Production of chemicals and fuels from biomass

The present invention provides methods, reactor systems, and catalysts for converting in a continuous process biomass to fuels and chemicals. The invention includes methods of converting the water insoluble components of biomass, such as hemicellulose, cellulose and lignin, to volatile C 2+ O 1-2 oxygenates, such as alcohols, ketones, cyclic ethers, esters, carboxylic acids, aldehydes, and mixtures thereof. In certain applications, the volatile C 2+ O 1-2 oxygenates can be collected and used as a final chemical product, or used in downstream processes to produce liquid fuels, chemicals and other products.

Fischer-tropsch catalyst regeneration

A process for the regeneration of deactivated catalyst from a Fischer-Tropsch synthesis reactor, the catalyst being a supported cobalt catalyst. The process comprises the following steps: a withdrawal step, in which a portion of deactivated catalyst together with liquid hydrocarbon is withdrawn from the reactor; a concentration step, in which the concentration of the catalyst in the liquid hydrocarbon is increased; a calcination step, in which the deactivated catalyst composition is subjected to an oxidising gas to oxidise carbonaceous material contained in the deactivated catalyst in to gaseous oxides of the components of the carbonaceous material; and a reactivation step, in which the deactivated catalyst composition is reactivated to produced a regenerated catalyst.

Method for regenerating and hydrogenation catalyst

Disclosed is a method for regenerating a hydrogenation catalyst. More specifically, disclosed is a method for regenerating a hydrogenation catalyst poisoned during hydrogenation of a hydroformylation product for preparation of alcohol by stopping hydrogenation in a hydrogenation stationary phase reactor in which the hydrogenation catalyst is set and flowing hydrogen gas under a high temperature normal pressure. The method has an effect in that the poisoned hydrogenation catalyst can be efficiently recovered through a simple process.

METHODS OF REFINING NATURAL OILS, AND METHODS OF PRODUCING FUEL COMPOSITIONS

A method for suppressing dehydrogenation includes reacting an optionally functionalized olefin reactant in a metathesis reaction to form an olefin metathesis product; and providing a dehydrogenation suppression agent in admixture with (a) the olefin metathesis product and/or the optionally functionalized olefin reactant, and (b) a metal-containing material selected from the group consisting of residual metathesis catalyst, a hydrogen transfer agent, and a combination thereof, under conditions that are sufficient to passivate at least a portion of the metal-containing material. Methods of refining natural oils and methods of producing fuel compositions are also described. 1. A method of refining a natural oil comprising:providing a feedstock comprising a natural oil;reacting the feedstock in the presence of a metathesis catalyst to form a metathesized product comprising olefins and esters;providing a dehydrogenation suppression agent in admixture with the feedstock and/or the metathesized product;passivating a metal-containing material with the dehydrogenation suppression agent;separating the olefins in the metathesized product from the esters in the metathesized product; and wherein the metal-containing material comprises residual metathesis catalyst, a hydrogen transfer agent, or a combination thereof; and', 'wherein non-passivated metal-containing material is configured to participate in, catalyze, promote, and/or facilitate dehydrogenation of the natural oil and/or the metathesized product., 'transesterifying the esters in the presence of an alcohol to form a transesterified product and/or hydrogenating the olefins to form a fully or partially saturated hydrogenated product;'}2. The invention of wherein the natural oil and/or the metathesized product comprises one or a plurality of substructures having a formula —CH═CH—CH—CH═CH—.3. The invention of wherein the natural oil is selected from the group consisting of canola oil claim 1 , rapeseed oil claim 1 , coconut ...

METHOD FOR STOPPING OPERATION OF REACTOR

The method for stopping operation of a reactor is provided with a stop step of stopping supply of a synthesis gas containing a carbon monoxide gas and a hydrogen gas into the reactor; a slurry discharge step of discharging slurry from the reactor; a steam supply step of supplying steam higher in temperature than the decomposition temperatures of metal carbonyls into the reactor, thereby discharging gaseous matters inside the reactor; and a carbon monoxide gas detecting step of detecting an amount of carbon monoxide gas contained in the gaseous matters discharged from the reactor. In the steam supply step, supply of the steam is stopped when an amount of the detected carbon monoxide gas continuously declines to be lower than a predetermined reference value. 1. A method for stopping operation of a reactor , which is performed after hydrocarbon compounds are synthesized by supplying a synthesis gas containing a carbon monoxide gas and a hydrogen gas into the reactor which accommodates slurry , the method comprising: a slurry discharge step of discharging the slurry from the reactor after the stop step;', 'a steam supply step of supplying steam higher in temperature than the decomposition temperatures of metal carbonyls into the reactor after the slurry discharge step, thereby discharging gaseous matters inside the reactor; and', 'a carbon monoxide gas detecting step of detecting during the steam supply step an amount of carbon monoxide gas contained in the gaseous matters discharged from the reactor, wherein', 'in the steam supply step, supply of the steam is stopped when an amount of the detected carbon monoxide gas continuously declines to be lower than a predetermined reference value., 'a stop step of stopping supply of the synthesis gas into the reactor;'}2. The method for stopping operation of a reactor according to claim 1 , further comprising:an inert gas filling step of filling an inert gas into the reactor after the slurry discharge step and before the steam ...

TEMPERATURE CONTROL SYSTEM, HYDROCARBON SYNTHESIS REACTION APPARATUS, HYDROCARBON SYNTHESIS REACTION SYSTEM, AND TEMPERATURE CONTROL PROCESS

The temperature control system is provided with a lower heat removing unit which is disposed at the bottom of a reactor inside which an exothermic reaction takes place and through which a liquid coolant is flowed, and an upper heat removing unit which is disposed in the reactor further above from the lower heat removing unit and through which the liquid coolant is flowed, recovering reaction heat inside the reactor and controlling a temperature inside the reactor. The lower heat removing unit is supplied with the liquid coolant which is adjusted for temperature by a first temperature adjustment unit, and the upper heat removing unit is supplied with the liquid coolant which is adjusted for temperature by a second temperature adjustment unit different from the first temperature adjustment unit. 1. A temperature control system for controlling a temperature inside a reactor in which an exothermic reaction takes place by recovering reaction heat in the reactor , the temperature control system comprising:a lower heat removing unit which is disposed at the bottom of the reactor and through which a liquid coolant is flowed; andan upper heat removing unit which is disposed in the reactor further above from the lower heat removing unit and through which the liquid coolant is flowed, whereinthe lower heat removing unit is supplied with the liquid coolant which is adjusted for temperature by a first temperature adjustment unit, andthe upper heat removing unit is supplied with the liquid coolant which is adjusted for temperature by a second temperature adjustment unit different from the first temperature adjustment unit.2. The temperature control system according to comprising:a reaction heat temperature determination unit which determines a temperature inside the bottom of the reactor, whereinthe first temperature adjustment unit is controlled on the basis of a determination result of the reaction heat temperature determination unit.3. The temperature control system according ...

METHOD FOR PRODUCING HYDROCARBON OIL, FISCHER-TROPSCH SYNTHESIS REACTION DEVICE, AND HYDROCARBON OIL PRODUCTION SYSTEM

The present invention provides a process for producing a hydrocarbon oil by performing a Fischer-Tropsch synthesis reaction using a reactor for a Fischer-Tropsch synthesis including a reaction apparatus having a slurry containing catalyst particles and a gaseous phase located above the slurry to obtain a hydrocarbon oil, wherein the Fischer-Tropsch reaction is performed while controlling a temperature of the slurry so that a difference T−Tbetween the average temperature Tof the slurry and a temperature Tat the liquid level of the slurry in contact with the gaseous phase is 5 to 30° C. 1. A process for producing a hydrocarbon oil by performing a Fischer-Tropsch synthesis reaction using a reactor for a Fischer-Tropsch synthesis comprising a reaction apparatus having a slurry containing catalyst particles and a gaseous phase located above the slurry to obtain a hydrocarbon oil , wherein{'sub': 2', '1', '1', '2, 'the Fischer-Tropsch reaction is performed while controlling a temperature of the slurry so that a difference T−Tbetween an average temperature Tof the slurry and a temperature Tof a liquid level of the slurry in contact with the gaseous phase is 5 to 30° C.'}2. A reactor for a Fischer-Tropsch synthesis for obtaining a hydrocarbon oil by contacting raw gas containing carbon monoxide and hydrogen with a slurry containing catalyst particles , the reactor comprising:a reaction apparatus having the slurry and a gaseous phase located above the slurry;a raw gas feeder for feeding the raw gas to the slurry; and{'sub': 2', '1', '1', '2, 'temperature control means for controlling a temperature of the slurry so that a difference T−Tbetween the average temperature Tof the slurry and a temperature Tat the liquid level of the slurry in contact with the gaseous phase is 5 to 30° C.'}3. A system for producing a hydrocarbon oil claim 2 , comprising the reactor for a Fischer-Tropsch synthesis according to . The present invention relates to a reactor for a Fischer-Tropsch ...

PROCESS FOR THE CONVERSION OF OXYGENATES TO C5+ HYDROCARBONS BOILING IN THE GASOLINE BOILING RANGE

Process for the conversion of oxygenates to C hydrocarbons boiling in the gasoline boiling range, comprising the steps of continuously a) providing one or more feed streams of one or more oxygenate compounds; b) heating the one or more feed streams to an inlet temperature of one or more downstream conversion reactors; c) introducing the one or more heated feed stream into inlet of the one or more conversion reactors; d) converting in the one or more conversion reactors the one or more heated feed stream in presence of catalyst to a converted oxygenate product comprising C hydrocarbons; e) withdrawing from the one or more conversion reactors the converted oxygenate product; f) determining at outlet of the one or more conversion reactors amount of the one or more unconverted oxygenate compounds in the withdrawn converted oxygenate product; g) separating the converted oxygenate product into a Chydrocarbon fraction, a fraction with the Chydrocarbons boiling in the gasoline boiling range and a fraction comprising water and the one or more unconverted oxygenate compounds, wherein the inlet temperature of the one or more feed streams in step b is continuously adjusted to maintain a constant amount of the one or more unconverted oxygenate compounds as determined in step f. 1. Process for the conversion of oxygenates to C hydrocarbons boiling in the gasoline boiling range , comprising the steps of continuouslya) providing one or more feed streams of one or more oxygenate compounds;b) heating the one or more feed streams to an inlet temperature of one or more downstream conversion reactors;c) introducing the one or more heated feed stream into inlet of the one or more conversion reactors;{'sub': '5+', 'd) converting in the one or more conversion reactors the one or more heated feed stream in presence of catalyst to a converted oxygenate product comprising C hydrocarbons;'}e) withdrawing from the one or more conversion reactors the converted oxygenate product;f) determining at ...

Enhanced Distillate Oil Recovery From Thermal Processing and Catalytic Cracking of Biomass Slurry

A method for thermal processing and catalytic cracking of a biomass to effect distillate oil recovery can include, particle size reduction. slurrying the biomass with a carrier fluid to create a reaction mixture, slurrying a catalyst with a carrier fluid to create a catalyst slurry, heating the reaction mixture and/or the catalyst slurry, and depolymerizing the reaction mixture with the catalyst. The reaction mixture can undergo distillation and fractionation to produce distillate fractions that include naphtha, kerosene, and diesel. In some embodiments, thermal processing and catalytic cracking includes vaporization of the biomass followed by distillation and fractionation. In some embodiments, a resulting distillate can be used as a carrier fluid. In some embodiments, the method can include desulfurization, dehydration, and/or decontamination. 1. A method of thermal processing and catalytic cracking of a biomass , the method comprising the steps of:(a) slurrying said biomass within a first carrier fluid to create a reaction mixture; dehydrating said reaction mixture to remove and recover the water;(b) slurrying a catalyst within a second carrier fluid to create a catalyst slurry, heating separately said reaction mixture and said catalyst slurry to different temperatures that once added together within a reactor, said catalyst slurry and said reaction mixture form a catalytic active biomass slurry, wherein said catalytic active biomass is at a temperature above a catalyst activation temperature of said catalyst to immediately initiate catalyst cracking;(c) directing a residual reaction mixture to a vaporizer for thermal processing, whereby an additional catalyst is optionally added and a system operated to cause both distillation and catalyst cracking, whereby a vapor is optionally further exposed to a different catalyst type using a different method of catalyst addition to enhance a quality and a composition of a distillate;(d) distilling via thermal processing a ...

DISCRIMINATE MASS TRANSFER IN A WET OXIDATION SYSTEM

A method for treatment of a carbonaceous feedstock such as coal or biomass. The method comprises adsorbing an oxidizing agent selected from an oxygen containing gas, hydrogen peroxide, ozone and oxidizing acids from a liquid phase of an aqueous mixture comprising water and a carbonaceous feedstock onto the surface of the and the carbonaceous feedstock to produce an aqueous mixture with the liquid phase having a reduced content of the oxidizing agent carbonaceous feedstock having oxidizing agent adsorbed on a surface thereof, and heating this aqueous mixture to a temperature and for a sufficient time to partially oxidize and solubilize at least a portion of the carbonaceous feedstock. The reaction products may be chemically or physically separated, recycled to the heating step and/or subjected to microbial digestion in order to generate one or more desirable products from the carbonaceous feedstock. The solid portion of the reaction products may be further processed to be used in the paper industry. 1. A method for treating a carbonaceous feedstock , comprising the steps of{'b': '100', 'adsorbing () at least one oxidizing agent selected from an oxygen-containing gas, hydrogen peroxide, ozone and oxidizing acids from a liquid phase of an aqueous mixture comprising water, at least one oxidizing agent and the carbonaceous feedstock, onto the carbonaceous feedstock under conditions at which substantially no oxidative depolymerization of carbonaceous materials of the carbonaceous feedstock will occur in order to produce an aqueous mixture with the liquid phase having a reduced content of the oxidizing agent and the carbonaceous feedstock having oxidizing agent adsorbed on a surface thereof; and'}{'b': 200', '100, 'heating () the aqueous mixture produced in the adsorbing step () to a temperature and for a sufficient time to oxidatively depolymerize and solubilize at least a portion of the carbonaceous feedstock.'}2. The method of claim 1 , wherein the oxidizing agent is an ...

Fcc co-processing of biomass oil

Systems and methods are provided for co-processing of biomass oil in a fluid catalytic cracking (FCC) system that include recovering an additional source of H 2 or synthesis gas from the overhead product gas stream. The additional H 2 can be used to partially hydrogenate biomass oil prior to co-processing the biomass oil in the fluid catalytic cracking system. Additionally or alternately, the additional synthesis gas can represent an additional yield of products from the process, such as an additional yield that can be used for synthesis of further liquid products.

SYSTEMS AND METHODS FOR IMPROVING YIELDS OF HYDROCARBON FUELS FROM ALCOHOLS

Systems and methods are provided that permit temperature control of a catalyst bed for conversion of alcohols to fuel hydrocarbons by modulating the water content of the alcohol feed stream provided to the catalyst bed. Heat generated by exothermic reactions in the catalyst bed can be utilized to pre-heat the alcohol feed stream. In some embodiments a secondary catalyst bed is provided for the conversion of light hydrocarbons found in the initial hydrocarbon product to fuel hydrocarbons that are liquid at ambient temperature and pressure. 135.-. (canceled)36. A method for controlling temperature in a catalyst bed comprising:providing a catalyst bed configured to process alcohol to a fuel hydrocarbon mixture;providing a first flow of a first stream comprising the alcohol;directing a second flow of a second stream comprising water into the first stream to produce a third stream, wherein the third stream is directed to the catalyst bed; andmodulating the first flow or the second flow to modulate water content of the third stream to maintain temperature of the catalyst bed within a desired temperature range.37. The method of claim 36 , further comprising the step of generating temperature data characterizing temperature of the catalyst bed.38. The method of claim 37 , further comprising the steps of:providing the temperature data to a controller;within the controller, using an algorithm to determine a flow rate of either the first flow or the second flow necessary to maintain temperature of the catalyst bed within a desired range; andtransmitting an instruction from the controller to a flow control device to modulate flow rate of either the first flow or the second flow.39. The method of claim 36 , wherein a mean temperature within the desired temperature range is from 200° C. to 600° C. claim 36 , and wherein the mean temperature is surrounded by a temperature range selected from the group consisting of ±20° C. claim 36 , ±30° C. claim 36 , ±40° C. claim 36 , ±50° C. ...

Recovery system for high pressure processing system

The invention relates to a method of separating and purifying products from a high pressure processing system adapted for processing a feed mixture comprising carbonaceous material(-s) at a pressure of from about 150 bar to about 400 bar and a temperature from about 300° C. to about 430° C. in the presence of homogeneous catalysts in the form of potassium and/or sodium in a concentration of at least 0.5% by weight and liquid organic compounds in a concentration from about 5% to about 40% by weight in a predefined time thereby producing a converted feed mixture, wherein the converted feed mixture is cooled to a temperature in the range 50 to 250° C., and depressurized to a pressure in the range 1 to 150 bar, and where the converted feed mixture is separated in to a gas phase comprising carbon dioxide, hydrogen, and methane, an oil phase comprising oil phase liquid organic compounds, and a water phase comprising water phase liquid organic compounds, dissolved salts and optionally suspended particles, where the water phase liquid organic compounds and dissolved homogenous catalysts in the form of potassium and/or sodium are at least partly recovered from said water phase thereby producing a first water phase stream enriched in water phase liquid organic compounds and homogeneous catalysts in the form of potassium and sodium, and a second water phase stream depleted in water phase liquid organic compounds and homogeneous catalysts in the form of potassium and sodium, where the first water phase is at least partly recycled to said the feed mixture to provide at least part of said liquid organic compounds and homogeneous catalysts in the feed mixture, and where further a bleed stream is withdrawn from said water phase enriched in water phase liquid organic compounds and homogeneous catalysts in the form of potassium and sodium prior to recycling said first recycle stream to the feed mixture.

Hydrocarbon aromatization catalyst composition and method of formation

A method for forming a catalyst can comprise: heating a Ge-ZSM-5 zeolite powder at a temperature of 400 to 600° C.; ion-exchanging the heat-treated zeolite powder with an alkali metal and impregnating the heat-treated zeolite powder with noble metal; heating the ion-exchanged, impregnated zeolite powder to a temperature of 250 to 350° C.; mixing the second heat-treated zeolite powder with a solid silica binder and a colloidal silica binder to form a mixture, wherein if the solid silica has a purity of less than or equal to 66 wt % of silica oxide based on the total weight of the solid silica, then the mixture is free of an extrusion aide and the colloidal silica has a particle size of less than 20 nm as measured along a major axis; forming the mixture into a shaped body; and heating the shaped body to 100 to 350° C. to result in the catalyst.

Enhanced Distillate Oil Recovery from Thermal Processing and Catalytic Cracking of Biomass Slurry

A method for thermal processing and catalytic cracking of a biomass to effect distillate oil recovery can include, particle size reduction. slurrying the biomass with a carrier fluid to create a reaction mixture, slurrying a catalyst with a carrier fluid to create a catalyst slurry, heating the reaction mixture and/or the catalyst slurry, and depolymerizing the reaction mixture with the catalyst. The reaction mixture can undergo distillation and fractionation to produce distillate fractions that include naphtha, kerosene, and diesel. In some embodiments, thermal processing and catalytic cracking includes vaporization of the biomass followed by distillation and fractionation. In some embodiments, a resulting distillate can be used as a carrier fluid. In some embodiments, the method can include desulfurization, dehydration, and/or decontamination. 1. A method of thermal processing and catalytic cracking of a biomass , the method comprising the steps of:(a) slurrying said biomass within a first carrier fluid to create a reaction mixture;(b) slurrying a first catalyst within a second carrier fluid to create a catalyst slurry; and(c) mixing said catalyst slurry and said reaction mixture to form a catalytic active biomass slurry, wherein said catalytic active biomass is at a temperature above a catalyst activation temperature of said first catalyst to initiate catalytic cracking.2. The method of further comprising:(d) distilling a carrier fluid portion containing a plurality of residuals to enable said carrier fluid portion to be recycled.3. The method of further comprising:(d) directing a residual reaction mixture, wherein said residual reaction mixture is made up of a portion of said catalytic active biomass slurry, to a vaporizer for thermal processing.4. The method of further comprising:(d) dehydrating said reaction mixture to remove an amount of water.5. The method of further comprising:(d) dehydrating said reaction mixture to recover an amount of water.6. The method ...

Renewable Diesel Fuel Production in Retrofitted Fossil Petroleum Refinery to Produce Biiofuel and Bio-Feedstock for Steam Crackers

The present invention relates to a process for the conversion of a feedstock comprising at least 50 wt % related to the total weight of the feedstock of triglycerides, fatty acid esters and/or fatty acids having at least 10 carbon atoms into hydrogen, olefins, dienes, aromatics, gasoline, diesel fuel, jet fuel, naphtha and liquefied petroleum gas comprising: 112.-. (canceled)14. The process according to wherein the first and second reactors are existing units used and wherein the process is obtained from the retrofit of an existing plant.15. The process according to wherein the feedstock comprises at least 25 wt % of triglycerides claim 13 , fatty acid esters and/or fatty acids related to the total weight of the feedstock.16. The process according to wherein hydrogen used in step a) is supplied from a naphtha reformer claim 13 , steam cracker being the steam cracker of step c) or steam methane reformer.17. The process according to wherein in step c) the sum of hydrogen claim 13 , ethylene claim 13 , propylene claim 13 , butadiene and benzene produced on the steam cracker originating from the first stream is at least 60 wt % of the converted first stream.18. The process according to wherein the naphtha or liquefied petroleum gas or any mixture thereof produced in step d) are mixed with the first stream of step c) before being sent to the steam cracker of step c).19. The process according to wherein the triglycerides claim 13 , fatty acids esters and/or fatty acids contained in the feedstock are obtained by at least one of the following purification steps:Chemical refining, physical refining, including degumming, bleaching, steam distillation or vacuum distillation, of fats and oils, orhydrolysis of triglycerides of fats and oils, to obtain glycerol and a mixture of free fatty acids.20. The process according to wherein the hydrodesulfurization catalyst is selected among Ni claim 13 , Mo claim 13 , W claim 13 , Co or mixtures like NiW claim 13 , NiMo claim 13 , CoMo ...

IMPROVED METHOD FOR PREPARING START UP OF PROCESS AND EQUIPMENT FOR PRODUCING LIQUID HYDROCARBONS

The invention relates to a process for continuously converting carbonaceous material contained in one or more feedstocks into a liquid hydrocarbon product, said feedstocks including the carbonaceous material being in a feed mixture including one or more fluids, said fluids including water, the process comprising: converting at least part of the carbonaceous material by pressurising the feed mixture to an operational pressure in the range 150-400 bar, heating the feed mixture to an operational temperature in the range 300-450° C., and maintaining said pressurized and heated feed mixture in the desired pressure and temperature ranges in a reaction zone for a predefined time; cooling the feed mixture to a temperature in the range 25-200° C. and expanding the feed mixture to a pressure in the range of 1-70 bar, thereby causing the carbonaceous material to be converted to a liquid hydrocarbon product; and separating from the converted feed mixture a fraction comprising liquid hydrocarbon product; where prior to the pressurisation and heating of the feed mixture the system has been brought to an operational state by filling the system with a fluid while the system being at a temperature and a pressure below the operational temperature and pressure, and subsequently heating and pressurizing the fluid to the operational conditions at a predetermined heating and pressurisation rate, where the pressure is constantly kept at a level above the saturation pressure for the fluid at a given temperature; and where upon reaching the operational temperature and pressure the fluid inflow to the pressurisation is terminated and the feed mixture inflow to the pressurisation is initiated. 112-. (canceled)14. A method according to claim 13 , where the heating rate is preferably 2 to 10° C./min claim 13 , most preferably the heating rate is in the range 3-8° C./min.15. A method according to claim 13 , where the pressure is at least 150 bars such as at least 180 bars claim 13 , preferably ...

REGENERATED CATALYST COOLING METHOD AND DEVICE THEREFOR

The present invention provides a method of cooling a regenerated catalyst and a device thereof, which employs low-line-speed operation, wherein a range of the superficial gas velocity is 0.005-0.7 m/s, wherein at least one fluidization wind distributor is provided, wherein the main fluidization wind enters the dense bed layer of the catalyst cooler from the distributor, and the heat removal load of the catalyst cooler and/or the temperature of the cold catalyst is controlled by adjusting the fluidization wind quantity. The method and a device thereof of the present invention has an extensive application range, and can be extensively used for various fluid catalytic cracking processes, including heavy oil catalytic cracking, wax oil catalytic cracking, light hydrocarbon catalytic conversion and the like, or used for other gas-solid fluidization reaction charring processes, including residual oil pretreating, methanol to olefin, methanol to aromatics, fluid coking, flexicoking and the like. 112-. (canceled)13. A method of cooling a regenerated catalyst , comprising providing a catalyst cooler comprising a catalyst outlet , at least one fluidization medium distributor , heat exchange tubes , a dense phase fluidized bed , and a catalyst inlet;providing hot catalyst particles, wherein the hot catalyst particles enter from the catalyst inlet, flow downwardly through the dense fluidized bed, and are cooled by pipe wall of the heat exchange tubes, and the cooled catalyst flows out from the catalyst outlet at its bottom; andfeeding a fluidized medium from the at least one fluidization medium distributor at the bottom, wherein the fluidized medium flows upwardly through the dense phase fluidized bed, along with a removed gas that is entrained by the hot catalyst particles from a regenerator, and returns to the regenerator.14. The method of claim 13 , further comprising:adjusting a flow rate of the fluidized medium and/or adjusting a flow rate of the cooled catalyst leaving ...

PROCESS FOR PRODUCING DIESEL FUEL FROM A BIORENEWABLE FEED

The process produces a diesel from a biorenewable feedstock by hydrotreating to remove heteroatoms and saturate olefins. The biorenewable feedstock is contacted in a guard bed reactor in the presence of hydrogen to saturate olefins and remove metals to produce a contacted feed stream. The contacted feed stream is then heated in a charge heater to a higher temperature than in the guard bed reactor and hydrotreated in the presence of a hydrotreating hydrogen stream and a hydrotreating catalyst to deoxygenate the contacted feed stream to provide a hydrotreated stream. 1. A process for hydrotreating a biorenewable feedstock , the process comprising:contacting a biorenewable feed stream with a guard bed catalyst in a guard bed reactor in the presence of hydrogen to saturate olefins and remove metals to produce a contacted biorenewable feed stream;heating said entire contacted biorenewable feed stream in a charge heater; andhydrotreating said contacted biorenewable feed stream in the presence of a hydrotreating hydrogen stream and a hydrotreating catalyst to deoxygenate said contacted biorenewable feed stream to provide a hydrotreated stream.2. The process of further comprising heating the biorenewable feed stream by heat exchange with the hydrotreated stream.3. The process of further comprising measuring the temperature of the contacted biorenewable feed stream exiting the heat exchange claim 2 , comparing it to a set point and bypassing a portion of the hydrotreated stream around the heat exchange with the contacted biorenewable feed stream to decrease the temperature of the contacted biorenewable feed stream exiting the heat exchange.4. The process of further comprising charging the guard bed reactor with the biorenewable feed stream at a guard inlet temperature claim 1 , discharging the contacted biorenewable feed stream from the guard bed reactor at a guard outlet temperature that is greater than the guard inlet temperature and charging said contacted biorenewable ...

DISCRIMINATE MASS TRANSFER IN A WET OXIDATION SYSTEM

A method for treatment of a lignocellulosic biomass using an oxidizing agent selected from an oxygen-containing gas, hydrogen peroxide, ozone and oxidizing acids. The treatment products may be subjected to microbial digestion in order to generate one or more desirable products from the carbonaceous feedstock. The solid portion of the reaction products may be further processed to be used in the paper industry. 1. A method for treating a lignocellulosic biomass , comprising the steps of:{'b': '10', 'swelling () the lignocellulosic biomass with water and/or steam in the presence of a chemical base;'}{'b': 100', '10, 'adsorbing (), after the swelling step (), at least one oxidizing agent selected from an oxygen-containing gas, hydrogen peroxide, ozone and oxidizing acids from a liquid phase of an aqueous mixture comprising water, at least one oxidizing agent and the lignocellulosic biomass, onto the lignocellulosic biomass under conditions at which substantially no oxidative depolymerization of carbonaceous materials of the lignocellulosic biomass will occur in order to produce an aqueous mixture with the liquid phase having a reduced content of the oxidizing agent and lignocellulosic biomass having oxidizing agent adsorbed on a surface thereof; and'}{'b': 200', '100, 'heating () the aqueous mixture produced in the adsorbing step () to a temperature and a sufficient time to oxidatively depolymerize and solubilize at least a portion of the lignocellulosic biomass.'}210. The method of claim 1 , wherein the swelling step () is carried out at a temperature in a range of from about 25° C. to about 100° C. and under a pressure of less than about 30 psi.3100. The method of claim 1 , wherein the adsorbing step () is carried out a temperature below about 220° C. for a period of less than about 1 hour.4200. The method of claim 1 , wherein the products of the heating step () have an oxygen to carbon molar ratio that is from 30% to 200% higher than an oxygen to carbon molar ratio ...

A METHOD FOR PRODUCING HIGH-OCTANE MOTOR GASOLINES OF LOW-OCTANE HYDROCARBON FRACTIONS, FRACTIONS OF GASEOUS OLEFINS AND OXYGENATES AND A PLANT FOR THE METHOD EMBODIMENT

The invention relates to method and plant for the production of high-octane gasolines from raw hydrocarbon fractions, fractions of gaseous olefins and oxygenates. A method has been proposed, wherein the feedstock component flow is supplied to a unit for supplying flows to be treated, into the reactor, wherein the reaction is carried out in the presence of a zeolite-containing catalyst, high-octane gasoline is isolated by separation of the conversion product, while diverting simultaneously the reaction water and the exhaust gases. A reactor contains at least two reaction zones, between which there are further arranged means for mixing the reaction product from the previous reaction zone and the supplied oxygenates and olefin-containing feedstock, whereas using the unit for supplying flows there is supplied a flow oxygenates and olefin-containing feedstock and the flow of raw hydrocarbon fractions into the first reaction zone of the reactor, and the flow oxygenates and olefin-containing feedstock into the second reaction zone of the reactor.

Enhanced Distillate Oil Recovery From Thermal Processing and Catalytic Cracking of Biomass Slurry

A method for thermal processing and catalytic cracking of a biomass to effect distillate oil recovery can include, particle size reduction. slurrying the biomass with a carrier fluid to create a reaction mixture, slurrying a catalyst with a carrier fluid to create a catalyst slurry, heating the reaction mixture and/or the catalyst slurry, and depolymerizing the reaction mixture with the catalyst. The reaction mixture can undergo distillation and fractionation to produce distillate fractions that include naphtha, kerosene, and diesel. In some embodiments, thermal processing and catalytic cracking includes vaporization of the biomass followed by distillation and fractionation. In some embodiments, a resulting distillate can be used as a carrier fluid. In some embodiments, the method can include desulfurization, dehydration, and/or decontamination.

RED MUD COMPOSITIONS AND METHODS RELATED THERETO

This disclosure relates to red mud compositions. This disclosure also relates to methods of making red mud compositions. This disclosure additionally relates to methods of using red mud compositions. 1. A composition comprising:dried and calcined catalytic particles comprising red mud and one or more additives, wherein the particles comprise at least about 50% red mud by weight.2. The composition of claim 1 , wherein the one or more additives comprise nickel deposited onto the surface of the particles.3. The composition of claim 2 , wherein the nickel comprises up to and including about 40% of the particles by weight.4. The composition of claim 2 , wherein the particles comprise dried claim 2 , calcined claim 2 , and reduced particles.5. The composition of claim 2 , wherein the particles have a mean particle size of about 50 micron to about 250 micron.6. The composition of claim 2 , wherein the particles have a specific surface area of about 50 m/g to about 80 m/g.7. The composition of claim 1 , wherein the particles comprise a dried claim 1 , extruded claim 1 , and calcined particle.8. The composition of claim 7 , wherein the particles have a mean particle size of about 1 mm to about 5 mm.9. The composition of claim 7 , wherein the particles have a specific surface area of about 30 m/g to about 65 m/g.10. The composition of claim 7 , wherein the red mud comprises colloidally-dispersed red mud.11. The composition of claim 8 , wherein the one or more additives comprise colloidally-dispersed silica.12. The composition of claim 11 , wherein the particles comprise spray dried and agglomerated particles.13. The composition of claim 11 , wherein the particles have a mean particle size of about 250 micron to about 650 micron.14. The composition of claim 8 , wherein the one or more additives comprise colloidally-dispersed calcium oxide.15. The composition of claim 7 , wherein the one or more additives comprise colloidally-dispersed zirconia.16. The composition of claim 1 , ...

FISCHER-TROPSCH SYNTHESIS

A method () of synthesising Fischer-Tropsch products () includes feeding a synthesis gas () to a moving-bed Fischer-Tropsch synthesis reactor () containing a Fischer-Tropsch catalyst in a moving catalyst bed and catalytically converting at least a portion of the synthesis gas () in the moving catalyst bed to Fischer-Tropsch products (). The Fischer-Tropsch products () are removed from the moving-bed Fischer-Tropsch synthesis reactor (). The method () further includes, while the moving-bed Fisher-Tropsch synthesis reactor () is on-line, withdrawing a portion () of the Fischer-Tropsch catalyst from the moving-bed Fischer-Tropsch synthesis reactor (), adding a reactivated Fischer-Tropsch catalyst () to the moving-bed Fischer-Tropsch synthesis reactor (), and adding a fresh Fischer-Tropsch catalyst (), in addition to the reactivated catalyst (), to the moving-bed Fischer-Tropsch synthesis reactor (). 1. A method of synthesising Fischer-Tropsch products , the method includingfeeding a synthesis gas to a moving-bed Fischer-Tropsch synthesis reactor containing a Fischer-Tropsch catalyst in a moving catalyst bed, catalytically converting at least a portion of the synthesis gas in the moving catalyst bed to Fischer-Tropsch products and withdrawing the Fischer-Tropsch products from the moving-bed Fischer-Tropsch synthesis reactor, withdrawing a portion of the Fischer-Tropsch catalyst from the moving-bed Fischer-Tropsch synthesis reactor;', 'adding a reactivated Fischer-Tropsch catalyst to the moving-bed Fischer-Tropsch synthesis reactor; and', 'adding a fresh Fischer-Tropsch catalyst, in addition to the reactivated catalyst, to the moving-bed Fischer-Tropsch synthesis reactor., 'the method further including, while the moving-bed Fisher-Tropsch synthesis reactor is on-line2. The method according to claim 1 , wherein at least a portion of the withdrawn Fischer-Tropsch catalyst is subjected to a reactivation treatment thereby to produce at least a portion of the reactivated ...

REMOVAL OF CATALYST FINES FROM FLUIDIZED BED EFFLUENT IN THE CONVERSION OF OXYGENATE FEEDSTOCK

A method comprising of converting an oxygenate feed stream stock to a hydrocarbon product stream having substantially no detectable solid content can include conveying the oxygenate feed stream stock through a fluidized catalyst bed comprising catalyst particles to convert the oxygenate feedstock to the product stream comprising catalyst particles and a hydrocarbon selected from the group consisting of a C gasoline, an olefin, an aromatic, and combinations thereof; and conveying the product stream through a plurality of filter units comprising filter medium to generate a filtered product stream having substantially no detectable solid material, wherein the filter medium comprises a metal alloy, a sintered metal alloy, or a combination thereof. 1. A method comprising:{'sub': '5+', 'conveying an oxygenate feed stream stock through a fluidized catalyst bed comprising catalyst particles to convert the oxygenate feedstock to a product stream comprising catalyst particles and a hydrocarbon selected from the group consisting of a C gasoline, an olefin, an aromatic, and combinations thereof; and'}conveying the product stream through a plurality of filter units comprising a filter medium to generate a filtered product stream having substantially no detectable solid material, wherein the filter medium comprises a metal alloy, a sintered metal alloy, or a combination thereof.2. The method of claim 1 , wherein the product stream comprises no detectable solid material.3. The method of claim 1 , further comprising separating the filtered product stream into one or more of a C gasoline fraction claim 1 , a C fraction claim 1 , an liquid petroleum gas fraction claim 1 , an aromatics fraction claim 1 , an olefin fraction claim 1 , and a C-Colefin fraction.4. The method of claim 3 , further combining the C fraction with the oxygenate feed stream.5. The method of claim 1 , further comprising alkylating Cand Cgasses in the filtered product stream to produce C gasoline.6. The method of ...

CONVERSION OF ALCOHOLS TO HYDROCARBONS USING A DUAL CATALYST SYSTEM COMPRISING BASIC OXIDE ON MIXED OXIDE OR MESOPOROUS CARRIER AND ETCHED METAL LOADED ZEOLITE CATALYST

A method for converting an alcohol to hydrocarbons comprises two serially placed catalysts. The fraction of aromatics is reduced to desired levels. The method comprises: a) contacting the alcohol with a first catalyst on a carrier, said carrier is selected from a mixed oxide and a mesoporous carrier, said first catalyst comprises at least one basic oxide and optionally at least one selected from the group consisting of metals and metal oxides, then b) contacting the resulting mixture from step a) with a second catalyst wherein said second catalyst is an etched metal loaded zeolite catalyst wherein the etched metal loaded zeolite catalyst is manufactured with a method comprising etching with subsequent loading of metal onto the catalyst, wherein the metal is in the form of nanoparticles, and wherein at least two different metals are loaded onto the etched zeolite catalyst. The hydrocarbons are recovered and used for instance for fuel including gasoline, kerosene, diesel, and jet propellant, and jet fuel. Naturally, other uses of hydrocarbons should not be excluded. 1. A method for converting an alcohol to hydrocarbons , said method comprising the steps of:a) contacting the alcohol with a first catalyst on carrier, said carrier is selected from a mixed oxide and a mesoporous carrier, said first catalyst comprises at least one basic oxide and optionally at least one selected from the group consisting of metals and metal oxides,b) contacting the resulting mixture from step a) with a second catalyst wherein said second catalyst is an etched metal loaded zeolite catalyst wherein the etched metal loaded zeolite catalyst is manufactured with a method comprising a step of etching with subsequent loading of metal onto the catalyst, wherein the metal is in the form of nanoparticles, and wherein at least two different metals are loaded onto the etched zeolite catalyst,c) recovering the hydrocarbons resulting from the reaction.2. The method according to claim 1 , wherein the ...

Method of simultaneous modeling and complexity reduction of bio-crudes for process simulation

The present invention relates to a method for reducing the complexity of bio-crudes. The method includes (a) obtaining experimental data of quantitative and qualitative analyses for the bio-crudes, (b) grouping compounds contained in the bio-crudes according to a predetermined basis based on the experimental data, (c) selecting representative compounds from among the compounds belonging to the same group, and (d) reconstituting the bio-crudes as a mixture of the representative compounds. In the method for reducing the complexity of the bio-crudes for process simulation according to the present invention, the number of constituent compounds of the bio-crudes is minimized and the physical properties of the bio-crudes are accurately represented using only experimental data obtained through GC-MS, thereby enabling accurate and efficient process simulation of the bio-crudes.

TURNING OXYGENATES UNDER HIGH PRESSURE AND HIGH PERFORMANCE WITH A CATALYST IMPACT CYCLE

В заявке описана реакционная система для газа/твердых частиц для усовершенствования рекуперации продукта в реакционной системе с несколькими реакторами. Оксигенатный исходный материал, целесообразно с высокой концентрацией оксигената, взаимодействует с катализатором, обладающим от низкой до умеренной кислотности и значением соотношения Si/Alот 0,10 до 0,32. Реакция протекает в реакционной зоне реактора с псевдоожиженным слоем под абсолютным парциальном давлением оксигената по меньшей мере 45 фунтов/кв.дюйм, при реакторной приведенной скорости газа по меньшей мере 10 футов/с и транспортировке катализатора через реакционную зону в циркуляционную зону. В циркуляционной зоне катализатор подвергается обработке вытеснением инертным газом при приведенной скорости вытесняющего газа по меньшей мере 0,03 м/с, после чего по меньшей мере часть, предпочтительно значительную часть, возвращают в реакционную зону. Катализатор характеризуется продолжительностью пребывания в циркуляционной зоне, по меньшей мере вдвое превышающей продолжительность пребывания катализатора в реакционной зоне. Экстраординарная активность катализатора при высокой селективности в отношении олефинов достигается несмотря на незначительные изменения содержания кокса на катализаторе и образовании коса, если сравнивать с процессами под более низким давлением. The application describes a gas / solids reaction system to improve product recovery in a multi-reactor reaction system. The oxygenate starting material, suitably with a high oxygenate concentration, is reacted with a catalyst having a low to moderate acidity and a Si / Al ratio of 0.10 to 0.32. The reaction proceeds in a reaction zone of a fluidized bed reactor at an oxygenate absolute partial pressure of at least 45 psi, a reactor superficial gas velocity of at least 10 ft / s, and transporting the catalyst through the reaction zone to a circulation zone. In the circulation zone, the catalyst is subjected to displacement treatment with an inert gas at a ...

Method and system for regenerating catalyst from a plurality of hydrocarbon conversion apparatuses

The present invention is directed to a method and system for integrating a catalyst regeneration system with a plurality of hydrocarbon conversion apparatuses, preferably, a plurality of multiple riser reactor units. One embodiment of the present invention is a reactor system including a plurality of reactor units, at least one reactor unit preferably comprising a plurality of riser reactors. The system also includes a regenerator for converting an at least partially deactivated catalyst to a regenerated catalyst. A first conduit system transfers the at least partially deactivated catalyst from the reactor units to the regenerator, and a second conduit system transfers regenerating catalysts from the regenerator to the plurality of reactor units. Optionally, catalysts from a plurality of hydrocarbon conversion apparatuses may be directed to a single stripping unit and/or a single regeneration unit.

用于由烃原料生产中间馏分油产物和低级烯烃的系统和方法

一种系统，其包括：提升管反应器，所述提升管反应器包含在催化裂化条件下的粗柴油原料和第一催化剂，以获得包含裂化粗柴油产物和第一用过的催化剂的提升管反应器产物；中间反应器，所述中间反应器包含在高苛刻度条件下的至少一部分裂化粗柴油产物和第二催化剂，以获得裂化中间反应器产物和第二用过的催化剂；其中中间反应器原料包含脂肪酸和脂肪酸酯中的至少一种。

Systems and methods for making a middle distillate product and lower olefins from a hydrocarbon feedstock

A system comprising a riser reactor for contacting a gas oil feedstock with a catalytic cracking catalyst under catalytic cracking conditions to yield a riser reactor product comprising a cracked gas oil product and a spent cracking catalyst; a separator for separating said riser reactor product into said cracked gas oil product and said spent cracking catalyst; a regenerator for regenerating said spent cracking catalyst to yield a regenerated catalyst; a intermediate reactor for contacting a gasoline feedstock with said regenerated catalyst under high severity conditions to yield a cracked gasoline product and a used regenerated catalyst; a first conduit connected to the intermediate reactor and the riser reactor, the first conduit adapted to send the used regenerated catalyst to the riser reactor to be used as the catalytic cracking catalyst; and a second conduit connected to the intermediate reactor and the regenerator, the second conduit adapted to send the used regenerated catalyst to the regenerator to yield a regenerated catalyst.

Catalyst pretreatment with aldehyde in an oxygenate to olefins reaction system

This invention concerns processes for converting oxygenates to olefins that include a step of pretreating catalyst used in the conversion reaction. A fresh or regenerated metalloaluminophosphate molecular sieve, which is low in carbon content, is pretreated with an aldehyde. The aldehyde forms a hydrocarbon co-catalyst within the pore structure of the molecular sieve, and the pretreated molecular sieve containing the co-catalyst is used to convert oxygenate to an olefin product.

Pretreating a catalyst containing molecular sieve and active metal oxide

This invention relates to processes for converting oxygenates to olefins that include a step of pretreating catalyst, which comprises molecular sieve and one or more active metal oxides of one or more metals, with a hydrocarbon composition to provide an integrated hydrocarbon co-catalyst within the molecular sieve. The combination of molecular sieve and hydrocarbon co-catalyst converts oxygenate to an olefin product with high selectivity to light olefins (i.e., ethylene or propylene, or mixture thereof).

Katalytisk omdannelse av oksygenater til olefiner

Reducing temperature differences within the regenerator of an oxygenate to olefin process

THE PRESENT INVENTION PROVIDES A PROCESS FOR MAKING AN OLEFIN PRODUCT FROM AN OXYGENATE FEEDSTOCK WHICH COMPRISES: a) CONTACTING THE FEEDSTOCK IN A REACTION ZONE WITH A CATALYST COMPRISING i) A MOLECULAR SIEVE HAVING DEFINED PORE OPENINGS AND ii) A CO OXIDATION METAL, UNDER CONDITIONS EFFECTIVE TO CONVERT THE FEEDSTOCK INTO AN OLEFIN PRODUCT STREAM COMPRISING C2-C3 OLEFINS AND TO FORM CARBONACEOUS DEPOSITS ON THE CATALYST SO AS TO PROVIDE A CARBON-CONTAINING CATALYST; a) CONTACTING AT LEAST A PORTION OF THE CARBON-CONTAINING CATALYST WITH A REGENERATION MEDIUM COMPRISING OXYGEN IN A REGENERATION ZONE COMPRISING A FLUID BED REGENERATOR HAVING A DENSE FLUID PHASE AND A DILUTE FLUID PHASE UNDER CONDITIONS EFFECTIVE TO OBTAIN A REGENERATED CATALYST PORTION, WHEREIN THE DIFFERENCE BETWEEN THE TEMPERATURE OF THE DILUTE PHASE AND THE TEMPERATURE OF THE DENSE PHASE IS NO GREATER THAN 100°C; c) INTRODUCING SAID REGENERATED CATALYST PORTION INTO SAID REACTION ZONE; AND d) REPEATING STEPS a)-c).(FIG.1)

Making an olefin product from an oxygenate

Disclosed is a method for making olefin product from an oxygenate-containing feedstock. In the method, a silicoaluminophosphate molecular sieve catalyst is contacted with the oxygenate-containing feedstock in a reactor at an average catalyst feedstock exposure index of at least 1.0. The method produces lower coke yield and provides an olefin product which is low in C 1 -C 4 paraffin content. The invention is particularly effective in producing an olefin product having a very low propane content.

Methanol, olefin, and hydrocarbon synthesis process

An improved method for the production of methanol and hydrocarbons from a methane-containing gas, such as natural gas. The improved method integrates a hydrocarbon synthesis unit with a methanol synthesis unit. The invention combines a syngas stream from a steam reformer, a syngas stream from an oxidation reformer and additional carbon dioxide to form an optimal syngas composition that is directed to a methanol synthesis reactor. The invention also integrates other process parameters and process components of a methanol and hydrocarbon synthesis process plant to effectively convert most of the carbon in the natural gas to commercial-value products. The invention is also directed to a method of making olefin from the methanol produced by the process of the invention.

Reactor with multiple risers and consolidated transport

The present invention is directed to a hydrocarbon conversion apparatus. The apparatus comprises the following: a plurality of riser reactors, each of the riser reactors having a first end into which a catalyst can be fed and a second end through which the catalyst can exit the riser reactor; a separation zone provided to separate the catalyst from products of a reaction conducted in the hydrocarbon conversion apparatus; at least one transport conduit having a first end in fluid communication with at least two of the second ends of the riser reactors and a second end extending into the separation zone; and at least one catalyst return in fluid communication with the separation zone and the first ends of the riser reactors, the catalyst return being provided to transfer the catalyst from the separation zone to the first ends of the riser reactors.

Multiple riser reactor with centralized catalyst return

The present invention is directed to a hydrocarbon conversion apparatus and process. The apparatus comprises the following: a plurality of riser reactors, each having a first end into which a catalyst is fed, a second end through which the catalyst can exit, and optionally a center axis extending therebetween. The apparatus also includes a separation zone having a plurality of inlets, each inlet not being oriented along the center axes of the riser reactors, the separation zone being provided to separate the catalyst from products of a reaction conducted in the hydrocarbon conversion apparatus. A plurality of deviating members are also provided, each deviating member being in fluid communication between the second end of a respective riser reactor and a respective inlet of the separation zone. The apparatus also includes a catalyst retention zone provided to contain catalyst, which is fed to the riser reactors. A catalyst return is in fluid communication between the separation zone and the catalyst retention zone.

Selectively removing undesirably sized catalyst particles from a reaction system

The present invention provides various processes for selectively removing undesirably sized catalyst particles from a reaction system. In one embodiment, a plurality of catalyst particles, having a first median particle diameter, is withdrawn from the reaction system and is directed to a separation unit such as a counter flow cyclone separator. In the separation unit, the particles are separated into a small catalyst stream and a large catalyst stream, the small catalyst stream having a second median particle diameter less than the first median particle diameter, and the large catalyst stream having a third median particle diameter greater than the first median particle diameter. At least a portion of the small or large catalyst stream is then directed back to the reaction system in order to maintain a desirable particle size distribution therein.

Multiple riser reactor

The present invention is directed to a hydrocarbon conversion apparatus. The apparatus comprises the following: a plurality of riser reactors, each of the riser reactors having a first end into which a catalyst can be fed and a second end through which the catalyst can exit the riser reactor, a separation zone into which the second ends of the riser reactors extend, the separation zone being provided to separate the catalyst from products of a reaction conducted in the hydrocarbon conversion apparatus; and at least one catalyst return in fluid communication with the separation zone and the first ends of the riser reactors, the catalyst return being provided to transfer the catalyst from the separation zone to the first ends of the riser reactors.

Multiple riser reactor

The present invention is directed to a hydrocarbon conversion apparatus. The apparatus comprises the following: a plurality of riser reactors, each of the riser reactors having a first end into which a catalyst can be fed and a second end through which the catalyst can exit the riser reactor, a separation zone into which the second ends of the riser reactors extend, the separation zone being provided to separate the catalyst from products of a reaction conducted in the hydrocarbon conversion apparatus; and at least one catalyst return in fluid communication with the separation zone and the first ends of the riser reactors, the catalyst return being provided to transfer the catalyst from the separation zone to the first ends of the riser reactors.

Multiple riser reactor

The present invention is directed to a hydrocarbon conversion apparatus. The apparatus comprises the following: a plurality of riser reactors, each of the riser reactors having a first end into which a catalyst can be fed and a second end through which the catalyst can exit the riser reactor; a separation zone into which the second ends of the riser reactors extend, the separation zone being provided to separate the catalyst from products of a reaction conducted in the hydrocarbon conversion apparatus; and at least one catalyst return in fluid communication with the separation zone and the first ends of the riser reactors, the catalyst return being provided to transfer the catalyst from the separation zone to the first ends of the riser reactors.

Reactor with multiple risers and consolidated transport

The present invention is directed to a hydrocarbon conversion apparatus. The apparatus comprises the following: a plurality of riser reactors, each of the riser reactors having a first end into which a catalyst can be fed and a second end through which the catalyst can exit the riser reactor; a separation zone provided to separate the catalyst from products of a reaction conducted in the hydrocarbon conversion apparatus; at least one transport conduit having a first end in fluid communication with at least two of the second ends of the riser reactors and a second end extending into the separation zone; and at least one catalyst return in fluid communication with the separation zone and the first ends of the riser reactors, the catalyst return being provided to transfer the catalyst from the separation zone to the first ends of the riser reactors.

Multiple riser reactor with centralized catalyst return

The present invention is directed to a hydrocarbon conversion apparatus and process. The apparatus comprises the following: a plurality of riser reactors, each having a first end into which a catalyst is fed, a second end through which the catalyst can exit, and optionally a center axis extending therebetween. The apparatus also includes a separation zone having a plurality of inlets, each inlet not being oriented along the center axes of the riser reactors, the separation zone being provided to separate the catalyst from products of a reaction conducted in the hydrocarbon conversion apparatus. A plurality of deviating members are also provided, each deviating member being in fluid communication between the second end of a respective riser reactor and a respective inlet of the separation zone. The apparatus also includes a catalyst retention zone provided to contain catalyst, which is fed to the riser reactors. A catalyst return is in fluid communication between the separation zone and the catalyst retention zone.

Multiple riser reactor with centralized catalyst return

The present invention is directed to a hydrocarbon conversion apparatus and process. The apparatus comprises the following: a plurality of riser reactors, each having a first end into which a catalyst is fed, a second end through which the catalyst can exit, and optionally a center axis extending therebetween. The apparatus also includes a separation zone having a plurality of inlets, each inlet not being oriented along the center axes of the riser reactors, the separation zone being provided to separate the catalyst from products of a reaction conducted in the hydrocarbon conversion apparatus. A plurality of deviating members are also provided, each deviating member being in fluid communication between the second end of a respective riser reactor and a respective inlet of the separation zone. The apparatus also includes a catalyst retention zone provided to contain catalyst, which is fed to the riser reactors. A catalyst return is in fluid communication between the separation zone and the catalyst retention zone.

Multiple riser reactor with centralized catalyst return

The present invention is directed to a hydrocarbon conversion apparatus and process. The apparatus comprises the following: a plurality of riser reactors, each having a first end into which a catalyst is fed, a second end through which the catalyst can exit, and optionally a center axis extending therebetween. The apparatus also includes a separation zone having a plurality of inlets, each inlet not being oriented along the center axes of the riser reactors, the separation zone being provided to separate the catalyst from products of a reaction conducted in the hydrocarbon conversion apparatus. A plurality of deviating members are also provided, each deviating member being in fluid communication between the second end of a respective riser reactor and a respective inlet of the separation zone. The apparatus also includes a catalyst retention zone provided to contain catalyst, which is fed to the riser reactors. A catalyst return is in fluid communication between the separation zone and the catalyst retention zone.

Selectively removing undesirably sized catalyst particles from a reaction system

The present invention provides various processes for selectively removing undesirably sized catalyst particles from a reaction system. In one embodiment, a plurality of catalyst particles, having a first median particle diameter, is withdrawn from the reaction system and is directed to a separation unit such as a counter flow cyclone separator. In the separation unit, the particles are separated into a small catalyst stream and a large catalyst stream, the small catalyst stream having a second median particle diameter less than the first median particle diameter, and the large catalyst stream having a third median particle diameter greater than the first median particle diameter. At least a portion of the small or large catalyst stream is then directed back to the reaction system in order to maintain a desirable particle size distribution therein.

Fluidizing a population of catalyst particles having a low catalyst fines content

The present invention relates to processes for fluidizing a population of catalyst particles that are depleted of catalyst fines. In one embodiment, the process includes providing a plurality of catalyst particles in the reactor, wherein the catalyst particles have a d2 value of greater than about 40 microns. The catalyst particles are contacted with a fluidizing medium under conditions effective to cause the catalyst particles to behave in a fluidized manner and form a fluidized bed. The particles are contacted with one or more primary obstructing members while in the fluidized bed. By fluidizing the catalyst particles in this manner, the catalyst particles can be maintained at an axial gas Peclet number of from about 10 to about 20.

Fluidizing a population of catalyst particles having a low catalyst fines content

The present invention relates to processes for fluidizing a population of catalyst particles that are depleted of catalyst fines. In one embodiment, the process includes providing a plurality of catalyst particles in the reactor, wherein the catalyst particles have a d 2 value of greater than about 40 microns. The catalyst- particles are contacted with a fluidizing medium under conditions effective to cause the catalyst particles to behave in a fluidized manner and form a fluidized bed. The particles are contacted with one or more primary obstructing members while in the fluidized bed. By fluidizing the catalyst particles in this manner, the catalyst particles can be maintained at an axial gas Peclet number of from about 10 to about 20.

Fluidizing a population of catalyst particles having a low catalyst fines content

A process and apparatus for fluidizing a population of catalyst particles having a low catalyst fines content includes a fluidized bed reactor which includes a plurality of catalyst particles in the reactor wherein the catalyst particles having a d 2 value of greater than about 40 microns. The catalyst particles are contacted with a fluidizing medium under conditions to fluidize the particles, the reactor includes a continuous reaction zone and separation zone and the fluidized of the catalyst particles are situated within the reaction and both the reaction zone and the separation zone include obstructing members which obstruct the flow of particles such that the catalyst particles can be maintained at an axial gas Peclet number from about 10 to about 20.

Fluidizing a population of catalyst particles having a low catalyst fines content

The present invention relates to processes for fluidizing a population of catalyst particles that are depleted of catalyst fines. In one embodiment, the process includes providing a plurality of catalyst particles in the reactor, wherein the catalyst particles have a dvalue of greater than about 40 microns. The catalyst particles are contacted with a fluidizing medium under conditions effective to cause the catalyst particles to behave in a fluidized manner and form a fluidized bed. The particles are contacted with one or more primary obstructing members while in the fluidized bed. By fluidizing the catalyst particles in this manner, the catalyst particles can be maintained at an axial gas Peclet number of from about 10 to about 20.

Fluidizing A Population of Catalyst Particles Having A Low Catalyst Fines Content

The present invention relates to processes for fluidizing a population of catalyst particles that are depleted of catalyst fines. In one embodiment, the process includes providing a plurality of catalyst particles in the reactor, wherein the catalyst particles have a d 2 value of greater than about 40 microns. The catalyst particles are contacted with a fluidizing medium under conditions effective to cause the catalyst particles to behave in a fluidized manner and form a fluidized bed. The particles are contacted with one or more primary obstructing members while in the fluidized bed. By fluidizing the catalyst particles in this manner, the catalyst particles can be maintained at an axial gas Peclet number of from about 10 to about 20.

Fluidizing a population of catalyst particles having a low catalyst fines content

The present invention relates to processes for fluidizing a population of catalyst particles that are depleted of catalyst fines. In one embodiment, the process includes providing a plurality of catalyst particles in the reactor, wherein the catalyst particles have a d 2 value of greater than about 40 microns. The catalyst- particles are contacted with a fluidizing medium under conditions effective to cause the catalyst particles to behave in a fluidized manner and form a fluidized bed. The particles are contacted with one or more primary obstructing members while in the fluidized bed. By fluidizing the catalyst particles in this manner, the catalyst particles can be maintained at an axial gas Peclet number of from about 10 to about 20.

Low metal content catalyst compositions and processes for making and using same

The invention provides low metal content molecular sieve catalyst compositions, processes for making such catalysts, and processes for using such catalysts in the conversion of an oxygenate into one or more light olefins. Preferably, the catalyst composition comprises a matrix material having a low metal content. By utilizing matrix materials having low metal contents, the amount of metal-catalyzed side reaction byproducts formed in a reaction system, particularly in an oxygenate-to-olefin reaction system, can be advantageously reduced.

Method of transferring catalyst in a reaction system

The invention is directed to methods of transfering catalyst particles into and within reaction systems. The reaction systems are those that use catalysts that comprise molecular sieves, particularly metalloaluminophosphate molecular sieves, especially metalloaluminophosphate molecular sieves which are susceptible to loss of catalytic activity due to contact with water molecules. The transfer methods provide appropriate mechanisms for transporting catalyst into and within a reactor to protect against loss of catalytic activity that can occur due to contact with water molecules.

Method of transferring catalyst in a reaction system

The invention is directed to methods of transfering catalyst particles into and within reaction systems. The reaction systems are those that use catalysts that comprise molecular sieves, particularly metalloaluminophosphate molecular sieves, especially metalloaluminophosphate molecular sieves which are susceptible to loss of catalytic activity due to contact with water molecules. The transfer methods provide appropriate mechanisms for transporting catalyst into and within a reactor to protect against loss of catalytic activity that can occur due to contact with water molecules.

Plant and method of producing medium distillate and lower olefins from hydrocarbon raw stock

FIELD: oil-and-gas production. SUBSTANCE: invention relates to petrochemical industry. Proposed method comprises the following stages: catalytic cracking of raw gas oil in the zone of vertical reactor of fluidised catalytic cracking (FCC) by bringing in contact said gas oil with first catalyst at 400-600°C to produce product of said vertical reactor. Said product is separated into gas oil cracking product and first used catalyst. It comprises also bringing intermediate reactor raw stock containing, at least, a portion of gas oil cracking product with second catalyst in intermediate cracking reactor at 482-871°C to produce intermediate reactor product containing, at least, one compound of lower olefin and second used catalyst. Besides, it includes separating said intermediate reactor cracking product to produce lower olefin product containing, at least, one compound of said olefin wherein raw stock of intermediate reactor containing, at least, one compound selected from fat acid and fat acid ester. EFFECT: higher conversion into lower olefins. 11 cl, 2 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 452 762 (13) C2 (51) МПК C10G 11/18 (2006.01) C10G 3/00 (2006.01) C10G 51/06 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ Приоритет(ы): (30) Конвенционный приоритет: 13.04.2007 US 60/911,715 (73) Патентообладатель(и): ШЕЛЛ ИНТЕРНЭШНЛ РИСЕРЧ МААТСХАППИЙ Б.В. (NL) (43) Дата публикации заявки: 20.05.2011 Бюл. № 14 (56) Список документов, цитированных в отчете о поиске: WO 2006020547 А1, 23.02.2006. US 3974062 А, 10.08.1976. US 3894933 А, 15.07.1975. US 5944982 А, 31.08.1999. US 3748251 А, 24.07.1973. US 6767451 B2, 27.07.2004. US 3928172 A, 23.12.1975. ЕР 0325437 A2, 18.01.1989. US 4830728 A, 16.05.1989. NL 8700587 A, 03.10.1988. US 20050003957 A1, 06.01.2005. EA 7055 В1, 30.06.2006. SU 408960 A, 15.06.1979. RU 2202592 C1, 20.04.2003. C 2 C 2 2 4 5 2 7 6 2 (45) Опубликовано: 10.06.2012 Бюл. № 16 R U 2 4 5 2 7 6 2 (85) Дата начала ...

Способы и устройства для обработки топлива для повышения качества потока пиролизного масла и углеводородного потока

1. Способ повышения качества потока пиролизного масла и углеводородного потока, который включает стадии:раздельного введения потока пиролизного масла и углеводородного потока в реакционную зону для формирования смеси потока пиролизного масла и углеводородного потока в реакционной зоне;каталитического крекинга смеси потока пиролизного масла и углеводородного потока в присутствии частиц катализатора крекинга в реакционной зоне; иподдержание потока пиролизного масла при температуре ниже или равной 100°C по существу до введения в реакционную зону.2. Способ по п. 1, в котором поддержание потока пиролизного масла при температуре ниже или равной 100°C включает активное охлаждение потока пиролизного масла.3. Способ по п. 2, в котором поток пиролизного масла активно охлаждают по существу вплоть до введения потока пиролизного масла в реакционную зону.4. Способ по п. 2, в котором активное охлаждение потока пиролизного масла включает внешнее охлаждение потока пиролизного масла внешней охлаждающей средой.5. Способ по п. 1, в котором углеводородный поток вводят в реакционную зону при температуре более высокой, чем температура потока пиролизного масла.6. Способ по п. 1, в котором углеводородный поток вводят в реакционную зону выше по потоку, чем поток пиролизного масла.7. Способ по п. 1, дополнительно включающий пиролиз потока биомассы для получения потока пиролизного масла.8. Способ по п. 7, в котором поток пиролизного масла, полученный пиролизом биомассы, вводят в реакционную зону без промежуточного повышения качества потока пиролизного масла.9. Способ повышения качества потока пиролизного масла и углеводородного потока в установке крекинга с псевдоожиженным

脂肪醇制备液体燃料的方法

一种脂肪醇制备液体燃料的方法，包括如下步骤：(1)在塔式反应器中，非均相酸催化剂催化脂肪醇至少发生脱水反应，液相产物(A)从塔底分出，而裂解气与水一起从塔顶分出；(2)所述液相产物(A)催化加氢制备适度饱和的液体燃料该方法具有如下特点：工艺流程简单，原料适应性强，催化剂廉价易得，氢气消耗低，液体燃料产率高。

Pretreating a catalyst containing molecular sieve and active metal oxide

This invention relates to processes for converting oxygenates to olefins that include a step of pretreating catalyst, which comprises molecular sieve and one or more active metal oxides of one or more metals, with a hydrocarbon composition to provide an integrated hydrocarbon co-catalyst within the molecular sieve. The combination of molecular sieve and hydrocarbon co-catalyst converts oxygenate to an olefin product with high selectivity to light olefins (i.e., ethylene or propylene, or mixture thereof).

使催化剂细粉末含量低的全体催化剂颗粒流态化

本发明涉及用于使催化剂细粉末贫化的全体催化剂颗粒流态化的方法。在一种实施方案中，所述方法包括在反应器中提供多个催化剂颗粒，其中所述催化剂颗粒具有大于约40μm的d 2 值。在有效使所述催化剂颗粒表现出流化行为和形成流化床的条件下，使催化剂颗粒与流化介质接触。在流化床中时，使所述颗粒与一个或多个初级阻隔构件接触。通过这种方式流化所述催化剂颗粒，可以使该催化剂颗粒保持在约10-约20的轴向气体Peclet数下。

甲醇和/或二甲醚催化转化制芳烃的方法

本发明涉及一种甲醇和/或二甲醚催化转化制芳烃的方法，主要解决现有技术中芳烃收率低、催化剂水热失活严重的问题。本发明通过甲醇和/或二甲醚原料进入流化床反应器和改性ZSM‑5催化剂接触反应得到包含芳烃的产物和待生催化剂，待生催化剂进入第一再生器和再生介质Ⅰ接触烧焦得到半再生催化剂和一再烟气，半再生催化剂进入脱气罐的脱气罐Ⅰ区和脱气介质Ⅰ接触得到脱气后半再生催化剂，脱气后半再生催化剂进入第二再生器和再生介质Ⅱ接触继续烧焦得到再生催化剂和二再烟气，再生催化剂进入脱气罐的脱气罐Ⅱ区和脱气介质Ⅱ接触得到脱气后再生催化剂，脱气后再生催化剂返回流化床反应器，较好地解决了该问题，可用于芳烃工业生产中。

SYNTHESIS OF FISHER-TROPSHA

Способ (10) синтеза продуктов (20) Фишера-Тропша предусматривает подачу синтез-газа (30) в реактор (16) синтеза Фишера-Тропша с подвижным слоем, содержащий катализатор синтеза Фишера-Тропша в подвижном слое катализатора, и каталитическое превращение по меньшей мере части синтез-газа (30) в подвижном слое катализатора в продукты (20) Фишера-Тропша. Продукты (20) Фишера-Тропша отводят из реактора (16) синтеза Фишера-Тропша с подвижным слоем. Способ (10) также предусматривает, когда реактор синтеза Фишера-Тропша с подвижным слоем (16) находится в рабочем режиме, извлечение части (50) катализатора синтеза Фишера-Тропша из реактора (16) синтеза Фишера-Тропша с подвижным слоем, добавление реактивированного катализатора (57, 58) синтеза Фишера-Тропша в реактор (16) синтеза Фишера-Тропша с подвижным слоем и добавление свежего катализатора (60, 58) синтеза Фишера-Тропша, в дополнение к реактивированному катализатору (57,58), в реактор (16) синтеза Фишера-Тропша с подвижным слоем. The method (10) of the synthesis of products (20) of Fischer-Tropsch provides for the supply of synthesis gas (30) to the reactor (16) of the Fischer-Tropsch synthesis with a moving layer, containing a catalyst for the Fischer-Tropsch synthesis in the moving bed of catalyst, and catalytic conversion of at least parts of the synthesis gas (30) in the moving catalyst bed in the products (20) Fischer-Tropsch. Products (20) Fischer-Tropsch withdrawn from the reactor (16) Fischer-Tropsch synthesis with a moving layer. Method (10) also provides, when the moving-bed Fisher-Tropsch synthesis reactor (16) is in operation, removing part (50) of the Fischer-Tropsch synthesis catalyst from the moving-bed Fisher-Tropsch synthesis reactor (16), adding reactive catalyst (57, 58) of the Fischer-Tropsch synthesis to the reactor (16) of the Fischer-Tropsch synthesis with a moving bed and the addition of fresh catalyst (60, 58) of the Fischer-Tropsch synthesis, in addition to the reactivated catalyst (57,58), to the ...

NEW REACTOR WITH TWO REACTIONAL ZONES FLUIDIZED WITH INTEGRATED GAS / SOLID SEPARATION SYSTEM

Method for making biofuels and biolubricants

A process for producing biofuels and biolubricants from lipid material includes reacting lipid material with a motive fluid in a reactor. The reactor may be configured to cause a high energy collision between the motive fluid and the lipid material that facilitates the reactions that result in biofuels and biolubricants. A heavy fraction of the effluent may be repeatedly recycled back through the reactor until most, if not all, of the lipid material has been converted.

Methods and fuel processing apparatuses for upgrading a pyrolysis oil stream and a hydrocarbon stream

Methods and apparatuses for upgrading a pyrolysis oil stream and a hydrocarbon stream are provided herein. In an embodiment, a method for upgrading a pyrolysis oil stream and a hydrocarbon stream includes separately introducing the pyrolysis oil stream and the hydrocarbon stream into a reaction zone to form a mixture of the pyrolysis oil stream and the hydrocarbon stream in the reaction zone. The mixture of the pyrolysis oil stream and the hydrocarbon stream is catalytically cracked in the presence of a particulate cracking catalyst in the reaction zone. The pyrolysis oil stream is maintained at a temperature of less than or equal to about 100° C. substantially up to introduction into the reaction zone.

Making an olefin product from an oxygenate

본 발명은 산소화물 함유 공급원료로부터 올레핀 생성물을 제조하는 방법을 개시한다. 상기 방법에서, 실리코알루미노포스페이트 분자체 촉매를 1.0 이상의 평균 촉매 공급원료 노출 지수로 반응기 중의 산소화물 함유 공급원료와 접촉시킨다. 상기 방법은 보다 낮은 수율로 코크스를 생성시키고 C 1 -C 4 파라핀 함량이 낮은 올레핀 생성물을 제공한다. 본 발명은 프로판 함량이 매우 낮은 올레핀 생성물의 제조에 특히 유효하다. The present invention discloses a process for preparing olefin products from oxygenate containing feedstocks. In this process, the silicoaluminophosphate molecular sieve catalyst is contacted with an oxygenate containing feedstock in the reactor with an average catalyst feedstock exposure index of at least 1.0. The process produces coke in lower yields and provides olefin products with a lower C 1 -C 4 paraffin content. The invention is particularly effective for the production of olefin products with very low propane content.

分子筛催化剂组合物，其制备和在转化方法中的用途

本发明涉及分子筛催化剂组合物、制备或形成分子筛催化剂组合物的方法、和使用催化剂组合物的转化方法。尤其是，本发明涉及：在分子筛的存在下，其在絮凝剂的存在下合成，由原料优选含有含氧化合物的原料来制备烯烃优选乙烯和/或丙烯的转化方法。

Systems and methods for making a middle distillate product and lower olefins from a hydrocarbon feedstock

A system comprising a riser reactor comprising a gas oil feedstock and a first catalyst under catalytic cracking conditions to yield a riser reactor product comprising a cracked gas oil product and a first used catalyst; a intermediate reactor comprising at least a portion of the cracked gas oil product and a second catalyst under high severity conditions to yield a cracked intermediate reactor product and a second used catalyst; wherein the intermediate reactor feedstock comprises at least one of a fatty acid and a fatty acid ester.

Systems and methods for making a middle distillate product and lower olefins from a hydrocarbon feedstock

A system comprising a riser reactor comprising a gas oil feedstock and a first catalyst under catalytic cracking conditions to yield a riser reactor product comprising a cracked gas oil product and a first used catalyst; a intermediate reactor comprising at least a portion of the cracked gas oil product and a second catalyst under high severity conditions to yield a cracked intermediate reactor product and a second used catalyst; wherein the intermediate reactor feedstock comprises at least one of a fatty acid and a fatty acid ester.

Production of diesel fuel from biorenewable feedstocks using non-flashing quench liquid

A process has been developed for producing diesel boiling range fuel from renewable feedstocks such as plant oils and animal oils, fats, and greases. The process involves treating a renewable feedstock by hydrogenating and deoxygenating to provide a hydrocarbon fraction useful as a diesel or aviation boiling range fuel or fuel blending component. If desired, the hydrocarbon fraction can be isomerized to improve cold flow properties. A portion of the hydrogenated and deoxygenated feedstock is used as a non-flashing liquid quench stream to control the temperature of the hydrogenation and deoxygenation reactor.

Catalytic process for the preparation of light olefins from methanol in a fluidised bed reactor

Method for converting oxygenates to olefins

본 발명은 산소화물 함유 공급물을 올레핀으로 전환하는 방법으로서, 산소화물 함유 공급물을 제공하는 단계; 공급물을 반응기 장치에서 분자체 함유 촉매와 접촉시키고, 이때 이러한 접촉이 산소화물을 경질 올레핀 함유 생성물로 전환하기에 효과적인 조건하에 일어나고 이러한 조건이 반응 영역의 하나 이상의 지점에서 초 당 2 미터 이상의 기체의 겉보기 속도를 포함하는 단계; 및 촉매의 제 1 부분을 재순환시켜 공급물과 재접촉시키는 단계를 포함한다. The present invention provides a method of converting an oxygenate containing feed to an olefin, comprising the steps of: providing an oxygenate containing feed; The feed is contacted with a molecular sieve containing catalyst in a reactor apparatus, where such contacting occurs under conditions effective to convert the oxygenate to a light olefin containing product and such conditions occur at least two meters of gas per second at one or more points in the reaction zone. Including an apparent velocity; And recycling the first portion of the catalyst to recontact the feed.

用于由烃原料生产中间馏分油产物和低级烯烃的系统和方法

一种系统，其包括：提升管反应器，用于在催化裂化条件下使粗柴油原料与催化裂化催化剂接触，以获得包含裂化粗柴油产物和废裂化催化剂的提升管反应器产物；分离器，用于将所述提升管反应器产物分离成所述裂化粗柴油产物和所述废裂化催化剂；再生器，用于再生所述废裂化催化剂，以获得再生催化剂；中间反应器，用于在高苛刻度条件下使汽油原料与所述再生催化剂接触，以获得裂化汽油产物和用过的再生催化剂；第一导管，其连接至中间反应器和提升管反应器，第一导管用于将用过的再生催化剂送至提升管反应器以用作催化裂化催化剂；和第二导管，其连接至中间反应器和再生器，第二导管用于将用过的再生催化剂送至再生器以获得再生催化剂。

Method of converting olefin or alcohol and method of producing propylene or aromatic compound

FIELD: chemistry. SUBSTANCE: invention relates to a method of converting olefin or alcohol and a method of producing propylene or an aromatic compound. Method of converting olefin or alcohol involves the stage of preliminary treatment, in which a conducting catalyst is obtained by loading a reactor with a fluidized bed with a non-conducting catalyst containing zeolite and/or silicon oxide and feeding a heated hydrocarbon gas into the reactor with the fluidized bed for deposition of carbonaceous coke and its application of the non-conducting catalyst, and the stage of conversion of olefin or alcohol with the help of a reaction in the fluidized bed using the said conducting catalyst, where the gas feeding rate makes 0.40 m/sec or less at the stage of preliminary treatment in the form of the gas flow rate in the fluidized bed reactor, and the gas feeding rate is 0.5 m/sec or more at the stage of conversion of olefin or alcohol in the form of the gas flow rate in the fluidized bed reactor. EFFECT: invention provides suppression of electrostatic charging of the catalyst and high efficiency of the reaction. 7 cl, 9 dwg, 1 tbl, 4 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 599 749 C2 (51) МПК B01J 8/24 (2006.01) B01J 29/00 (2006.01) C07C 2/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2015103122/05, 09.08.2013 (24) Дата начала отсчета срока действия патента: 09.08.2013 (72) Автор(ы): ИИЦУКА Такехиро (JP), ТАКАМАЦУ Йосиказу (JP) 10.08.2012 JP 2012-178398 (43) Дата публикации заявки: 27.09.2016 Бюл. № 27 R U (73) Патентообладатель(и): АСАХИ КАСЕИ КЕМИКАЛЗ КОРПОРЕЙШН (JP) Приоритет(ы): (30) Конвенционный приоритет: (45) Опубликовано: 10.10.2016 Бюл. № 28 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 10.03.2015 (86) Заявка PCT: 2 5 9 9 7 4 9 (56) Список документов, цитированных в отчете о поиске: JP 2004-345972 A, 09.12.2004. JP 0291030 A, 30.03.1990. JP 2012-120978 A, 28.06.2012. RU ...

Method for converting oxygenates to olefins

菱沸石型分子筛、其合成及其在含氧化合物转化成烯烃中的应用

一种结晶材料，该结晶材料基本上不含有骨架磷而且包含有堆垛层错或至少一个CHA骨架类型分子筛与AEI骨架类型分子筛共生相的CHA骨架类型分子筛，其中所述材料在其焙烧、无水形式的组成包括以下摩尔关系：(n)X 2 O 3 :YO 2 ，其中X为三价元素；Y为四价元素；和n为0至约0.5。该材料在甲醇至低级烯烃尤其是乙烯和丙烯的转化中表现出活性和选择性。

Molecular sieve compositions, catalysts thereof, their making and use in conversion processes

The invention relates to a conversion process of a feedstock, preferably an oxygenated feedstock, into one or more olefin(s), preferably ethylene and/or propylene, in the presence of a molecular sieve catalyst composition that includes a molecular sieve and a Group 3 metal oxide and/or an oxide of a Lanthanide or Actinide series element. The invention is also directed to methods of making and formulating the molecular sieve catalyst composition useful in a conversion process of a feedstock into one or more olefin(s).

Molecular sieve compositions, catalysts thereof, their making and use in conversion processes

The invention relates to a conversion process of a feedstock, preferably an oxygenated feedstock, into one or more olefin(s), preferably ethylene and/or propylene, in the presence of a molecular sieve catalyst composition that includes a molecular sieve and a Group 3 metal oxide and/or an oxide of a Lanthanide or Actinide series element. The invention is also directed to methods of making and formulating the molecular sieve catalyst composition useful in a conversion process of a feedstock into one or more olefin(s).

Method for regenerating hydrogenation catalyst

Disclosed is a method for regenerating a hydrogenation catalyst. More specifically, disclosed is a method for regenerating a hydrogenation catalyst poisoned during hydrogenation of a hydroformylation product for preparation of alcohol by stopping hydrogenation in a hydrogenation stationary phase reactor in which the hydrogenation catalyst is set and flowing hydrogen gas under a high temperature normal pressure. The method has an effect in that the poisoned hydrogenation catalyst can be efficiently recovered through a simple process.

Removal of oxygenate from an olefin stream

This invention is to a process for removing dimethyl ether from an olefin stream. The process includes contacting the olefin stream with a molecular sieve that has improved capacity to adsorb the dimethyl ether from the olefin stream. The molecular sieve used to remove the dimethyl ether has low or no activity in converting the olefin in the olefin stream to other products.

Removal of oxygenate from an olefin stream

This invention is to a process for removing dimethyl ether from an olefin stream. The process includes contacting the olefin stream with a molecular sieve that has improved capacity to adsorb the dimethyl ether from the olefin stream. The molecular sieve used to remove the dimethyl ether has low or no activity in converting the olefin in the olefin stream to other products.

Molecular sieve compositions, catalysts thereof, their making and use in conversion processes

The invention relates to a conversion process of a feedstock, preferably an oxygenated feedstock, into one or more olefin(s), preferably ethylene and/or propylene, in the presence of a molecular sieve catalyst composition that includes a molecular sieve and a Group 3 metal oxide and/or an oxide of a Lanthanide or Actinide series element. The invention is also directed to methods of making and formulating the molecular sieve catalyst composition useful in a conversion process of a feedstock into one or more olefin(s).

Making an olefin product from an oxygenate

多提升管反应器

本发明涉及一种烃转化装置。该装置包括：多个提升管反应器，每个提升管反应器都具有可送入催化剂的第一端和可使催化剂离开提升管反应器的第二端；分离区，提升管反应器的所述第二端插入其中，分离区用来将催化剂与在烃转化装置中进行反应的产品分离；与分离区和提升管反应器的第一端流体连通的至少一个催化剂回路，催化剂回路用来将催化剂从分离区输送到提升管反应器的第一端。

Patent JPH0240379B2

Method of producing benzines or concentrates of aromatic compounds with different distribution of oxygenate and olefin-containing streams

FIELD: chemistry. SUBSTANCE: invention relates to a method of producing benzines or concentrates of aromatic compounds, in which the raw material used is three streams, one of which includes a hydrocarbon fraction, the second stream includes an oxygenate, third stream contains an olefin-containing fraction containing one or more olefins selected from a group comprising: ethylene, propylene, normal butylenes, isobutylene in total amount of 10 to 50 wt%, and where three reaction zones are used, filled with zeolite catalyst, with distribution of hydrocarbon fraction preferably into first reaction zone, with distribution of oxygenate into first reaction zone and with distribution of olefin-containing fraction by three reaction zones, note here that mass fraction of third flow distributed into last reaction zone is higher than mass fraction of third flow distributed into each of previous reaction zones. EFFECT: method increases output of C 5+ hydrocarbons, increases conversion of n-hexane and n-heptane, reduces content of benzene in the product, eliminates recycling of gaseous products, and reduces consumption of oxygenates. 36 cl, 7 tbl, 12 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 747 869 C1 (51) МПК C10G 35/095 (2006.01) C10G 3/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК C10G 35/095 (2020.08); C10G 3/00 (2020.08); C10G 3/49 (2020.08); C10G 3/60 (2020.08) (21)(22) Заявка: 2020121543, 29.06.2020 (24) Дата начала отсчета срока действия патента: Дата регистрации: 17.05.2021 (45) Опубликовано: 17.05.2021 Бюл. № 14 Адрес для переписки: 121205, Москва, территория инновационного центра "Сколково", ул. Луговая, 4, ООО "ЦИС "Сколково", Котлов Дмитрий Владимирович 2 7 4 7 8 6 9 C 1 (56) Список документов, цитированных в отчете о поиске: WO 2017155431 A1, 14.09.2017. RU 2671568 C1, 02.11.2018. CN 206751740 U, 15.12.2017. (54) СПОСОБ ПОЛУЧЕНИЯ БЕНЗИНОВ ИЛИ КОНЦЕНТРАТОВ АРОМАТИЧЕСКИХ СОЕДИНЕНИЙ С РАЗЛИЧНЫМ ...

Biomass hydrolysis for obtaining high-quality liquid fuels

FIELD: chemistry.SUBSTANCE: invention relates to versions of methods for obtaining liquid products from biomass. Method includes the following stages: a) biomass hydrolysis in reactor hydrolysis reservoir, containing molecular hydrogen and deoxigenation catalyst to obtain product, containing CO, CO and C-Cgas, partially deoxygenated hydrolysis product and charcoal, at hydrolysis reactor output; b) removal of said charcoal from said partially deoxygenated hydrolysis product; c) hydroconversion of said partially deoxygenated hydrolysis product in reactor hydroconversion reservoir with application of hydroconversion catalyst in presence of CO, CO and C-Cgas, generated at step a), to obtain in fact fully deoxygenated hydrocarbon liquid and gas mixture, containing CO, COand light hydrocarbon gases (C-C), d) steam reforming of, at least, part of said gas mixture to obtain molecular hydrogen of reforming and e) introduction of said molecular hydrogen of reforming into said reactor reservoir for said biomass hydrolysis. Steps a) and c) function under conditions, in which approximately 30-70% of oxygen in said biomass are converted into HO and approximately 30-70% of said oxygen are converted into CO and CO.EFFECT: method makes it possible to maximise output with simultaneous preservation of high degree of oxygen removal.44 cl, 8 dwg, 1 tbl РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 539 598 C2 (51) МПК C07C 1/00 (2006.01) C10G 1/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2011144864/04, 05.04.2010 (24) Дата начала отсчета срока действия патента: 05.04.2010 Приоритет(ы): (30) Конвенционный приоритет: (72) Автор(ы): МАРКЕР Терри Л. (US), ФЕЛИКС Ларри Дж. (US), ЛИНК Мартин Б. (US) 07.04.2009 US 12/419,535; 11.01.2010 US 12/685,352 R U (73) Патентообладатель(и): ГЭЗ ТЕКНОЛОДЖИ ИНСТИТЬЮТ (US) (43) Дата публикации заявки: 20.05.2013 Бюл. № 14 2 5 3 9 5 9 8 (45) Опубликовано: 20.01.2015 Бюл. № 2 (56) Список ...

Method for hydroprocessing renewable materials with optimized gas recycle

本发明涉及加氢处理获自可再生来源的进料的方法，其中将进料总物流F分成等于催化区数n的多个不同的进料的部分物流F1至Fn，其中n为1‑10的整数，送至第一催化区的氢气的质量流量占加氢处理方法中所用氢气的总质量流量的超过80wt％以在反应器出口产生至少一种含链烷烃的流出物，获自步骤a)的所述流出物经历至少一个分离步骤，将至少一部分含链烷烃的所述液体馏分以如下方式再循环到第一催化区和下面的催化区：各床的局部再循环比率即所述液体再循环馏分的物流和引入催化区的进料的部分物流Fn的重量比为2或更小，各床的局部稀释比率即引入催化区n的液体和气体物流量与引入该催化区的进料的部分物流Fn的重量比为小于4。

Conversion of oxygenates to olefins

A process is described for converting an oxygenate-containing feedstock into one or more olefins in which the feedstock is contacted in a reaction zone with a fluidized bed of a particulate catalyst composition comprising a molecular sieve and at least one metal oxide having an uptake of carbon dioxide at 100° C. of at least 0.03 mg/m 2 of the metal oxide whereby at least part of the feedstock is converted into a product stream comprising one or more olefins and a carbonaceous material is deposited on the catalyst composition to produce a coked catalyst composition. The coked catalyst composition is separated from the product stream and divided into at least first and second portions. The first portion of the coked catalyst composition is contacted with a regeneration medium in a regeneration zone under conditions to remove at least part of the carbonaceous material from the coked catalyst composition and produce a regenerated catalyst composition, which is subsequently recycled to the reaction zone. The second portion of the coked catalyst composition is also recycled to the reaction zone but without being initially contacted with a regeneration medium.

Heat removal and recovery in biomass pyrolysis

Pyrolysis methods and apparatuses that allow effective heat removal, for example when necessary to achieve a desired throughput or process a desired type of biomass, are disclosed. According to representative methods, the use of a quench medium (e.g., water), either as a primary or a secondary type of heat removal, allows greater control of process temperatures, particularly in the reheater where char, as a solid byproduct of pyrolysis, is combusted. Quench medium may be distributed to one or more locations within the reheater vessel, such as above and/or within a dense phase bed of fluidized particles of a solid heat carrier (e.g., sand) to better control heat removal.

Heat removal and recovery in biomass pyrolysis

Pyrolysis methods and apparatuses that allow effective heat removal, for example when necessary to achieve a desired throughput or process a desired type of biomass, are disclosed. According to representative methods, the use of a quench medium (e.g., water), either as a primary or a secondary type of heat removal, allows greater control of process temperatures, particularly in the reheater where char, as a solid byproduct of pyrolysis, is combusted. Quench medium may be distributed to one or more locations within the reheater vessel, such as above and/or within a dense phase bed of fluidized particles of a solid heat carrier (e.g., sand) to better control heat removal.

Catalyst for oxygen devices cooling substances conversion reactor.

Procédé de conversion de substances oxygénées en oléfines légères, comprenant une mise en contact d'un courant d'alimentation de substance oxygénée avec un catalyseur et une conversion dudit courant en oléfines légères, tout en épuisant ledit catalyseur, une régénération d'une première partie du catalyseur épuisé et un retour de celle-ci pour entrer en contact avec ledit courant d'alimentation et un refroidissement d'une seconde partie dudit catalyseur épuisé dans un dispositif de refroidissemsent, une introduction d'un fluide échangeur de chaleur dans le dispositif de refroidissement à proximité de son sommet, et un retour de la dite seconde partie dudit catalyseur épuisé pour entrer en contact avec ledit courant d'alimentation de substance oxygénée. A process for converting oxygenated substances into light olefins, comprising contacting an oxygenated feed stream with a catalyst and converting said stream to light olefins, while exhausting said catalyst, regenerating a first portion spent catalyst and a return thereto for contacting said feed stream and cooling a second portion of said spent catalyst in a cooler, introducing a heat exchanging fluid into the feed device; cooling near its top, and a return of said second portion of said spent catalyst to contact said oxygenated feed stream.

Method for converting oxygenates to olefins

本发明提供了用于将含有含氧化合物的原料转化为烯烃的方法，所述方法包括以下步骤：提供包括含氧化合物的原料；使该原料在反应器装置中与包括分子筛的催化剂接触，该接触在有效将含氧化合物转化为包括轻烯烃的产物的条件下进行，所述条件包括在反应区的至少一个位置上至少2米/秒的气体表观速度；和将第一部分的催化剂再循环以重接触原料。

Method of treating biomass, fuel for fuel cell, gasoline, diesel fuel, liquefied petroleum gas, and synthetic resin

在使用具有反应带、分离带、汽提带和再生带的流化催化裂化装置，通过催化裂化处理生物质时，在反应带中，用含有10～50质量％超稳定Y型沸石的催化剂，在反应带出口温度为580～680℃、催化剂/油比率为10～40wt/wt、反应压力为1～3kg/cm 2 G和反应带中的原料油与催化剂的接触时间为0.1～1.0秒的条件下处理含有生物质的原料油，然后，在再生带中，在再生带温度为640～720℃、再生带压力为1～3kg/cm 2 G和再生带出口处的废气中的氧气浓度为0～3mol％的条件下处理催化剂。

Production of paraffinic fuel from renewable feedstocks

A process has been developed for producing fuel from renewable feedstocks such as plant and animal oils and greases. The process involves treating a first portion of a renewable feedstock by hydrogenating and deoxygenating in a first reaction zone and a second portion of a renewable feedstock by hydrogenating and deoxygenating in a second reaction zone to provide a diesel boiling point range fuel hydrocarbon product. If desired, the hydrocarbon product can be isomerized to improve cold flow properties. A portion of the hydrocarbon product is recycled to the first reaction zone to increase the hydrogen solubility of the reaction mixture.

Reducing hydrogen consumption in hydrotreating of biocomponent feeds

Processes are provided for deoxygenation of a biocomponent feedstock with reduced hydrogen consumption. The biocomponent feedstock can be processed under relatively low hydrogen partial pressures and at a relatively low treat gas ratio compared to the hydrogen need of the feedstock. The relatively low pressure, relatively low treat gas ratio hydroprocessing can result in reduced production of water and carbon monoxide and in increased production of carbon dioxide compared to relatively higher pressure process conditions.

Reducing hydrogen consumption in hydrotreating of biocomponent feeds

Processes are provided for deoxygenation of a biocomponent feedstock with reduced hydrogen consumption. The biocomponent feedstock can be processed under relatively low hydrogen partial pressures and at a relatively low treat gas ratio compared to the hydrogen need of the feedstock. The relatively low pressure, relatively low treat gas ratio hydroprocessing can result in reduced production of water and carbon monoxide and in increased production of carbon dioxide compared to relatively higher pressure process conditions.

Fischer-tropsch synthesis

A method (10) of synthesising Fischer-Tropsch products (20) includes feeding a synthesis gas (30) to a moving-bed Fischer-Tropsch synthesis reactor (16) containing a Fischer-Tropsch catalyst in a moving catalyst bed and catalytically converting at least a portion of the synthesis gas (30) in the moving catalyst bed to Fischer-Tropsch products (20). The Fischer-Tropsch products (20) are removed from the moving-bed Fischer- Tropsch synthesis reactor (16). The method (10) further includes, while the moving-bed Fisher-Tropsch synthesis reactor (16) is on-line, withdrawing a portion (50) of the Fischer-Tropsch catalyst from the moving-bed Fischer-Tropsch synthesis reactor (16), adding a reactivated Fischer-Tropsch catalyst (57, 58) to the moving-bed Fischer- Tropsch synthesis reactor (16), and adding a fresh Fischer-Tropsch catalyst (60,58), in addition to the reactivated catalyst (57,58), to the moving-bed Fischer-Tropsch synthesis reactor (16).