the catalyst 11 for waste gas treatment, are separated into bulk pieces 12, having size that exceeds threshold size S, and fine particles 13, having size that is not more than threshold size S; stage S3 of grinding into powder, in which bulk pieces 12, separated this way, are ground into fine powder, having average diameter of particles of not more than 0.1 mm; stage S4 of mixing and stage S5 of forming, in which fine powder is mixed with other raw materials and is formed as catalyst for waste gas treatment; and stage S6 of drying and stage S7 of calcination, in which the formed precursor is dried and calcinated to thus produce the regenerated catalyst 14 for waste gas treatment. Catalyst is described, regenerated by this method.
EFFECT: production of regenerated catalyst having efficiency equivalent for a newly prepared catalyst.
7 cl, 3 tbl, 2 ex, 2 dwg
SUBSTANCE: invention relates to processes of generating catalysts for hydrogenation of plant oil and fat. The invention describes a method of regenerating a spent palladium-containing catalyst for hydrogenating plant oil and fat through treatment with sodium hydroxide solution and washing with a condensate, where the catalyst is pre-washed with steam condensate until there are no traces of fat while simultaneously bubbling with hydrogen. Treatment is carried out with 10% solution of sodium hydroxide while blowing with hydrogen at the same time. Washing is carried out with steam condensate until there are completely no traces of alkali and soap and drying is carried out in a hydrogen stream at 145-150°C for 8-9 hours.
EFFECT: attaining high degree of purification and regeneration of the catalyst.
FIELD: industrial organic synthesis.
SUBSTANCE: molybdenum is recovered from catalytic olefin epoxidation products using organic hydroperoxides. Method comprises treating heavy epoxidate fraction with alkali solution, treating resultant spent alkali stream with extractant, and subsequent precipitation of molybdenum trisulfide using sulfur-alkali effluents formed in production of olefins by pyrolysis of hydrocarbon feedstock.
EFFECT: increased molybdenum recovery degree and simplified operation.
SUBSTANCE: invention relates to method of preparing silicoaluminophosphate (SAPO) molecular sieves, to containing them catalysts, and to methods of catalytic dehydration with application of said catalysts. Described is method of preparing SARO molecular sieve, preferably, possessing crystalline structure SAPO-34, including the following stages: mixing source P with source Al obtaining mixture, addition to said first source Si and template obtaining suspension or slime to value in the interval from 5 to 6.8, hydrothermal processing of said suspension or slime obtaining suspension of SAPO molecular sieve, isolation from suspension of said SAPO molecular sieve and its drying, and before addition of said source Si and said template said mixture of sources P and Al is boiled with stirring, said stage of boiling is carried out at temperature in the interval from 50 to 100°C, preferably at 75°C, during period of time from 10 to 30 h, preferably 24 h. Described is SAPO molecular sieve, preferably, possessing crystalline structure SAPO-34, which can be prepared in accordance with described method and is characterised by the following chemical composition: (SixAlyPZ)O2, where x, y and z stand for mole fractions of respectively Si, Al and P, and x stands for mole fraction of Si and has value in the interval from 0.001 to 0.1, y stands for mole fraction of Al and has value within the interval from 0.25 to 0.5, z stands for mole fraction of P within the interval from 0.4 to 0.8. Described is catalyst, including SAPO molecular sieve and matrix material, selected from group, including aluminium oxide, silicon dioxide, aluminium silicate, silicon dioxide- aluminium oxide and natural kaolin, preferably, activated aluminium oxide, contains at least 50 wt % of pseudoboehmite. Described are method of converting methanol into dimethyl ether (DME), method of converting methanol into olefins in presence of described above catalyst.
EFFECT: obtaining very pure highly crystalline SAPO molecular sieves, possessing exceptional activity in dehydration reactions, with very high output.
16 cl, 4 tbl, 9 ex, 7 dwg
FIELD: process engineering.
SUBSTANCE: invention can be used in chemical and petrochemical industries. Air fed into apparatus of reclamation of zeolite or nonzeolite molecular sieve catalyst is cleaned of metal salts. First, initial air is cooled to remove air in condenser and, then rinsed in scrubber to remove, is fact, all salts from said initial air. Preferably, water removed at cooling stage is recirculated to remove salts from initial air.
EFFECT: longer life.
10 cl, 1 ex
FIELD: petrochemical process catalysts.
SUBSTANCE: invention relates to a process and apparatus for thermal removal of coke from loose mass of granulated selective zeolite catalyst based on pentasil-type crystalline aluminosilicates for production of olefins having 2 and 3 carbon atoms from mixture of olefins having 4-8 carbon atoms or methanol or dimethyl ether. Process is carried out in reactor (1) wherein catalyst is used in the form of loose mass. In preliminary stage, reactor (1) is flushed by heated nitrogen stream at entry temperature 460-500°C in order to replace hydrocarbons out of catalyst. Then, reactor is cooled by heated nitrogen stream at entry temperature from 420 to less than 460°C. In the main stage, nitrogen/air mix slowly heated to entry temperature 460-500°C is passed through reactor and, in additional stage, reactor is flushed by nitrogen stream heated to entry temperature 460-500°C in order to wash out air out of zeolite catalyst. Apparatus for implementation of described process comprises heater (6) designed to heat nitrogen and nitrogen/air streams, in series connected reactor (1), in series connected air cooler (12), and in series connected pressure gun (14).
EFFECT: preserved catalytically activity of zeolite catalyst.
10 cl, 1 dwg
FIELD: petroleum processing.
SUBSTANCE: method is accomplished by burning out carbon-containing compounds in oxygen-containing gas medium and comprises stages: desorption of hydrocarbons from catalyst surface performed in plant reactor and burning out of hydrocarbon thickening products performed on a special installation in indirect-heating rotary kiln at 450-550°C and excessive pressure 0.4-1.0 bar. Desorption of hydrocarbons from catalyst surface is carried out in a hydrogen-containing gas medium with 60-80 vol % H2, while gradually raising temperature from 200-220°C to 380-400°C at a rate 35-30°C/h following by aging of catalysts at 380-400°C until concentration of hydrocarbons in hydrogen-containing gas is no higher than 0.5 wt %, after which temperature is lowered to 100-120°C at a rate 20-25°C/h and active catalyst components are passivated. Passivation is accomplished by treatment at 100-120°C and excessive pressure 4-10 bar with mixture of inert gas and oxygen-containing gas, in particular carbon dioxide and/or air used in amount providing oxygen concentration in gas mixture 0.02-0.5 vol %, which corresponds to consumption of gas mixture 400-600 nm3/m3 catalyst. Treatment is conducted until oxygen concentrations at inlet and outlet of reactor are leveled.
EFFECT: enabled industrially feasible maximally possible restoration of catalyst activity with minimum destruction loss of catalyst.
4 tbl, 7 ex