Device and method for controlling the conversion of biomass to biofuel

Embodiments presented herein describe an apparatus and method to control the conversion of carbonaceous materials, particularly biomass and those biomass resources, into a high performance solid fuel. This method, and the apparatus described as the means to accomplish this method, provides a process having a control system that enables the system to produce a fuel of uniform quality, even with a change in biomass supply.

Selective isomerization and oligomerization of olefin feedstocks for the production of turbine and diesel fuels

A process from converting alcohol feedstock to diesel/turbine fuels.

Process for hydrotreating naphtha fraction and process for producing hydrocarbon oil

A process for hydrotreating a naphtha fraction that includes a step of estimating the difference between the naphtha fraction hydrotreating reactor outlet temperature and inlet temperature, based on the reaction temperature of the Fischer-Tropsch synthesis reaction and the ratio of the flow rate of the treated naphtha fraction returned to the naphtha fraction hydrotreating step relative to the flow rate of the treated naphtha fraction discharged from the naphtha fraction hydrotreating step, a step of measuring the difference between the naphtha fraction hydrotreating reactor outlet temperature and inlet temperature, and a step of adjusting the reaction temperature of the naphtha fraction hydrotreating step so that the measured difference between the naphtha fraction hydrotreating reactor outlet temperature and inlet temperature becomes substantially equal to the estimated difference between the naphtha fraction hydrotreating reactor outlet temperature and inlet temperature.

Method of producing monocyclic aromatic hydrocarbons

A method of producing monocyclic aromatic hydrocarbons includes bringing a feedstock oil having a 10 vol % distillation temperature of 140° C. or higher and a 90 vol % distillation temperature of 380° C. or lower, into contact with a catalyst for monocyclic aromatic hydrocarbon production containing a crystalline aluminosilicate, in which a content ratio of monocyclic naphthenobenzenes in the feedstock oil is adjusted to 10 mass % to 90 mass %, by mixing a hydrocarbon oil A having a 10 vol % distillation temperature of 140° C. or higher and a 90 vol % distillation temperature of 380° C. or lower with a hydrocarbon oil B containing more monocyclic naphthenobenzenes than the hydrocarbon oil A.

CHARACTERIZATION OF PRE-REFINED CRUDE DISTILLATE FRACTIONS

Methods are provided for qualifying jet fuel fractions that are derived at least in part from pre-refined crude oil sources. The methods allow for determination of the stability of a jet fuel product over time by using an accelerated aging test. The methods are beneficial for verifying the stability of a jet fuel fraction that includes a portion derived from a pre-refined crude oil. 1. A method for preparing a jet fuel or kerosene product , comprising:determining a breakpoint for a first sample of a distillate fraction, the distillate fraction having an initial boiling point of at least about 284° F. (140° C.) and a final boiling point of about 572° F. (300° C.) or less, at least a portion of the distillate fraction being derived from a first pre-refined crude oil;maintaining a second sample of the distillate fraction at a temperature of at least about 40° C. for an aging period;determining a breakpoint for the aged second sample of the distillate fraction, the breakpoint for the aged second sample being at least about 265° C.; andpreparing a jet fuel product comprising a kerosene portion derived from a second pre-refined crude oil, the second pre-refined crude oil being derived from the same source as the first pre-refined crude oil, a volume percentage of the kerosene portion derived from the second pre-refined crude in the jet fuel product being about 110% or less of a volume percentage corresponding to the portion of the distillate fraction derived from the first pre-refined crude oil, the initial boiling point of the jet fuel product being at least about the initial boiling point of the distillate fraction, and the final boiling point of the jet fuel product being less than or equal to the final boiling point of the distillate fraction.2. The method of claim 1 , further comprising:obtaining a portion of the distillate fraction; andsplitting the portion of the distillate fraction to form at least the first sample and the second sample.3. The method of claim 1 , ...

PRODUCTION OF UPGRADED EXTRACT AND RAFFINATE

Systems and methods are provided for producing upgraded raffinate and extract products from lubricant boiling range feeds and/or other feeds having a boiling range of 400° F. (204° C.) to 1500° F. (816° C.) or more. The upgraded raffinate and/or extract products can have a reduced or minimized concentration of sulfur, nitrogen, metals, or a combination thereof. The reduced or minimized concentration of sulfur, nitrogen, and/or metals can be achieved by hydrotreating a suitable feed under hydrotreatment conditions corresponding to relatively low levels of feed conversion. Optionally, the feed can also dewaxed, such as by catalytic dewaxing or by solvent dewaxing. Because excessive aromatic saturation is not desired, the pressure for hydrotreatment (and optional dewaxing) can be 500 psig (˜3.4 MPa) to 1200 psig (˜8.2 MPa). 1. A method for forming a raffinate and an extract , comprising:hydrotreating a feedstock having a T5 boiling point of at least 400° F. and a T95 boiling point of 1500° F. or less under hydrotreating conditions comprising less than 15% feed conversion relative to a conversion temperature of 700° F. to form a hydrotreated effluent, the feedstock having a 650° F.+ aromatics content of 25 wt % to 90 wt % and a sulfur content of greater than 1000 wppm, the hydrotreated effluent comprising a hydrotreated effluent fraction having a T5 boiling point of at least 400° F., an aromatics content of at least 10 wt %, a sulfur content of less than 1000 wppm, and a combined amount of Ni, V, and Fe of less than 10 wppm; andperforming a solvent extraction on the hydrotreated effluent fraction to form at least a raffinate product having a nitrogen content of less than 50 wppm and an extract product comprising at least 70 wt % aromatics.2. The method of claim 1 , wherein the raffinate product has a nitrogen content of 10 wppm or less.3. The method of claim 1 , further comprising dewaxing at least a portion of the hydrotreated effluent fraction prior to performing the ...

Process for producing benzene from a c5-c12 hydrocarbon mixture

The invention relates to a process for producing benzene, comprising the steps of: (a) providing a hydrocracking feed stream comprising C5-C12 hydrocarbons, (b) contacting the hydrocracking feed stream in the presence of hydrogen with a hydrocracking catalyst comprising 0.01-1 wt-% hydrogenation metal in relation to the total catalyst weight and a zeolite having a pore size of 5-8 Å and a silica (SiO 2 ) to alumina (Al 2 O 3 ) molar ratio of 5-200 under process conditions including a temperature of 425-580° C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 0.1-15 h −1 to produce a hydrocracking product stream comprising benzene, toluene and C8+ hydrocarbons, (c) separating benzene, toluene and the C8+ hydrocarbons from the hydrocracking product stream and (d) selectively recycling back at least part of the toluene from the separated products of step (c) to be included in the hydrocracking feed stream.

POWER RECOVERY FROM QUENCH AND DILUTION VAPOR STREAMS

A process for reducing pressure of a vapor stream used for reducing a temperature or pressure in a reactor. A pressure of a vapor stream is reduced with a turbine to provide a lower pressure vapor stream. The vapor stream rotates a turbine wheel within the turbine. The turbine wheel is configured to transmit rotational movement to an electrical generator. Thus, electricity is generated with the turbine. The lower pressure vapor stream is injected into a reactor and reduces a temperature in the reactor or reduces a partial pressure of a hydrocarbon vapor in the reactor. 1. A process comprising: reducing a pressure of the vapor stream with a turbine to provide a lower pressure vapor stream, wherein the vapor stream comprises hydrogen;', 'rotating a turbine wheel within the turbine; and,', 'injecting the lower pressure vapor stream into the reactor and reducing the temperature in the reactor, wherein the reactor comprises an FCC reactor, and wherein the vapor stream comprises a steam stream,, 'reducing an amount of a vapor stream used for reducing a temperature, or heat load, in a reactor relative to a control valve bywherein the reactor comprises an FCC reactor, and wherein the vapor stream comprises a steam stream.2. A process comprising: providing a vapor stream comprising steam;', 'passing the vapor stream through a turbine, the turbine comprising a turbine wheel within the turbine; and,', 'reducing a partial pressure of a hydrocarbon vapor by mixing the reduced pressure vapor stream with the hydrocarbon vapor., 'reducing pressure of a vapor stream used for adjusting a partial pressure of a hydrocarbon vapor by3. The process of claim 1 , wherein the reduced pressure vapor stream is injected into an FCC reactor to reduce the partial pressure of the hydrocarbon vapor in the FCC reactor.4. The process of further comprising:recovering electricity generated with the turbine.5. The process of further comprising:adjusting one or more process conditions for the FCC reactor ...

ALLOYED ZEOLITE CATALYST COMPONENT, METHOD FOR MAKING AND CATALYTIC APPLICATION THEREOF

The presently disclosed and claimed inventive concept(s) generally relates to a method of making a solid catalyst component comprising a zeolite with a modifier and at least one Group VIII metal alloyed with at least one transition metal and a process of converting mixed waste plastics into low molecular weight organic compounds using the solid catalyst component. The process of converting mixed waste plastics into low molecular weight organic compounds may employ the use of a non-thermal catalytic plasma reactor, which may be configured as a fluid bed reactor or fixed bed reactor. 113.-. (canceled)14. A process of converting a mixed waste plastic into a low molecular weight organic compound , comprising the steps of(a) feeding particles of the mixed waste plastic, plasma, and a solid catalyst component into a non-thermal catalytic plasma reactor, the solid catalyst component comprising (i) a modified zeolite and (ii) alloyed metals into a fluidized bed reactor;(b) heating the particles of the mixed waste plastic and the solid catalyst component at a temperature effective to produce a coarse filler, inorganic components, coke, a volatile organic component, and a spent catalyst component;(c) withdrawing a first stream comprising the volatile organic component from the reactor;(d) withdrawing a second stream comprising the spent catalyst component, the coke, the coarse filler and the inorganic components from the reactor;(e) heating the second stream in a regenerator in the presence of oxygen, air, or a blend of oxygen with an inert gas at a temperature effective to convert the coke to a mixture of carbon monoxide, carbon dioxide and water, and to regenerate the solid catalyst component; and(f) separating the regenerated solid catalyst component from the coarse filler and the inorganic components.15. The process of claim 14 , wherein the inert gas of step (e) is nitrogen claim 14 , steam or combinations thereof.16. The process of claim 14 , wherein the volatile ...

Catalyst System and Use in Heavy Aromatics Conversion Processes

Disclosed are a catalyst system and its use in a process for the conversion of a feedstock containing C 8 + aromatic hydrocarbons to produce light aromatic products, comprising benzene, toluene and xylene. The catalyst system comprises (a) a first catalyst bed comprising a first catalyst composition, said first catalyst composition comprising a zeolite having a constraint index of 3 to 12 combined (i) optionally with at least one first metal of Group 10 of the IUPAC Periodic Table, and (ii) optionally with at least one second metal of Group 11 to 15 of the IUPAC Periodic Table; and (b) a second catalyst bed comprising a second catalyst composition, said second catalyst composition comprising (i) a meso-mordenite zeolite, combined (ii) optionally with at least one first metal of Group 10 of the IUPAC Periodic Table, and (iii) optionally with at least one second metal of Group 11 to 15 of the IUPAC Periodic Table, wherein said meso-mordenite zeolite is synthesized from TEA or MTEA and having a mesopore surface area of greater than 30 m 2 /g and said meso-mordenite zeolite comprises agglomerates composed of primary crystallites, wherein said primary crystallites have an average primary crystal size as measured by TEM of less than 80 nm and an aspect ratio of less than 2.

PROCESS FOR CONVERTING LPG TO HIGHER HYDROCARBON(S)

The present invention relates to a process for converting a feed comprising C2-C4 alkanes to higher hydrocarbon(s) including aromatic hydrocarbon(s) in n reaction zones operated in series, wherein m reaction zones are not participating in the conversion process and only (n-m) reaction zones are operated under reaction conditions sufficient to convert at least a portion of said a feed comprising C2-C4 alkanes to an effluent having said higher hydrocarbon(s). An object of the present invention is to provide a process for converting LPG to higher hydrocarbon(s) including aromatic hydrocarbon(s) wherein a high reactant, i.e. ethane, propane and/or butane, conversion can be achieved. 1. A process for converting LPG to higher hydrocarbon(s) including aromatic hydrocarbon(s) in n reaction zones operated in series , wherein m reaction zones are not participating in the conversion process and only (n-m) reaction zones are operated under reaction conditions sufficient to convert at least a portion of said LPG to an effluent having said higher hydrocarbon(s) , wherein each reaction zone is initially numbered serially with a designator from 1 to n , the process comprising:(a) providing a quantity of catalytic material within each reaction zone;(b) providing to the reaction zone designated as 1 a hydrocarbon feedstock containing LPG;(c) heating at least a portion of the effluent of the said reaction zone designated as 1 to the inlet temperature of the reaction zone designated as 2, and more generally, heating at least a portion of the effluent of each reaction zone with a designator equal or smaller than (n-m−1) to the inlet temperature of the reaction zone with a designator larger by one than that of the reaction zone from which said effluent originates;(d) transferring said at least portion of said effluent of the said reaction zone designated as 1 to said reaction zone designated as 2, and more generally, transferring said at least portion of said reaction zone with a ...

Power Generation using Independent Dual Organic Rankine Cycles from Waste Heat Systems in Diesel Hydrotreating-Hydrocracking and Atmospheric Distillation-Naphtha Hydrotreating-Aromatics Facilities

Optimizing power generation from waste heat in large industrial facilities such as petroleum refineries by utilizing a subset of all available hot source streams selected based, in part, on considerations for example, capital cost, ease of operation, economics of scale power generation, a number of ORC machines to be operated, operating conditions of each ORC machine, combinations of them, or other considerations are described. Subsets of hot sources that are optimized to provide waste heat to one or more ORC machines for power generation are also described. Further, recognizing that the utilization of waste heat from all available hot sources in a mega-site such as a petroleum refinery and aromatics complex is not necessarily or not always the best option, hot source units in petroleum refineries from which waste heat can be consolidated to power the one or more ORC machines are identified.

CRYSTALLINE TRANSITION METAL TUNGSTATE PROCESS DATA SYSTEM

A hydroprocessing catalyst has been developed. The catalyst is a crystalline transition metal tungstate material or metal sulfides derived therefrom, or both. The hydroprocessing using the crystalline transition metal tungstate material may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking. A data system comprising at least one processor; at least one memory storing computer-executable instructions; and at least one receiver configured to receive data of at least one unit or stream in fluid communication with and downstream from or upstream to a conversion process comprising at least one reaction catalyzed by the catalyst or a metal sulfide decomposition product of the catalyst has been developed. 2. The system of further comprising an Input/Output device to collect the data claim 1 , or evaluate the date claim 1 , or correlate the data claim 1 , or any combination thereof.3. The system of further comprising a transmitter to transmit a signal to the conversion process.4. The system of wherein the signal comprises instructions.5. The system of wherein the signal comprises instructions regarding an adjustment to a parameter.6. The system of further comprising collecting data from multiple systems wherein one system is the parameter data system.7. The system of wherein the processor is configured to generate predictive information or quantitative information.8. The system of wherein the at least one unit or stream is not in direct fluid communication with the conversion process10. The method of further comprising at least one of displaying or transmitting or analyzing the received data.11. The method of further comprising analyzing the received data to generate at least one instruction and transmitting the at least one instruction.12. The method of further comprising analyzing the received data and generating predictive information or ...

PROCESS FOR XYLENE PRODUCTION WITH ENERGY OPTIMIZATION

A method for producing xylenes from a heavy reformate feed includes the steps of introducing the heavy reformate feed and a hydrogen feed to a dealkylation reactor, reacting the heavy reformate feed with the hydrogen gas in the presence of the dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, introducing the dealkylation effluent to a splitter unit, separating the dealkylation effluent into a light gas stream, a toluene stream, a benzene stream, a C9 aromatics stream, a C10+ aromatics stream, and a mixed xylene stream in the splitter unit, introducing the toluene stream, the C9 aromatics stream, and a hydrogen stream into a transalkylation reactor, reacting the toluene stream and the C9 aromatics stream in the presence of the transalkylation catalyst to produce a transalkylation effluent, introducing the transalkylation effluent to the splitter unit, and separating the transalkylation effluent in the splitter unit. 1. A method for producing mixed xylenes from a heavy reformate feed , the method comprising the steps of:introducing the heavy reformate feed to a feed exchanger to produce a hot feed stream, wherein the feed exchanger increases the temperature of the heavy reformate feed, wherein the heavy reformate comprises aromatic hydrocarbons with nine or more carbon atoms (C9+ aromatics), wherein the hydrogen feed comprises hydrogen gas;mixing the hot feed stream and a hydrogen feed to produce a mixed feed;increasing a temperature of the mixed feed in a feed-effluent exchanger to produce a hot mixed feed, wherein a temperature of the hot mixed feed is between 324 deg C. and 344 deg C.;increasing the temperature of the hot mixed feed in a feed fired heater to produce a hot reactor feed, wherein a temperature of the hot reactor feed is between 380 deg C. and 400 deg C.;introducing the hot reactor feed to a dealkylation reactor, wherein the dealkylation reactor comprises a dealkylation catalyst;reacting the heavy reformate feed with ...

TWO-STAGE HYDROCRACKING PROCESS COMPRISING A HYDROGENATION STAGE DOWNSTREAM OF THE SECOND HYDROCRACKING STAGE, FOR THE PRODUCTION OF MIDDLE DISTILLATES

The invention relates to the implementation of a multi-stage hydrocracking process comprising a hydrogenation stage located downstream of the second hydrocracking stage, said hydrogenation stage treating the effluent produced in the second hydrocracking stage, in the presence of a specific hydrogenation catalyst. In addition, the hydrogenation and second hydrocracking stages are implemented under specific operating conditions and particularly under very specific temperature conditions. 1. Process for producing middle distillates from hydrocarbon feedstocks containing at least 20% by volume of compounds boiling above 340° C. , said process comprising the following steps:{'sup': '−1', 'a) a step of hydrotreating said feedstocks in the presence of hydrogen and at least one hydrotreating catalyst, at a temperature of between 200° C. and 450° C., under a pressure of between 2 and 25 MPa, at a space velocity of between 0.1 and 6 hand with an amount of hydrogen introduced such that the litre of hydrogen/litre of hydrocarbon volume ratio is between 100 and 2000 Nl/l,'}{'sup': '−1', 'b) a step of hydrocracking at least one portion of the effluent resulting from step a), the hydrocracking step b) taking place, in the presence of hydrogen and at least one hydrocracking catalyst, at a temperature of between 250° C. and 480° C., under a pressure of between 2 and 25 MPa, at a space velocity of between 0.1 and 6 hand with an amount of hydrogen introduced such that the litre of hydrogen/litre of hydrocarbon volume ratio is between 80 and 2000 Nl/l,'}c) a step of high-pressure separation of the effluent resulting from the hydrocracking step b) to produce at least a gaseous effluent and a liquid hydrocarbon effluent, a gaseous fraction,', 'at least one petroleum fraction having at least 80% by volume of products boiling at a temperature below 150° C.,', 'at least one middle distillates fraction having at least 80% by volume of products having a boiling point between 150° C. and 380° ...

CATALYST WITH IMPROVED ACTIVITY/SELECTIVITY FOR LIGHT NAPHTHA AROMATIZATION

In an embodiment, A catalyst comprises a zeolite comprising Si, Al, and Ge in the framework with Pt deposited thereon; wherein the catalyst has an Si:Almole ratio of greater than or equal to 125, an Si:Ge mole ratio of 40 to 400, and an Na:Al mole ratio of 0.9 to 2.5; wherein the catalyst has an aluminum content of less than or equal to 0.75 wt %; wherein the catalyst is non-acidic. 1. A catalyst comprising:a zeolite comprising Si, Al, and Ge in the framework with Pt deposited thereon; wherein the zeolite is a medium pore zeolite having an average pore size of 5 to 8 Å;{'sub': '2', 'wherein the catalyst has an Si:Almole ratio of 125 to 211, an Si:Ge mole ratio of 40 to 400, and an Na:Al mole ratio of 0.9 to 2.5;'}wherein the catalyst has an aluminum content of less than or equal to 0.75 wt %, and a Ge content of 0.1 to 3 wt %, based on the total weight of the catalyst excluding any binder and extrusion aide;wherein the catalyst is non-acidic.2. The catalyst of claim 1 , wherein the Ge is present in an amount of 0.4 to 2.5 wt % claim 1 , and/or the Na is present in an amount of 0.5 to 2 wt % and/or the Pt is present in an amount of 0.05 to 3 wt % claim 1 , wherein the wt % values are based on the total weight of the catalyst excluding any binder and extrusion aide.3. The catalyst of claim 2 , wherein the catalyst has all of the Ge content of 0.4 to 2.5 wt % claim 2 , the Na content of 0.5 to 2 wt % claim 2 , and the Pt content of 0.05 to 3 wt % claim 2 , wherein the wt % values are based on the total weight of the catalyst excluding any binder and extrusion aide.4. The catalyst of claim 1 , wherein the catalyst has a Ge content of 0.4 to 1.5 wt % based on the total weight of the catalyst excluding any binder and extrusion aide.5. The catalyst of claim 1 , wherein the catalyst comprises Al in an amount of 0.45 to 0.7 wt % based on the total weight of the catalyst excluding any binder and extrusion aide.6. The catalyst of claim 1 , wherein the zeolite is MTW claim 1 , ...

Producing method of monocyclic aromatic hydrocarbons and monocyclic aromatic hydrocarbon production plant

A producing method of monocyclic aromatic hydrocarbons in which reaction products including monocyclic aromatic hydrocarbons are produced by bringing an oil feedstock and an aromatic production catalyst into contact with each other, the oil feedstock having a 10 volume % distillation temperature of more than or equal to 140° C. and a 90 volume % distillation temperature of less than or equal to 380° C., the method including the steps of: introducing the oil feedstock into a fluidized-bed reaction apparatus housing the aromatic production catalyst; bringing the oil feedstock and the aromatic production catalyst into contact with each other in the fluidized-bed reaction apparatus; and introducing steam into the fluidized-bed reaction apparatus based on the introducing amount of the oil feedstock per hour.

ENERGY-RECOVERY TURBINES FOR GAS STREAMS

Processes for controlling the flowrate of and recovering energy from a gas stream in a processing unit are described. One process comprises directing a portion of the gas stream through one or more variable-resistance power-recovery turbines to control the flowrate of the gas stream and generate electric power therefrom; and controlling the pressure and temperature of the gas stream so that the gas exiting the power-recovery turbine remains in the gas phase. 1. A process for controlling a flowrate of and recovering energy from a gas stream in a processing unit comprising:directing at least a portion of the gas stream through one or more variable-resistance power-recovery turbine to control the flowrate of the gas stream and generate electric power therefrom;controlling a pressure and temperature of the gas stream through the one or more power-recovery turbines so that the gas exiting the one or more power-recovery turbine remains in a gas phase; andmeasuring the flowrate using turbine revolutions per minute of the one or more power-recovery turbine and a load on a circuit.2. The process of further comprising controlling the flowrate by varying one or more of the speed or shaft torque of the one or more power-recovery turbine.3. The process of further comprising replacing a control valve with the one or more power-recovery turbine before directing the at least the portion of the gas stream through the one or more power-recovery turbine.4. The process of wherein the one or more power-recovery turbine is used in conjunction with a control valve claim 1 , and further comprising directing a second portion of the gas stream through the control valve.5. The process of wherein the portion of the gas stream directed through the one or more power-recovery turbine is greater than the second portion of the gas stream directed though the control valve.6. The process of wherein the power recovered is displayed on at least one display screen.7. The process of further comprising: ...

DETECTING AND CORRECTING THERMAL STRESSES IN HEAT EXCHANGERS IN A PETROCHEMICAL PLANT OR REFINERY

A plant or refinery may include equipment such as reactors, heaters, heat exchangers, regenerators, separators, or the like. Types of heat exchangers include shell and tube, plate, plate and shell, plate fin, air cooled, wetted-surface air cooled, or the like. Operating methods may impact deterioration in equipment condition, prolong equipment life, extend production operating time, or provide other benefits. Mechanical or digital sensors may be used for monitoring equipment, and sensor data may be programmatically analyzed to identify developing problems. For example, sensors may be used in conjunction with one or more system components to detect and correct maldistribution, cross-leakage, strain, pre-leakage, thermal stresses, fouling, vibration, problems in liquid lifting, conditions that can affect air-cooled exchangers, conditions that can affect a wetted-surface air-cooled heat exchanger, or the like. An operating condition or mode may be adjusted to prolong equipment life or avoid equipment failure. 1. A system comprising:a reactor;a heater;a heat exchanger;a regenerator;a separator;one or more sensors associated with the heat exchanger; one or more processors of the data collection platform;', 'a communication interface of the data collection platform; and', receive, from the one or more sensors associated with the heat exchanger, sensor data comprising operation information associated with the heat exchanger;', 'correlate the sensor data from the one or more sensors with metadata comprising time data, the time data corresponding to the operation information associated with the heat exchanger; and', 'transmit the sensor data; and, 'memory storing executable instructions that, when executed, cause the data collection platform to], 'a data collection platform comprising one or more processors of the data analysis platform;', 'a communication interface of the data analysis platform; and', receive, from the data collection platform, the sensor data comprising ...

PROCEDURE TO PREPARE A SUPPORTED TRIMETALLIC CATALYST FOR PRODUCTION OF ULTRA LOW SULFUR DIESEL AND ITS APPLICATION

According to this invention, a Ni—Mo—W trimetallic catalyst supported on porous alumina is obtained that shows very high activity for hydrotreating (HDT) of gasoils, particularly deep hydrodesulfurization (HDS) and hydrodesnitrogenation (HDN) of straight run gasoil in conditions of moderate pressure. 1. A procedure to obtain a supported trimetallic catalytic formulation for the deep hydrodesulfurization of straight run gasoil and for the production of ultra low sulfur diesel (ULSD) , comprising the following steps:a) preparation of solution containing tungsten (solution a), b) preparation of solution containing molybdenum, nickel and phosphorus (solution b), c) preparation of solution containing nickel and EDTA (solution c), d) preparation of solution containing nickel, molybdenum and EDTA (solution d) and e) mixture of solutions (c) and (d); e) drying the catalytic support at a temperature of 100 to 120° C., for 3 to 6 hours, f) impregnation of the solution (a), ageing of the material for 10 to 15 hours, drying at a temperature of 100 to 120° C. for 3 to 5 hours, g) impregnation of the solution (b), ageing of the material for 8 to 10 hours, drying at a temperature of 100 to 120° C. for 4 to 6 hours, h) impregnation of the mixture of the solutions c+d, ageing of the material during 30-40 minutes, no longer aging time is allowed, and drying at a temperature of 60 to 200° C., for 4 to 15 hours, i) wetting of the catalyst with SRGO, j) sulfiding the impregnated catalyst.2. A procedure according to claim 1 , wherein the following solutions are prepared;a) aqueous solution containing a metal of group VIB as tungsten, from ammonium metatungstate in water, until obtaining a completely transparent and crystalline solution;b) acid solution containing a metal of group VIB, such as Mo and a metal of group VIIIB as Ni, dissolved in a phosphoric acid solution;c) solution containing a metal of group VIIIB as Ni, and an organic compound such as ethylenediaminetetraacetic acid ( ...

Aromatization Catalyst Preparation with Alkali Metal Present During a Washing Step

Methods for producing supported catalysts containing a transition metal and a bound zeolite base are disclosed. These methods employ a step of washing the bound zeolite base in the presence of an alkali metal, prior to impregnating the bound zeolitic support with the transition metal. Alkali metals such as potassium and cesium may be used. 1. A method of producing a supported catalyst , the method comprising:(a) providing a bound zeolite base;(b) washing the bound zeolite base with an aqueous solution comprising cesium to produce a cesium enriched zeolite support; and(c) impregnating the cesium enriched zeolite support with a transition metal and a halogen to produce the supported catalyst;wherein the concentration of cesium in the aqueous solution is in a range from about 0.01 M to about 5 M.2. The method of claim 1 , wherein:the bound zeolite base comprises a silica-bound K/L-zeolite;the transition metal comprises platinum; andthe halogen comprises chlorine, fluorine, or both.3. The method of claim 1 , wherein:the aqueous solution further comprises potassium, rubidium, or a combination thereof; andthe supported catalyst comprises from about 5 wt. % to about 30 wt. % of a binder, based on the total weight of the supported catalyst.4. The method of claim 1 , wherein the supported catalyst comprises:from about 0.2 wt. % to about 5 wt. % transition metal;from about 0.2 wt. % to about 3 wt. % halogen; andfrom about 2 wt. % to about 10 wt. % cesium;based on the total weight of the supported catalyst.5. The method of claim 1 , wherein step (b) comprises from 2 to 8 washing cycles claim 1 , each washing cycle conducted independently at a washing temperature in a range from about 20° C. to about 95° C. and for a time period in a range from about 5 minutes to about 2 hours.6. The method of claim 5 , wherein a ratio of the weight of the aqueous solution to the weight of the bound zeolite base in each washing cycle independently is in a range about 0.4:1 to about 10:1.7. The ...

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.

Process for producing btx from a c5-c12 hydrocarbon mixture

The present invention relates to a process for producing chemical grade BTX from a mixed feedstream comprising C5-C12 hydrocarbons by contacting said feedstream in the presence of hydrogen with a catalyst having hydrocracking/hydrodesulphurisation activity. Particularly, a process for producing BTX from a feedstream comprising C5-C12 hydrocarbons is provided comprising the steps of: (a) contacting said feedstream in the presence of hydrogen with a combined hydrocracking/hydrodesulphurisation catalyst to produce a hydrocracking product stream comprising BTX; and (b) separating the BTX from the hydrocracking product stream. The hydrocracking/hydrodesulphurisation catalyst comprises 0.1-1 wt-% hydrogenation metal in relation to the total catalyst weight. The hydrocracking/hydrodesulphurisation catalyst further comprises a zeolite having a pore size of 5-8 Å and a silica (SiO 2 ) to alumina (Al 2 O 3 ) molar ratio of 5-200. The hydrocracking/hydrodesulphurisation conditions include a temperature of 450-580° C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 0.1-10 h −1 .

Supercritical water processes for upgrading a petroleum-based composition while decreasing plugging

Embodiments of processes for upgrading a petroleum-based composition while decreasing plugging comprise mixing a supercritical water stream with a pressurized, heated petroleum-based composition in a mixing device to create a combined feed stream, and introducing to a supercritical upgrading reactor system are provided. The processes also comprise cooling the upgraded product in a cooling device, and decreasing the pressure of the cooled upgraded product in a pressure reducer. To reduce plugging, the processes also comprises injecting plug remover solution into one or more of the following injection locations: an injection port on a process line connecting the mixing device with the upgrading reactor system; an injection port on a process line connecting the upgrading reactor system with the cooling device; or an injection port on a process line connecting the cooling device with the pressure reducer.

Pyrolysis Tar Conversion

A process is provided for determining the suitability of pyrolysis tar, such as steam cracker tar, for upgrading using hydroprocessing without long term fouling of the hydroprocessing reactor. The process includes heating a sample of the tar, quenching the sample, and measuring the total free radical content of the quenched sample. A pyrolysis tar can be blended with one having a lesser total free radical content to produce a blend that can be hydroprocessed with decreased fouling. 1. A hydrocarbon process , comprising:{'sub': '1', '(a) providing a first pyrolysis tar having a temperature T≤350° C., the pyrolysis tar being a hydrocarbon-containing mixture which includes free radicals and is derived from hydrocarbon pyrolysis, wherein at least 70 wt. % of the mixture has a normal boiling point of at least 290° C.;'}{'sub': 2', 'h', '2', '1, '(b) isolating a sample from the first pyrolysis tar and producing additional free radicals in the sample by exposing the sample to a predetermined second temperature Tfor a predetermined time t, wherein T≥T+10° C.;'}{'sub': 3', '3', '1', 'T, '(c) cooling the sample to a temperature T, Tbeing ≤T, the cooled sample having a total free radical content R;'}{'sub': 'T', 'claim-text': {'sub': T', 'ref, 'claim-text': [{'sub': '1', '(A) providing a second pyrolysis tar at a temperature ≤T, the second pyrolysis tar being a hydrocarbon-containing mixture derived from hydrocarbon pyrolysis, wherein at least 70 wt. % of the mixture has a normal boiling point of at least 290° C., and combining the first pyrolysis tar with a predetermined amount of the second pyrolysis tar to produce a pyrolysis tar composition,'}, {'sub': 2', 'h', '3', 'T, '(B) (I) isolating a sample from the pyrolysis tar composition, (II) producing additional free radicals in the pyrolysis tar composition sample by exposing the pyrolysis tar composition sample to a temperature of at least Tfor time of at least t, and (III) cooling the pyrolysis tar composition sample to a ...

ALLOYED ZEOLITE CATALYST COMPONENT, METHOD FOR MAKING AND CATALYTIC APPLICATION THEREOF

The presently disclosed and claimed inventive concept(s) generally relates to a solid catalyst component comprising a zeolite with a modifier and at least one Group VIII meal alloyed with at least one transition metal. The presently disclosed and claimed inventive concept(s) further relates to a method of making the solid catalyst component and a process of converting mixed waste plastics into low molecular weight organic compounds using the solid catalyst component. 113.-. (canceled)14. A process of converting a mixed waste plastic into a low molecular weight organic compound , comprising the steps of(a) feeding particles of the mixed waste plastic and a solid catalyst component into a fluidized bed reactor, the solid catalyst component comprising (i) a modified zeolite and (ii) alloyed metals comprising at least one noble metal alloyed with at least one transition metal, wherein the zeolite is selected from the group consisting of chabazite, erionite, faujasite, ferrierite, mordenite, offretite, TEA-mordenite, zeolite A, zeolite beta, zeolite boron beta, zeolite L, zeolite X, zeolite Y, zeolite ZK-5, Breck-6, HZSM-5, ITQ-1, ITQ-21, MCM-22, MCM-36, MCM-39, MCM-41, MCM-48, PSH-3, SUZ-4, EU-1, SAPO-5, SAPO-11, SAPO-34, (S)AIPO-31, SSZ-23, SSZ-32, TUD-1, VPI-5, ZSM-4, ZSM-5, ZSM-8, ZSM-11, ZSM-12, ZSM-20, ZSM-21, ZSM-22, ZSM-23, ZSM-34, ZSM-35, ZSM-38, ZSM-48, ZSM-50, ZSM-57, and combinations thereof, and wherein the modified zeolite is modified with a modifier selected from the group consisting of (1) phosphorous, (2) boron, (3) phosphorous and boron, (4) an additive selected from the group consisting of gallium, zinc, zirconium, niobium, tantalum, and combinations thereof, and (5) combinations thereof;(b) heating the particles of the mixed waste plastic and the solid catalyst component at a temperature effective to produce a coarse filler, inorganic components, coke, a volatile organic component, and a spent catalyst component;(c) withdrawing a first stream ...

AMMONIATED QUENCHING OF A HYDROPROCESSING REACTION

The disclosure provided herein describes processes for rapidly quenching an over-temperature hydroprocessing reaction utilizing a pressurized quenching agent that is rapidly released into the hydroprocessing reactor. Optimally, the quenching agent blocks acidic catalytic sites of the hydroprocessing catalyst to competitively inhibit exothermic reaction rate. Exemplary quench agents include ammonia or a chemical that is converted to ammonia under hydroprocessing conditions. 1. A process for quenching a catalytic hydroprocessing reaction , comprising:a) contacting a feedstock derived from at least one of petroleum or biomass with a hydroprocessing catalyst comprising at least on acidic catalytic active site in a reaction zone at a temperature and pressure that facilitates hydroprocessing reactions, wherein the contacting converts the feedstock to a reactor effluent comprising a liquid hydrocarbon fuel or a blending component thereof;b) detecting a temperature condition in the reaction zone;c) dispensing a quenching agent from a pressurized vessel to the reaction zone when the temperature condition exceeds a first predetermined threshold temperature, wherein the quenching agent binds to and blocks at least one active site of the hydroprocessing catalyst.2. The process of claim 1 , wherein the first predetermined threshold temperature is at least 473° C. (820° F.)3. The process of claim 1 , wherein the first predetermined threshold temperature is at least 476° C. (825° F.).4. The process of claim 1 , wherein the first predetermined threshold temperature is at least 479° C. (830° F.).5. The process of claim 1 , wherein the first predetermined threshold temperature is at least 482° C. (835° F.).6. The process of claim 1 , wherein the first predetermined threshold temperature is at least 484° C. (840° F.).7. The process of claim 1 , wherein the first predetermined threshold temperature is at least 487° C. (845° F.).8. The process of claim 1 , wherein the first ...

Method for Monitoring Performance of Process Catalysts

Disclosed is a method for determining when to replace a guard bed material used to remove one or more catalyst poisons from a feed based on a parameter change in a process A guard bed having a guard bed material is in fluid communication with a catalyst bed having a catalyst. At least three monitors are positioned in said guard bed or said catalyst bed and at least one parameter of the guard bed or catalyst bed is monitored. A feed component comprising one or more catalyst poisons is supplied to said guard bed or said catalyst bed. The feed is contacted with said guard bed material or said catalyst to remove at least a portion of a catalyst poison and to form a product which produces an increase or a decrease in said parameter. The monitored parameters are compared to determine when to replace the guard bed material. 1. A method for determining when to replace a guard bed material used to remove a catalyst poison from a feed based on a parameter change in a process , said method comprising the steps of:(a) providing a guard bed comprising a guard bed material, said guard bed having an inlet and a downstream outlet;(b) placing at least three guard bed monitors proximate said guard bed, wherein a first guard bed monitor is located proximate said inlet to said guard bed, a third guard bed monitor is located downstream of said outlet of said guard bed, and one or more second guard bed monitors is located downstream of said inlet of said guard bed and upstream of said outlet of said guard bed;(c) monitoring at least one guard bed parameter of said guard bed with each of said at least three guard bed monitors;(d) at least intermittently supplying a feed to said guard bed, wherein said feed comprises a catalyst poison;(e) contacting said feed with said guard bed material under suitable guard bed treatment conditions to remove at least a portion of said catalyst poison from said feed and to form a treated feed; Wherein said contacting produces an increase or a decrease in ...

MULTI-STAGE RESID HYDROCRACKING

Processes and systems for upgrading resid hydrocarbon feeds are disclosed. The process system may operate in two different operating modes, maximum conversion and maximum quality effluent. The process system may be reversibly transitioned between the different operating modes. The system has the ability to reversibly transition between the two modes without shutting down the system or losing production. 1. A process for upgrading resid , comprising:feeding hydrogen and a resid hydrocarbon to a first ebullated bed reactor containing a first hydrocracking catalyst;contacting the resid and hydrogen in the presence of the hydrocracking catalyst at conditions of temperature and pressure to crack at least a portion of the resid;separating a product from the first reactor into a first gas phase and a first liquid phase product;feeding hydrogen and a deasphalted oil hydrocarbon fraction and a vacuum distillate hydrocarbon fraction to a second ebullated bed reactor containing a hydrotreating catalyst;contacting the deasphalted oil hydrocarbon fraction, the vacuum distillate hydrocarbon fraction and hydrogen in the presence of the hydrotreating catalyst at conditions of temperature and pressure to hydrotreat at least a portion of the deasphalted oil hydrocarbon fraction and the vacuum distillate hydrocarbon fraction;separating a product from the second reactor into a second gas phase and a second liquid phase product;separating the second liquid phase product into a second reactor effluent and a residual fluid catalytic cracking (RFCC) feed;fractionating the first liquid phase product and the second reactor effluent to form at least one distillate hydrocarbon fraction, the vacuum distillate hydrocarbon fraction, and at least one resid hydrocarbon fraction; andfeeding the at least one resid hydrocarbon fraction to a solvent deasphalting unit to provide an asphaltene fraction and the deasphalted oil hydrocarbon fraction.2. The process of claim 1 , wherein the fractionating ...

METHOD, SERVER, COMPUTER-READABLE COMMAND, AND RECORDING MEDIUM FOR PROVIDING RECOMMENDED OPERATION CONDITION FOR PLANT

Provided is a method for providing a recommended operating condition with which an oil refinery device can be operated more efficiently. A server : acquires past operational data for a device, a scheduled operating condition which is an operation condition for the device scheduled by a user, and plant information including at least a usage expiry time of the device; creates a user-specific catalyst deterioration function from the past operational data; calculates, on the basis of the catalyst deterioration function, the plant information, and the schedule operating condition, a recommended operating condition that achieves a catalyst lifetime which is later than the usage expiry time of the device and is earlier than the catalyst lifetime when the device is operated under a scheduled operating condition calculated on the basis of the scheduled operating condition and the catalyst deterioration function; and transmits the recommended operating condition to a user terminal. 1. A method for providing a recommended operation condition for a plant that produces oils by passing stock oil through a catalyst , the recommended operation condition being provided by use of a server connected to a user terminal through a network ,wherein the server includes a processor and a non-transitory computer-readable command recording medium storing a computer-readable command, andwherein the method causes the server to:acquire, from the user terminal, past operation data of the plant, a scheduled operation condition, the scheduled operation condition being an operation condition of the plant scheduled by a user, and plant information including at least an expiration date for use of the plant;create a catalyst degradation function specific to the user from the past operation data; andcalculate, based on the catalyst degradation function, the plant information, and the scheduled operation condition, a recommended operation condition with which a catalyst lifetime ends earlier than a ...

Process for producing cumene and/or ethylbenzene from a mixed hydrocarbon feedstream

The present invention relates to a process for producing cumene and/or ethylbenzene from a mixed hydrocarbon feedstream comprising subjecting C6 cut separated from said mixed hydrocarbon feedstream to aromatization to provide an aromatization product stream and subjecting the thus obtained aromatization product stream to alkylation to produce an alkylated aromatic stream.

PROCESS FOR MAXIMIZING PRODUCTION OF XYLENES FROM HEAVY REFORMATE WITHOUT PURGE

A method for producing xylenes from a heavy reformate feed includes the steps of introducing the heavy reformate feed and a hydrogen feed to a dealkylation reactor, reacting the heavy reformate feed with the hydrogen gas in the presence of the dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, introducing the dealkylation effluent to a splitter unit, separating the dealkylation effluent into a light gas stream, a toluene stream, a benzene stream, a C9 aromatics stream, a C10+ aromatics stream, and a mixed xylene stream in the splitter unit, introducing the toluene stream, the C9 aromatics stream, and a hydrogen stream into a transalkylation reactor, reacting the toluene stream and the C9 aromatics stream in the presence of the transalkylation catalyst to produce a transalkylation effluent, introducing the transalkylation effluent to the splitter unit, and separating the transalkylation effluent in the splitter unit. 1. A method for producing mixed xylenes from a heavy reformate feed , the method comprising the steps of:introducing the heavy reformate feed and a hydrogen feed to a dealkylation reactor, wherein the dealkylation reactor comprises a dealkylation catalyst, wherein the heavy reformate feed comprises aromatic hydrocarbons with nine or more carbon atoms (C9+ aromatics), wherein the hydrogen feed comprises hydrogen gas;reacting the heavy reformate feed with the hydrogen feed in the presence of the dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, wherein the dealkylation reactor is at a dealkylation temperature, wherein the dealkylation reactor is at a dealkylation pressure, wherein the dealkylation reactor has a liquid hourly space velocity;introducing the dealkylation effluent to a splitter unit, where the dealkylation effluent comprises light gases, toluene, benzene, mixed xylenes, and C9+ aromatics;separating the dealkylation effluent into a light gas stream, a toluene stream, a ...

Liquid-Phase Hydroisomerization System And Process Therefor And Use Thereof

Provided are a liquid-phase hydroisomerization system and a process therefor and use thereof. The system comprises a gas-liquid mixer (), a hydroisomerization reactor () and a fractionating column (). An oil product and hydrogen are mixed as a liquid hydrogen-oil mixture, and are introduced into the hydroisomerization reactor for a hydroisomerization reaction, and after being fractionated, a target product is led out. A supplemental hydrogen-dissolving inner member is provided at least between a group of two adjacent catalyst bed layers in order to supplement hydrogen to the reactants. The process cancels a circulating hydrogen compressor, has a simple process flow, and can be applied to the production of a lubricant base oil by the hydroisomerization of a lubricant raw material or the production of a low freezing point diesel by the hydroisomerization of and the reduction in the freezing point of a diesel raw material. 1. A liquid-phase hydroisomerization system , characterized in that the system comprises:a hydrogen-dissolving unit, a hydroisomerization reactor, and a fractionating column;wherein the hydrogen-dissolving unit comprises an oil feed line, a hydrogen feed line and a hydrogen-oil-mixture line, the hydrogen-oil-mixture line is in communication with the bottom of the hydroisomerization reactor, and the top of the hydroisomerization reactor is in communication with the fractionating column;the hydroisomerization reactor includes at least two catalyst beds, and an internal dissolved-hydrogen replenishment member is provided between at least one pair of two adjacent catalyst beds;the internal dissolved-hydrogen replenishment member comprises a bottom sieve separating plate, a middle mixing space and a top separating plate, the top separating plate is provided with multiple liquid discharging pipes, and the middle mixing space is provided with a hydrogen inlet and a hydrogen outlet; hydrogen and oil are mixed in the middle mixing space, the liquid phase in ...

PROCESS FOR XYLENE PRODUCTION WITH ENERGY OPTIMIZATION

A method for producing xylenes from a heavy reformate feed includes the steps of introducing the heavy reformate feed and a hydrogen feed to a dealkylation reactor, reacting the heavy reformate feed with the hydrogen gas in the presence of the dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, introducing the dealkylation effluent to a splitter unit, separating the dealkylation effluent into a light gas stream, a toluene stream, a benzene stream, a C9 aromatics stream, a C10+ aromatics stream, and a mixed xylene stream in the splitter unit, introducing the toluene stream, the C9 aromatics stream, and a hydrogen stream into a transalkylation reactor, reacting the toluene stream and the C9 aromatics stream in the presence of the transalkylation catalyst to produce a transalkylation effluent, introducing the transalkylation effluent to the splitter unit, and separating the transalkylation effluent in the splitter unit. 1. A system for producing mixed xylenes from a heavy reformate feed , the system comprising:a feed exchanger, the feed exchanger configured to transfer heat from a mixed xylene stream to the heavy reformate feed to increase a temperature of the heavy reformate feed to produce a hot feed stream, wherein the feed exchanger is a cross process exchanger, wherein the heavy reformate comprises aromatic hydrocarbons with nine or more carbon atoms (C9+ aromatics), wherein the hydrogen feed comprises hydrogen gas, wherein a temperature of the mixed xylene stream is reduced to produce a cooled mixed stream;a mixing point fluidly connected to the feed exchanger, the mixing point configured to mix the hot feed stream and a hydrogen feed to produce a mixed feed;a feed-effluent exchanger fluidly connected to the mixing point, the feed-effluent exchanger configured to transfer heat from a dealkylation effluent to the mixed feed to increase a temperature of the mixed feed to produce a hot mixed feed, wherein the feed-effluent exchanger ...

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 ...

POWER RECOVERY FROM QUENCH AND DILUTION VAPOR STREAMS

A process for reducing pressure of a vapor stream used for reducing a temperature or pressure in a reactor. A pressure of a vapor stream is reduced with a turbine to provide a lower pressure vapor stream. The vapor stream rotates a turbine wheel within the turbine. The turbine wheel is configured to transmit rotational movement to an electrical generator. Thus, electricity is generated with the turbine. The lower pressure vapor stream is injected into a reactor and reduces a temperature in the reactor or reduces a partial pressure of a hydrocarbon vapor in the reactor. 1. A process for reducing pressure of a vapor stream used for reducing a temperature , heat load , or hydrocarbon partial pressure in a reactor , the process comprising:reducing a pressure of a vapor stream with a turbine to provide a lower pressure vapor stream;rotating a turbine wheel within the turbine,injecting the lower pressure vapor stream into a reactor and reducing a temperature in the reactor or reducing a partial pressure of a hydrocarbon vapor in the reactor.2. The process of further comprising increasing the feed rate to the reactor by relaxing a high temperature bottleneck by extracting energy from the vapor stream.3. The process of wherein the turbine wheel is configured to transmit rotational movement to an electrical generator claim 1 , and the process further comprising:generating electricity with the turbine.4. The process of further comprising:receiving information from the turbine relative to an amount of electricity generated by the turbine; and,displaying the amount of electricity generated by the turbine on at least one display screen.5. The process of further comprising:maintaining a throughput of the reactor while adjusting at least one process parameter of the reactor.6. The process of claim 4 , wherein the reactor comprises a plurality of turbines each configured to generate electricity claim 4 , and wherein the process comprises:determining a total power generated based ...

CATALYSTS BASED ON SILICOALUMINOPHOSPHATE SAPO-11 AND USES THEREOF

The invention provides a process for preparing SAPO-11, that comprises combining in an aqueous solution alumina source, P 2 O source and a silica source in the presence of a crystallization template and a surfactant to form a gel, which is then subjected to hydrothermal crystallization and calcination. The so-formed SAPO-11, which possesses unique silicon distribution, high resistance to hydrothermal degradation (desilication) and high surface area, forms another aspect of the invention. Hydroprocessing of a vegetable oil in the presence of a catalyst comprising the Pt and SAPO-11 of the invention is also demonstrated. 1) A process comprising:{'sub': 2', '5', '2', '3, '(i) stirring an alumina source and POsource in an aqueous medium in the presence of at least one crystallization template, and combining same with a silica source in the presence of a surfactant and an organic solvent, wherein the molar ratio surfactant: AlOis equal to or higher than 0.55, and increasing the amount of water in the reaction mixture as the reaction advances, to form a gel;'}(ii) hydrothermally crystallizing the so-formed gel, to form a powder; and(iii) calcining said powder and collecting a solid consisting essentially of SAPO-11.2) A process according to claim 1 , wherein the molar ratio surfactant: AlOis from 0.56 to 0.63 claim 1 , inclusive.3) A process according to claim 2 , wherein the gel formation reaction of step (i) comprises stirring the alumina source and the P2O5 source in a first amount of water (w1) claim 2 , adding at least one crystallization template claim 2 , allowing the mixture to stand under stirring claim 2 , introducing the surfactant claim 2 , the organic solvent and a second amount of water (w2) to the reaction mixture claim 2 , with the silica source and a third amount of water (w3) being lastly added with further stirring claim 2 , to form the gel.4) A process according to claim 3 , wherein the weight ratios wl1:w2:w3 are in the range from 1:0.4-0.6:0.8-1.2.5) ...

SERVER, METHOD, AND PROGRAM FOR SUPPLYING DESULFURIZATION CATALYST-RELATED INFORMATION, AND COMPUTER-READABLE RECORDING MEDIUM RECORDING SAME

A server is configured to be connected to a user terminal via a network, and to supply a desulfurization catalyst lifetime of a user plant to a user based on desulfurization catalyst pilot plant data and a desulfurization catalyst lifetime function. The server includes a processor and a memory storing computer-readable instructions. When the computer-readable instructions are executed by the processor, the server receives user plant-related data and a user desulfurization catalyst performance prediction condition from the user terminal to the user plant based on a comparison between the desulfurization catalyst pilot plant data and the obtained user plant-related data, calculates a catalyst lifetime for the user's desulfurization catalyst based on the obtained user desulfurization catalyst performance prediction condition and the user desulfurization catalyst lifetime function, and transmits the calculated catalyst lifetime to the user terminal. 1. A server to be connected to a user terminal via a network to supply a desulfurization catalyst lifetime of a user plant to a user based on desulfurization catalyst pilot plant data and a desulfurization catalyst lifetime function , the server comprising:a processor and a memory storing computer-readable instructions,wherein, when the computer-readable instructions are executed by the processor, the serverreceives user plant-related data and a user desulfurization catalyst performance prediction condition from the user terminal,generates from the desulfurization catalyst lifetime function a user desulfurization catalyst lifetime function tailored to the user plant based on a comparison between the desulfurization catalyst pilot plant data and the received user plant-related data,calculates a catalyst lifetime for a user desulfurization catalyst based on the received user desulfurization catalyst performance prediction condition and the user desulfurization catalyst lifetime function, andtransmits the calculated catalyst ...

PRODUCTION OF UPGRADED EXTRACT AND RAFFINATE

Systems and methods are provided for producing upgraded raffinate and extract products from lubricant boiling range feeds and/or other feeds having a boiling range of 400° F. (204° C.) to 1500° F. (816° C.) or more. The upgraded raffinate and/or extract products can have a reduced or minimized concentration of sulfur, nitrogen, metals, or a combination thereof. The reduced or minimized concentration of sulfur, nitrogen, and/or metals can be achieved by hydrotreating a suitable feed under hydrotreatment conditions corresponding to relatively low levels of feed conversion. Optionally, the feed can also dewaxed, such as by catalytic dewaxing or by solvent dewaxing. Because excessive aromatic saturation is not desired, the pressure for hydrotreatment (and optional dewaxing) can be 500 psig (˜3.4 MPa) to 1200 psig (˜8.2 MPa). 1. A method for forming a raffinate and an extract , comprising:hydrotreating a feedstock having a T5 boiling point of at least 400° F. and a T95 boiling point of 1500° F. or less under hydrotreating conditions comprising less than 15% feed conversion relative to a conversion temperature of 700° F. to form a hydrotreated effluent, the feedstock having a 650° F.+ aromatics content of 25 wt % to 90 wt % and a sulfur content of greater than 1000 wppm, the hydrotreated effluent comprising a hydrotreated effluent fraction having a T5 boiling point of at least 400° F., an aromatics content of at least 10 wt %, a sulfur content of less than 1000 wppm, and a combined amount of Ni, V, and Fe of less than 10 wppm; andperforming a solvent extraction on the hydrotreated effluent fraction to form at least a raffinate product having a nitrogen content of less than 50 wppm and an extract product comprising at least 70 wt % aromatics.2. The method of claim 1 , wherein the raffinate product has a nitrogen content of 10 wppm or less.3. The method of claim 1 , further comprising dewaxing at least a portion of the hydrotreated effluent fraction prior to performing the ...

PROCESS FOR MAXIMIZING XYLENES PRODUCTION FROM HEAVY AROMATICS FOR USE THEREIN

A method for producing xylenes from a heavy reformate feed includes the steps of introducing the heavy reformate feed and a hydrogen feed to a dealkylation reactor, reacting the heavy reformate feed with the hydrogen gas in the presence of the dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, introducing the dealkylation effluent to a splitter unit, separating the dealkylation effluent into a light gas stream, a toluene stream, a benzene stream, a C9 aromatics stream, a C10+ aromatics stream, and a mixed xylene stream in the splitter unit, introducing the toluene stream, the C9 aromatics stream, and a hydrogen stream into a transalkylation reactor, reacting the toluene stream and the C9 aromatics stream in the presence of the transalkylation catalyst to produce a transalkylation effluent, introducing the transalkylation effluent to the splitter unit, and separating the transalkylation effluent in the splitter unit. 1. A method for producing mixed xylenes from a heavy reformate feed , the method comprising the steps of: A method for producing mixed xylenes from a heavy reformate feed , the method comprising the steps of:introducing the heavy reformate feed and a hydrogen feed to a dealkylation reactor, wherein the dealkylation reactor comprises a dealkylation catalyst, wherein the heavy reformate comprises toluene and aromatic hydrocarbons with nine or more carbon atoms (C9+ aromatics), wherein the hydrogen feed comprises hydrogen gas;reacting the heavy reformate feed with the hydrogen gas in the presence of the dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, wherein the dealkylation reactor is at a dealkylation temperature, wherein the dealkylation reactor is at a dealkylation pressure, wherein the dealkylation reactor has a liquid hourly space velocity;introducing the dealkylation effluent to a splitter unit, where the dealkylation effluent comprises light gases, toluene, benzene, mixed ...

Heavy Oil Hydrotreating System and Heavy Oil Hydrotreating Method

A heavy oil hydrotreating system has a prehydrotreating reaction zone, a transition reaction zone, and a hydrotreating reaction zone that are connected in series successively, sensor units, and a control unit. In the initial reaction stage, the prehydrotreating reaction zone includes at least two prehydrotreating reactors connected in parallel, and the transition reaction zone includes or doesn't include prehydrotreating reactors; in the reaction process, the control unit controls material feeding to and material discharging from each prehydrotreating reactor in the prehydrotreating reaction zone according to pressure drop signals of the sensor units, so that when the pressure drop in any of the prehydrotreating reactors in the prehydrotreating reaction zone reaches a predetermined value, the prehydrotreating reactor in which the pressure drop reaches the predetermined value is switched from the prehydrotreating reaction zone to the transition reaction zone.

CATALYST WITH IMPROVED ACTIVITY/SELECTIVITY FOR LIGHT NAPHTHA AROMATIZATION

In an aspect, a method for the aromatization of hydrocarbons comprises contacting a hydrocarbon feedstream with a catalyst; wherein the catalyst comprises a zeolite comprising Si, Al, and Ge in the framework with Pt deposited thereon; wherein the zeolite further comprises Na; and wherein the catalyst has an Si:Almole ratio of greater than or equal to 125, an Si:Ge mole ratio of 40 to 400, and an Na:Al mole ratio of 0.9 to 2.5, wherein the catalyst has an aluminum content of less than or equal to 0.75 wt % excluding any binder and extrusion aide. 1. A method for the aromatization of hydrocarbons comprising:contacting a hydrocarbon feedstream with a catalyst;wherein the catalyst comprises a zeolite comprising Si, Al, and Ge in the framework with Pt deposited thereon; wherein the zeolite further comprises Na; and{'sub': '2', 'wherein the catalyst has an Si:Almole ratio of greater than or equal to 125, an Si:Ge mole ratio of 40 to 400, and an Na:Al mole ratio of 0.9 to 2.5, wherein the catalyst has an aluminum content of less than or equal to 0.75 wt % excluding any binder and extrusion aide.'}2. The method of claim 1 , wherein the hydrocarbon feedstream comprises an olefinic compound.3. The method of claim 1 , wherein the hydrocarbon feedstream comprises an alkane compound.4. The method of claim 3 , wherein the alkane compound comprises a Calkane.5. The method of claim 3 , wherein the alkane compound comprises a Calkane.6. The method of claim 5 , wherein the feed stream comprises 20 to 100 vol % of at least one of the C claim 5 , C claim 5 , or Calkane.7. The method of claim 1 , wherein the hydrocarbon feedstream comprises naphthene.8. The method of claim 1 , wherein the hydrocarbon feedstream comprises a naphtha feed.9. The method of claim 8 , wherein the naphtha feed comprises up to 1 claim 8 ,000 parts per million by weight sulfur and/or up to 100 parts per million by weight of nitrogen compounds.10. The method of claim 1 , wherein the Ge is present in an amount of ...

COMPOSITION FOR OPENING POLYCYCLIC RINGS IN HYDROCRACKING

A catalyst composition comprising a support comprising a mixture of amorphous silica-alumina and non-zeolitic alumina comprising no more than 75 wt % amorphous silica-alumina and having a ratio of moles of silicon to moles of aluminum in the range of about 0.05 to about 0.50. A first hydrogenation metal comprising platinum, a second hydrogenation metal from Group VIIB or Group VIII of the Periodic Table other than platinum and an optional third metal from Group IA of the Periodic Table may be deposited on the support. The ratio of moles of silicon to the moles of the first hydrogenation metal, the second hydrogenation metal and the optional third metal on the support may be between about 15 and about 75. 1. A catalyst composition comprising:a support comprising a mixture of amorphous silica-alumina and non-zeolitic alumina comprising no more than 75 wt % amorphous silica-alumina and having a ratio of moles of silicon to moles of aluminum in the range of about 0.05 to about 0.50;a first hydrogenation metal comprising platinum;a second hydrogenation metal from Group VIIB or Group VIII of the Periodic Table other than platinum;an optional third metal from Group IA of the Periodic Table;wherein the first hydrogenation metal, the second hydrogenation metal and the optional third metal are deposited on the support; andthe ratio of moles of silicon to the moles of the first hydrogenation metal, the second hydrogenation metal and the optional third metal on the support is between about 15 and about 55 or between about 55 and about 75 with a ratio of moles of the second hydrogenation metal to the first hydrogenation metal of less than 1.5.2. The composition of wherein the overall mole ratio of silicon to aluminum in the support is no more than 0.20.3. The composition of wherein the amorphous silica-alumina has a mole ratio of silicon to aluminum of about 0.1 to about 1.0 in the support.4. The composition of wherein the mole ratio of the second hydrogenation metal to the ...

Pyrolysis Tar Conversion

This invention relates to a process for determining the suitability of pyrolysis tar, such as steam cracker tar, for upgrading using hydroprocessing without excessive fouling of the hydroprocessing reactor. A pyrolysis tar is sampled, the sample is analyzed to determine one or more characteristics of the tar related to tar reactivity, and the analysis is used to determine conditions under which the tar can be blended, pre-treated, and/or hydroprocessed. 1. A hydrocarbon conversion process , comprising: (i) the first pyrolysis tar contains free radicals and', '(ii) at least 70 wt. % of the first pyrolysis tar has a normal boiling point of at least 290° C.;, '(a) providing a first pyrolysis tar, wherein,'}{'sub': 'T', '(b) isolating a sample from the first pyrolysis tar and measuring a reactivity Rof the sample;'}{'sub': T', 'Ref, 'claim-text': [{'sub': T', 'Ref, '(i) when Ris less than or equal to a predetermined reference reactivity R, carrying out the hydroprocessing of step (d); or'}, {'sub': T', 'Ref, 'claim-text': [{'sub': HS', 'HS', 'HS', 'HS', 'HS, '(A) heating the first pyrolysis tar to achieve a temperature Tand maintaining the first pyrolysis tar at a temperature in a range of from Tto 360° C. for a time of time tto produce a pyrolysis tar composition, wherein Tis in the range of from 150° C. to 350° C. and tis ≥1 minute,'}, {'sub': 'T', '(B) isolating a sample from the pyrolysis tar composition and measuring the reactivity Rof the pyrolysis tar composition sample, and'}, '(C) repeating step (c); and, '(ii) when Ris greater than a predetermined reference reactivity R,'}], '(c) comparing Rto a predetermined reference reactivity R, wherein,'}(d) hydroprocessing at least a portion of the pyrolysis tar composition to produce a hydroprocessor effluent comprising hydroprocessed pyrolysis tar.2. (canceled)3. The process of claim 1 , wherein (i) Rand Rare determined by a Bromine Number measurement and expressed in BN units claim 1 , (ii) Ris ≤20 BN claim 1 , and ( ...

METHOD OF DOSING A SYSTEM WITH HCL THEN EVACUATING AND PURGING

A method of dosing a system with HCL is provided. The method includes at least two parallel trains. The method utilizes a first operating mode, wherein at least one primary train is actively providing HCL to an end user, and at least one secondary train is either inactive or also providing HCL to the end user. The method utilizes a second operating mode, wherein the least one primary train is evacuating the contents of the train to a disposal system, and the at least one secondary train is providing HCL to the end user. And the system utilizes a third operating mode, wherein the at least one primary train is purging the train, and the at least one secondary train is providing HCL to the end user. The first operating mode, the second operating mode, and the third operating mode are controlled by an electronic monitoring and control system. 2. The method of claim 1 , wherein the electronic monitoring and control system comprises a distributed control system or a programmable logic controller.3. The method of claim 1 , wherein during the first operating mode the at least one secondary train is inactive.4. The method of claim 1 , wherein during the first operating mode the at least one secondary train is omitted.5. The method of claim 1 , further comprising an active circuit claim 1 , the active circuit comprising:at least one first isolation block valve fluidically connected to at least one HCL cylinder or bulk container by way of a common manifold assembly,at least one second isolation block valve fluidically connected to the at least one first isolation block valve and an automatically controlled, dosing valve,a flow rate and total flow measuring device fluidically connected to the automatically controlled, dosing valve and an adjustable flow rate control valve, anda gas outlet to the system to be acidified fluidically connected to the adjustable flow control valve.6. The method of claim 5 , further comprising one or more heating devices configured to apply heat to ...

METHOD FOR PREPARATION OF NANOCERIA SUPPORTED ATOMIC NOBLE METAL CATALYSTS AND THE APPLICATION OF PLATINUM SINGLE ATOM CATALYSTS FOR DIRECT METHANE CONVERSION

Described are methods for converting methane to olefins, aromatics, or a combination thereof using a single atom catalyst comprising CeOnanoparticles impregnated with individual atoms of noble metals including Pt, Pd, Rh, Ru, Ag, Au, Ir, or a combination thereof. These single atom catalysts of the present invention are heated with methane to form olefins and aromatics. 1. A method for converting methane to olefins , aromatics , or a combination thereof comprising the following steps:{'sub': '2', 'providing a single atom catalyst comprising CeOnanoparticles impregnated with a noble metal atom;'}adding methane;increasing the temperature to in the range of 700° C. to 1200° C.; andforming olefins, aromatics, or a combination thereof.2. The method of wherein the single atom catalyst are preheated heated in the range of 15° C. to 500° C. prior to the addition of methane.3. The method of further comprising heating the single atom catalyst at the temperature in the range of 700° C. to 1200° C. for 30 minutes to 2 hours.4. The method of further comprising heating the single atom catalyst in a bed flow reactor.5. The method of wherein increasing the temperature to 900° C.6. The method of further comprising the step of increasing the temperature to 1000° C.7. The method of having a methane conversion in the range of 10% to 30%.8. The method of having a coke selectivity below than 15%.9. The method of having a Cproductivity of greater than 50%.10. The method of wherein the noble metal atom is selected from the group consisting of Pt claim 1 , Pd claim 1 , Rh claim 1 , Ru claim 1 , Ag claim 1 , Au claim 1 , Ir claim 1 , or a combination thereof.11. The method of wherein the noble metal atom comprises Pt.12. The method of making a single atom catalyst comprising the steps of:{'sub': 3', '3, 'dissolving Ce(NO)with a noble metal or a precursor of a noble metal in water and an organic surfactant selected from the group comprising ethylene glycol, propionic acid, or a combination ...

TRANSITION METAL TUNGSTATE MATERIAL

A hydroprocessing catalyst or catalyst precursor has been developed. The catalyst is a transition metal tungstate material or metal sulfides derived therefrom. The hydroprocessing using the crystalline ammonia transition metal tungstate material may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking. 2. The transition metal tungstate material of wherein the transition metal tungstate material is present in a mixture with at least one binder and wherein the mixture comprises up to 25 wt-% binder.3. The transition metal tungstate material of wherein the binder is selected from the group consisting of silicas claim 2 , aluminas claim 2 , and silica-aluminas.4. The transition metal tungstate material of wherein M is nickel or cobalt.5. The transition metal tungstate material of wherein M is nickel.7. The method of further comprising removing at least some of the NH claim 6 , the HO claim 6 , or the combination thereof to form an intermediate before reacting the mixture at a temperature from about 50° C. to about 250° C. in an autogenous environment.8. The method of wherein the reacting is conducted at a temperature of from 50° C. to about 250° C. for a period of time from about 30 minutes to 14 days.9. The method of wherein the recovering is by filtration or centrifugation.10. The method of further comprising drying the recovered transition metal tungstate material at a temperature from about 100° C. to about 350° C. for about 30 minutes to about 48 hours.11. The method of further comprising adding a binder to the recovered transition metal tungstate material.12. The method of wherein the binder is selected from the group consisting of aluminas claim 11 , silicas claim 11 , and alumina-silicas.13. The method of further comprising decomposing the recovered transition metal tungstate material by sulfidation to form metal sulfides.15. The process ...

Multi-step hydrodesulphurization process

Liquid sulphur-containing hydrocarbon feedstock is passed through two or more hydrodesulfurization zones and connected in a series each containing a packed bed of solid sulfurized catalyst. The liquid is passed from the first zone to the next until the final zone. Make up hydrogen is supplied to a hydrodesulfurization zone (i) other than the first hydrodesulfurization zone; hydrogen-containing gas is recovered from each hydrodesulfurization zone. The first hydrodesulfurization zone is supplied with hydrogen-containing gas recovered from a subsequent hydrodesulfurization zone. Hydrogen-containing gas recovered from the first hydrodesulfurization zone is purged. Liquid material recovered from the first hydrodesulfurization zone is recycled to the inlet of the hydrosulfurization zone so as to provide diluent for admixture with liquid feedstock. Any other hydrodesulfurization zone other than the first hydrodesulfurization zone and other than the hydrodesulfurization zone of step (i) is supplied with hydrogen-containing gas recovered from another hydrodesulfurization zone. The sulfur content of the hydrogen-containing gas and of the liquid hydrocarbon feedstock supplied to the first hydrodesulfurization zone is monitored and, if necessary, sulfur-containing material selected from hydrogen sulfide and active sulfur-containing materials is supplied to the first hydrodesulfurization zone so as to maintain the catalyst charge thereof in sulfided form.

Hydrodesulphurisation process

A hydrodesulphurisation process for continuously effecting hydrodesulphurisation of a liquid sulphur-containing hydrocarbon feedstock comprises: (a) providing a plurality of hydrodesulphurisation zones connected in series each containing a packed bed of a solid sulphided hydrodesulphurisation catalyst, said plurality of hydrodesulphurisation zones including a first hydrodesulphurisation zone and at least one other hydrodesulphurisation zone including a final hydrodesulphurisation zone; (b) maintaining temperature and pressure conditions in each hydrodesulphurisation zone effective for hydrodesulphurisation of the liquid feedstock; (c) supplyinmg liquid sulphur-containing hydrocarbon feedstock to the first hydrodesulphurisation zone; (d) passing the liquid feedstock through the plurality of hydrodesulphurisation zones in turn from the first hydrodesulphurisation zone to the final hydrodesulphurisation zone; (e) passing hydrogen-containing gas through the hydrodesulphurisation zones from one zone to another; (f) contacting the liquid feedstock with hydrogen under hydrodesulphurisation conditions in each hydrodesulphurisation zone in the presence of the respective charge of hydrodesulphurisation catalyst; and which further comprises: (i) supplying make up hydrogen to a hydrodesulphurisation zone other than the first hydrodesulphurisation zone; (ii) recovering a hydrogen-containing gas from each hydrodesulphurisation zone; (iii) supplying the first hydrodesulphurisation zone with hydrogen-containing gas recovered from a subsequent hydrodesulphurisation zone; (iv) purging hydrogen-containing gas recovered from the first hydrodesulphurisation zone; (v) supplying any other hydrodesulphurisation zone other than the first hydrodesulphurisation zone and other than the hydrodesulphurisation zone of step (i) with hydrogen-containing gas recovered from another hydrodesulphurisation zone; (vi) monitoring the sulphur content of the hydrogen-containing gas and of the liquid ...

Method and Apparatus for Predicting Properties of Feed and Products in Reformer

Disclosed are a method and apparatus of predicting properties of feed and products in a reformer. The method of predicting properties of feed and products in a reformer includes training a first predictive model for predicting the properties of feed in the reformer and a second predictive model for predicting the properties of products in the reformer; predicting the properties of feed being currently supplied to the reactor in real time by allowing a first prediction unit including the trained first prediction model to receive a current operating condition of the reactor in the reformer; and predicting the properties of products being produced in the reactor in real time by allowing a second prediction unit including the trained second prediction model to receive the current operating condition and the predicted properties of feed. 1. A method of predicting properties of feed and products in a reformer , comprising the steps of:training a first predictive model for predicting the properties of feed in the reformer and a second predictive model for predicting the properties of products in the reformer;predicting the properties of feed being currently supplied to the reactor in real time by allowing a first prediction unit including the trained first prediction model to receive a current operating condition of the reactor in the reformer; andpredicting the properties of products being produced in the reactor in real time by allowing a second prediction unit including the trained second prediction model to receive the current operating condition and the predicted properties of feed.2. The method of claim 1 , wherein the first prediction model is trained by using claim 1 , as training data claim 1 , experimental values for the properties of feed supplied to the reactor claim 1 , a past operating condition of the reactor claim 1 , and a difference in temperature between front and rear ends of the reactor.3. The method of claim 1 , wherein the second prediction model is ...

Methods of regenerating aromatization catalysts

Methods for treating or rejuvenating a spent catalyst are described. These methods can employ a step of halogenating the spent catalyst, followed by decoking the halogenated spent catalyst. The halogenation step can utilize fluorine and chlorine together, or fluorine and chlorine can be applied sequentially.

Control system method and apparatus for continuous liquid phase hydroprocessing

A continuous liquid phase hydroprocessing process, apparatus and process control systems, where the need to circulate hydrogen gas through the catalyst is eliminated. By mixing and/or flashing the hydrogen and the oil to be treated in the presence of a solvent or diluent in which the hydrogen solubility is high relative to the oil teed, all of the hydrogen required in the hydroprocessing reactions may be available in solution. The oil/diluent/hydrogen solution can then be fed to a plug flow reactor packed with catalyst where the oil and hydrogen react. No additional hydrogen is required; therefore, the large trickle bed reactors can be replaced by much smaller tubular reactors. The amount of hydrogen added to the reactor can be used to control the liquid level in the reactor or the pressure in the reactor. (FIG. 6)

水素化精製触媒及び炭化水素油の製造方法

　本発明の水素化精製触媒は、固体酸性を有する非晶性複合金属酸化物を含む担体と、前記担体に担持された周期表第８族～第１０族の貴金属から選択される少なくとも一種の活性金属と、を含有してなる水素化精製触媒であって、水素化精製触媒は炭素原子を含む炭素質物質を含有し、水素化精製触媒における炭素質物質の含有量が炭素原子換算で０．０５～１質量％である。

Heat exchangers in a petrochemical plant or refinery

A plant or refinery may include equipment such as reactors, heaters, heat exchangers, regenerators, separators, or the like. Types of heat exchangers include shell and tube, plate, plate and shell, plate fin, air cooled, wetted-surface air cooled, or the like. Operating methods may impact deterioration in equipment condition, prolong equipment life, extend production operating time, or provide other benefits. Mechanical or digital sensors may be used for monitoring equipment, and sensor data may be programmatically analyzed to identify developing problems. For example, sensors may be used in conjunction with one or more system components to detect and correct maldistribution, cross-leakage, strain, pre-leakage, thermal stresses, fouling, vibration, problems in liquid lifting, conditions that can affect air-cooled exchangers, conditions that can affect a wetted-surface air-cooled heat exchanger, or the like. An operating condition or mode may be adjusted to prolong equipment life or avoid equipment failure.

Detecting and correcting thermal stresses in heat exchangers in a petrochemical plant or refinery

A plant or refinery may include equipment such as reactors, heaters, heat exchangers, regenerators, separators, or the like. Types of heat exchangers include shell and tube, plate, plate and shell, plate fin, air cooled, wetted-surface air cooled, or the like. Operating methods may impact deterioration in equipment condition, prolong equipment life, extend production operating time, or provide other benefits. Mechanical or digital sensors may be used for monitoring equipment, and sensor data may be programmatically analyzed to identify developing problems. For example, sensors may be used in conjunction with one or more system components to detect and correct maldistribution, cross-leakage, strain, pre-leakage, thermal stresses, fouling, vibration, problems in liquid lifting, conditions that can affect air-cooled exchangers, conditions that can affect a wetted-surface air-cooled heat exchanger, or the like. An operating condition or mode may be adjusted to prolong equipment life or avoid equipment failure.

Early surge detection of rotating equipment in a petrochemical plant or refinery

A plant or refinery may include equipment such as condensers, regenerators, distillation columns, rotating equipment, compressors, pumps, turbines, or the like. Different operating methods may impact deterioration in equipment condition, thereby prolonging equipment life, extending production operating time, or providing other benefits. Mechanical or digital sensors may be used for monitoring equipment to determine whether problems are developing. For example, sensors may be used in conjunction with one or more system components to perform invariant mapping, monitor system operating characteristics, and/or predict pressure, volume, surges, reactor loop fouling, gas quality, or the like. An operating condition (e.g., of one or more pieces of equipment in the plant or refinery) may be adjusted to prolong equipment life or avoid equipment failure.

Incipient temperature excursion mitigation and control

Systems and methods are disclosed for detecting temperature excursion in a chemical plant or petrochemical plant or refinery. Aspects of the disclosure provide an enhanced control system for a reactor, such as in hydroprocessing. The enhanced control system may provide early warnings of impending undesirable events, directly or indirectly manipulate certain process variables to reduce undesirable outcomes, and/or directly or indirectly manipulate of certain process variables so as to place a reactor unit in a “safe park” state. This may avoid a high temperature trip, depressuration, associated operating risks, allow for faster recovery from temperature excursions, and/or avoid unplanned emergency shutdowns of the reactor, chemical process, plant, or refinery.

System and method to optimize crude oil distillation or other processing by inline analysis of crude oil properties

An apparatus includes at least one processor configured to obtain inline measurements of one or more properties of crude oil, translate the measurements into a set of process and control parameters, and apply the process and control parameters to process equipment. The process and control parameters configure the process equipment to process the crude oil having the one or more properties. The one or more properties of the crude oil may include at least one of: density, specific gravity, viscosity, carbon residue, and sulfur content of the crude oil. The process and control parameters could be applied to one or more controllers associated with a blending unit in a refinery or to one or more controllers associated with a crude oil distillation column in the refinery.

Molecular sieve ssz-74 composition of matter and synthesis thereof

The present invention relates to new crystalline molecular sieve SSZ- 74 prepared using a hexamethylene-1 ,6-bis-(N-methyl-N-pyrrolidinium) dication as a structure-directing agent, methods for synthesizing SSZ-74, and its use in hydrocarbon conversion reactions, reduction of oxides of nitrogen in a gas stream, partial oxidation reactions, acylation reactions, oxygenate conversions, gas separations, synthesis of amines, treatment of engine exhaust (reduction of cold start emissions), and Beckmann rearrangement.

Methods of regenerating aromatization catalysts

FIELD: chemistry. SUBSTANCE: invention discloses and describes methods for treating or regenerating spent catalysts containing a transition metal and a catalyst substrate, reforming methods, and a regenerated catalyst produced by the said methods. The method for treating the spent catalyst comprises: (1) contacting the spent catalyst with a halogen-containing stream containing chlorine and fluorine to produce a halogenated spent catalyst. The halogen-containing stream contains less than 100 ppm weight of the oxygen-containing compounds; (2) contacting the halogenated spent catalyst with a purge stream containing essentially inert gas; and (3) contacting the halogenated spent catalyst with a coke-removal gas stream containing oxygen; where the stream of coke oven gas contains less than 50 ppm weight of the halogenated compounds after step (2). Another method of treating the catalyst comprises: (i) bringing the spent catalyst into contact with a halogen-containing stream containing chlorine and fluorine to produce a halogenated spent catalyst; and (ii) bringing the halogenated spent catalyst into contact with a coke oven gas stream containing oxygen after step (i). In the halogenation step, fluorine and chlorine can be used together, or fluorine and chlorine can be used sequentially. The reforming method comprises: (a) bringing the hydrocarbon feed into contact with the aromatization catalyst under reforming conditions in the reactor system to produce an aromatic product; (b) carrying out step (a) for a period of time sufficient to form a spent aromatization catalyst; (c) bringing the spent aromatization catalyst into contact with a halogen-containing stream containing chlorine and fluorine to produce a halogenated spent catalyst; and (d) bringing the halogenated spent catalyst into contact with a coke oven gas stream containing oxygen. EFFECT: spent catalyst, which was initially halogenated, has a significantly lower start-up temperature than the spent catalyst, ...

METHOD OF AROMATIZATION OF METHANE-CONTAINING GAS FLOW

Способ ароматизации метансодержащего газового потока, содержащий этап, на котором приводят в контакт метансодержащий газовый поток в реакторе с псевдоожиженным слоем, содержащим катализатор ароматизации и акцептор водорода, в условиях ароматизации метансодержащего газа, чтобы получить поток продукта, содержащий ароматические соединения и водород, причем водород, по меньшей мере, частично связывается акцептором водорода в реакционной зоне и отводится из продукта и реакционной зоны. A method for aromatizing a methane-containing gas stream, comprising the step of contacting a methane-containing gas stream in a fluidized bed reactor containing an aromatization catalyst and a hydrogen scavenger under aromatization conditions for the methane-containing gas to obtain a product stream containing aromatic compounds and hydrogen, wherein hydrogen, is at least partially bound by a hydrogen scavenger in the reaction zone and removed from the product and reaction zone.

Система управления, способ и устройство для непрерывной жидкофазной гидропереработки

Изобретение относится к гидропереработке нефтяного сырья. Изобретение касается способа непрерывной жидкофазной гидропереработки с использованием реактора, который в установившемся режиме работает при заданной температуре и имеет верхнюю зону для газа и нижнюю зону значительно большего размера для водорода, растворенного в смеси жидкостей, окружающих катализатор, при этом упомянутые жидкости сводят к минимуму колебания упомянутой заданной температуры. За счет смешивания и/или мгновенного испарения водорода и очищаемой нефти в присутствии растворителя или разбавителя, в котором растворимость водорода является высокой по сравнению с нефтяным сырьем, весь водород, необходимый для реакций гидроочистки, может быть доступен в виде раствора. Затем раствор нефти/разбавителя/водорода загружают в реактор идеального вытеснения, который заполнен катализатором, где и происходит реакция нефти и водорода. Добавляемый в реактор водород может использоваться для регулирования уровня жидкости или давления в реакторе. Также изобретение касается реактора системы непрерывной жидкофазной гидропереработки. Технический результат - крупные реакторы с орошаемым слоем могут быть заменены реакторами гораздо меньших размеров, поскольку нет необходимости добавлять водород, улучшено регулирование температуры в реакторе, практически исключено закоксовывание катализатора, уменьшено образование легких углеводородов. 3 н. и 12 з.п. ф-лы, 19 ил. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 411 285 (13) C2 (51) МПК C10G 47/00 C10G 45/02 (2006.01) (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2007137780/04, 23.03.2006 (24) Дата начала отсчета срока действия патента: 23.03.2006 (72) Автор(ы): АКЕРСОН Майкл Д. (US), БЬЯРС Майкл (US) R U (73) Патентообладатель(и): Е.И.Дю Пон де Немур энд Компани (US) Приоритет(ы): (30) Конвенционный приоритет: 24.03.2005 US 11/089,477 (43) Дата публикации заявки: 27.04.2009 Бюл. № 12 2 4 ...

分子ふるいｓｓｚ−７４組成物及びその合成

用于乙烷转化成芳烃的方法

一种用于生产芳烃的方法，该方法包括：(a)使乙烷与脱氢芳构化催化剂接触，所述催化剂包含0.005-0.1wt％的铂、含量低于铂的量不超过0.02wt％的钝化金属、10-99.9wt％的铝硅酸盐和粘合剂，和(b)从步骤(a)的反应产物中分离甲烷、氢和C2-5烃以生产包含苯的芳烃反应产物。

Hydrogenation method and device

FIELD: oil and gas industry.SUBSTANCE: present invention relates to reactions of hydrogenation of different fractions in oil processing. Invention discloses a method of hydrogenating a hydrocarbon stream containing olefinic compounds, aromatic compounds or a combination thereof, involving the following steps: I) supply of hydrocarbon stream and hydrogen into first reaction zone of hydrogenation unit, II) hydrogenating, in a first reaction zone, at least a portion of aromatic compounds, olefin compounds or a combination thereof in the presence of a catalyst to obtain a first intermediate product, III) cooling and separating the first intermediate product into a first intermediate liquid stream and a first intermediate gas stream, IV) displacement first intermediate gas stream to second reaction zone of hydrogenation unit, V) separating the first intermediate liquid stream into a first portion of the first intermediate liquid stream and a second portion of the first intermediate liquid stream and a) moving the first portion of the first intermediate liquid stream to the inlet of the first reaction zone as a liquid recycle stream to limit temperature rise in the first reaction zone to less than 60 °C and b) moving a second portion of the first intermediate liquid stream to a second reaction zone, where remaining aromatic compounds, olefin compounds or a combination thereof, contained in the second portion of the first intermediate liquid stream, is hydrogenated by means of a first intermediate gas stream in the presence of a catalyst to obtain a saturated product or c) moving the second portion of the first intermediate liquid stream into the liquid bypass line which bypasses the second reaction zone, wherein the second portion of the first intermediate liquid stream comprises a saturated product, VI) separating a saturated product obtained in step b) or c) into a liquid product stream and separated gas stream, VII) extraction of liquid product stream from ...

生产芳烃和烯烃的方法

本公开的主题提供了由焦化石脑油产生烯烃和/或芳烃的方法。在非限制性实施方案中，用于产生芳烃的方法包括在第一催化剂的存在下氢化焦化石脑油流以除去二烯烃和硫(如果存在)，以获得氢化流，并在第二催化剂的存在下使氢化流经历芳构化，以产生包含苯、甲苯和二甲苯的富含芳烃的流。在某些实施方案中，用于产生烯烃的方法包括在第一催化剂的存在下氢化焦化石脑油流以除去二烯烃和硫(如果存在)，以获得氢化流，并在第二催化剂的存在下使氢化流经历催化裂化，以产生包含乙烯、丙烯和芳烃的富含烯烃的流。

一种加氢精制中氢解程度的实时预测方法及其系统

本发明提供一种加氢精制过程中含硫和/或氮的化合物的氢解程度的实时预测方法及其系统，所述方法包括：基于所述过程的当前操作条件，利用极限学习机ELM模型实时预测所述过程中含硫和/或氮的化合物的氢解程度。本发明根据加氢裂化流程在线可检测的过程变量利用ELM实时预测加氢精制过程含硫和/或氮的化合物的氢解程度，可为加氢裂化流程精制反应器的运行优化提供重要的状态信息。

Способ регенерации загрязненного серой катализатора ароматизации

Изобретение относится к способу регенерации загрязненного серой катализатора, содержащего переходный металл и подложку катализатора, содержащую цеолит L-типа, включающему промывку загрязненного серой катализатора водным раствором, причем водный раствор, необязательно, содержит щелочной металл, для получения промытого катализатора; приведение в контакт промытого катализатора с раствором галогена, содержащим хлорсодержащее соединение и фторсодержащее соединение, с получением галогенированного катализатора; и прокаливание галогенированного катализатора. Изобретение касается также способа риформинга углеводородного сырья. Технический результат - улучшенное восстановление каталитической активности загрязненных серой катализаторов ароматизации. 2 н. и 58 з.п. ф-лы, 1 табл., 5 пр., 8 ил. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 739 556 C1 (51) МПК B01J 38/54 (2006.01) B01J 38/64 (2006.01) B01J 37/06 (2006.01) B01J 37/24 (2006.01) B01J 37/26 (2006.01) C10G 35/095 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 38/54 (2020.08); B01J 38/64 (2020.08); B01J 37/06 (2020.08); B01J 37/24 (2020.08); B01J 37/26 (2020.08); C10G 35/095 (2020.08) (21)(22) Заявка: 2019118902, 14.12.2017 14.12.2017 (73) Патентообладатель(и): ШЕВРОН ФИЛЛИПС КЕМИКАЛ КОМПАНИ ЭлПи (US) Дата регистрации: 25.12.2020 20.12.2016 US 15/384,353 (45) Опубликовано: 25.12.2020 Бюл. № 36 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 22.07.2019 (86) Заявка PCT: 2 7 3 9 5 5 6 (56) Список документов, цитированных в отчете о поиске: US 5260238 A1, 09.11.1993. WO 8602861 A1, 22.05.1986. US 6190539 B1, 20.02.2001. US 20100160147 A1, 24.06.2010. US 4987109 A1, 22.01.1991. US 20090156871 A1, 18.06.2009. US 5155074 A1, 13.10.1992. RU 2486008 C2, 27.06.2013. RU 2580553 C2, 10.04.2016. Приоритет(ы): (30) Конвенционный приоритет: R U (24) Дата начала отсчета срока действия патента: (72) Автор(ы): СНЕЛЛ, Райан (US) 2 7 3 9 5 5 6 R U (87) Публикация ...

由可再生原料控制生产运输燃料

用于控制由可再生原料如植物油和动物油同时生产柴油范围烃和航空范围烃二者的方法。该方法包括确定期望产物的所需规格以及仍满足所述规格的产物期望的相对产率。为了形成满足所需产物规格和产率的链烷烃混合物，确定必要的异构化和选择性加氢裂化区条件。确定必要的分馏区条件以分离期望的产物。将可再生原料(2)通过氢化和脱氧(4)进行处理以提供包含链烷烃的流出物(6)，在预定条件下将至少一部分链烷烃异构化和选择性氢化(22)，并在预定分馏条件下通过分馏(42)进行分离，由此产生柴油范围烃产物(46)和航空范围烃产物(45)。

Method for producing regenerated hydrotreating catalyst and method for producing petroleum product

【課題】 使用済みの水素化処理用触媒から、安定して高い活性を有する再生水素化処理用触媒を製造可能な、再生水素化処理用触媒の製造方法を提供すること、及び再生水素化処理用触媒を用いた、経済的な石油製品の製造方法を提供すること。 【解決手段】 使用済み水素化処理用触媒を、所定の温度範囲で再生処理する再生水素化処理用触媒の製造方法であって、前記所定の温度範囲は、前記使用済み水素化処理用触媒を示差熱分析し、１００℃以上６００℃以下の測定温度領域における示差熱量を起電力の差に換算した値を温度で２回微分した場合の最小の極値及び２番目に小さい極値のうち、低温側の極値に対応する温度をＴ１、高温側の極値に対応する温度をＴ２としたときに、Ｔ１−３０℃以上Ｔ２＋３０℃以下の温度範囲であることを特徴とする再生水素化処理用触媒の製造方法。 【選択図】なし 【Task】 To provide a method for producing a regenerated hydrotreating catalyst capable of producing a regenerated hydrotreating catalyst having high activity stably from a spent hydrotreating catalyst, and to provide a regenerated hydrotreating catalyst. To provide an economical method for producing petroleum products. [Solution] A method for producing a regenerated hydrotreating catalyst for regenerating a used hydrotreating catalyst within a predetermined temperature range, wherein the predetermined temperature range is obtained by performing differential thermal analysis on the used hydrotreating catalyst. Of the minimum extreme value and the second smallest extreme value when the value obtained by converting the differential calorific value in the measurement temperature range of 100 ° C. to 600 ° C. into the difference in electromotive force is differentiated by temperature twice, the extreme value on the low temperature side Production of regenerative hydrotreating catalyst characterized in that the temperature range is from T1-30 ° C. to T2 + 30 ° C., where T1 is the temperature corresponding to the value and T2 is the temperature corresponding to the extreme value on the high temperature side. Method. [Selection figure] None

再生氢化处理用催化剂的制造方法及石油制品的制造方法

一种再生氢化处理用催化剂的制造方法，其特征在于，其为将使用后的氢化处理用催化剂在规定的温度范围内进行再生处理的再生氢化处理用催化剂的制造方法，所述规定的温度范围为T 1 -30℃以上且T 2 +30℃以下的温度范围，所述T 1 、T 2 如下定义：对前述使用后的氢化处理用催化剂进行差热分析，将在100℃以上600℃以下的测定温度范围内的差示热量换算成电动势的差，在将该换算后的值用温度进行2次微分时的最小极值及第2小极值之中，将对应低温侧的极值的温度设为T 1 、对应高温侧的极值的温度设为T 2 。

Methods of regenerating aromatization catalysts

Methods for treating or rejuvenating a spent catalyst are disclosed. Such methods can employ a step of halogenating the spent catalyst, followed by decoking the halogenated spent catalyst. The halogenation step can utilize fluorine and chlorine together, or fluorine and chlorine can be applied sequentially.

Methods of regenerating aromatization catalysts

Methods for treating or rejuvenating a spent catalyst are disclosed. Such methods can employ a step of halogenating the spent catalyst, followed by decoking the halogenated spent catalyst. The halogenation step can utilize fluorine and chlorine together, or fluorine and chlorine can be applied sequentially.

Способ изготовления регенерированного катализатора гидроочистки и способ получения нефтехимического продукта

Предложен способ приготовления регенерированного катализатора гидроочистки путем регенерации отработанного катализатора гидроочистки в заданном интервале температур, где заданным интервалом температур является интервал температур от Т 1 - 30°С или более до Т 2 + 30°С или менее, которые определены путем проведения дифференциального термического анализа отработанного катализатора гидроочистки, преобразования дифференциальной теплоты в интервале измерения температуры от 100°С или более до 600°С или менее в разность электродвижущей силы, двукратного дифференцирования преобразованного значения по температуре для того, чтобы получить наименьшее экстремальное значение и второе наименьшее экстремальное значение, и представления температуры, соответствующей экстремальному значению на стороне более низких температур, как Т 1 , и температуры, соответствующей экстремальному значению на стороне более высоких температур, как Т 2 . Также предложены способ получения нефтяного продукта с использованием указанного катализатора и сам регенерированный катализатор. Способ позволяет получить из отработанного катализатора гидроочистки регенерированный катализатор гидроочистки, имеющий неизменно высокую активность. 3 н. и 4 з.п. ф-лы, 5 ил., 1 табл., 4 пр. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 528 375 C2 (51) МПК B01J 38/02 (2006.01) B01J 38/12 (2006.01) C10G 45/08 (2006.01) C07C 5/02 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2012104538/04, 18.06.2010 (24) Дата начала отсчета срока действия патента: 18.06.2010 Приоритет(ы): (30) Конвенционный приоритет: (43) Дата публикации заявки: 20.08.2013 Бюл. № 23 (73) Патентообладатель(и): ДжейЭкс НИППОН ОЙЛ ЭНД ЭНЕРДЖИ КОРПОРЕЙШН (JP) R U 09.07.2009 JP 2009-162949 (72) Автор(ы): КОННО Соуитироу (JP), ИВАНАМИ Йосиму (JP), САХАРА Ватару (JP), КИМУРА Нобухару (JP) (45) Опубликовано: 20.09.2014 Бюл. № 26 068453 A, 25.03.1991 . RU 2358805 C1, 20.06.2009 . WO 2001/002091 A1, 11. ...

CATALYST HYDRAULIC CLEANING AND METHOD OF MANUFACTURING HYDROCARBON

Катализатор гидроочистки согласно настоящему изобретению представляет собой катализатор гидроочистки, включающий носитель катализатора, содержащий аморфный металлооксидный композитный материал, имеющий кислотность в твердом состоянии, и по меньшей мере один активный металл, нанесенный на носитель катализатора и выбранный из благородных металлов групп 8-10 Периодической системы элементов, причем данный катализатор гидроочистки содержит углеродистое вещество, включающее атомы углерода, и содержание углеродистого вещества в катализаторе гидроочистки составляет от 0,05 до 1 мас.% в расчете на массу атомов углерода. The hydrotreating catalyst according to the present invention is a hydrotreating catalyst comprising a catalyst carrier containing an amorphous metal oxide composite material having a solid acidity and at least one active metal supported on the catalyst carrier and selected from noble metals from Groups 8-10 of the Periodic Table of Elements , wherein the hydrotreating catalyst contains a carbonaceous substance containing carbon atoms, and the content of the carbonaceous substance in the hydrotreating catalyst is 0.05 to 1% by weight based on the weight of carbon atoms.

Heavy oil hydrofining system and heavy oil hydrofining method

FIELD: oil and gas industry.SUBSTANCE: present invention relates to the field of hydrofining of heavy oil, in particular to the heavy oil hydrofining system and the heavy oil hydrofining method. Method for heavy oil hydrofining involves mixing heavy crude oil with hydrogen and then feeding the mixture through a pre-hydrofining reaction zone, an intermediate reaction zone and a hydrofining reaction zone which are connected in series, where the sensor units are configured to detect pressure drop in each pre-hydrofining reactor in the pre-hydrofining reaction zone, and control unit is configured to receive pressure drop signals from sensor units; at the initial reaction stage, the pre-hydrofining reaction zone includes 3–6 pre-hydrofining reactors connected in parallel, transient reaction zone includes or does not include pre-hydrofining reactors; further, when the pressure drop in one of the pre-hydrofining reactors reaches a predetermined value, the pre-hydrofining reactor is switched from the pre-hydrofining reaction zone to the transition reaction zone and is referred to as the disconnected pre-hydrofining reactor I, wherein the pre-hydrofining reaction zone, the disconnected pre-hydrofining reactor I and the hydrofining reaction zone are connected in series; when the pressure drop in the next pre-hydrofining reactor reaches a predetermined value, the pre-hydrofining reactor is switched from the pre-hydrofining reaction zone to the transition reaction zone and is referred to as the disconnected pre-hydrofining reactor II, wherein the pre-hydrofining reaction zone, the disconnected pre-hydrofining reactor II, the disconnected pre-hydrofining reactor I and the hydrofining reaction zone are connected in series; other pre-hydrofining reactors are treated in the above method until all pre-hydrofining reactors are connected in series; wherein preset differential pressure in pre-hydrofining reactors makes 50–80 % of designed upper pressure drop for pre-hydrofining ...

Control system method and apparatus for two phase hydroprocessing

A continuous liquid phase hydroprocessing process, apparatus and process control systems, where the need to circulate hydrogen gas through the catalyst is eliminated. By mixing and/or flashing the hydrogen and the oil to be treated in the presence of a solvent or diluent in which the hydrogen solubility is high relative to the oil feed, all of the hydrogen required in the hydroprocessing reactions may be available in solution. The oil/diluent/hydrogen solution can then be fed to a plug flow reactor packed with catalyst where the oil and hydrogen react. No additional hydrogen is required; therefore, the large trickle bed reactors can be replaced by much smaller tubular reactors. The amount of hydrogen added to the reactor can be used to control the liquid level in the reactor or the pressure in the reactor.

Power generation from waste heat in integrated crude oil diesel hydrotreating and aromatics facilities

A power generation system includes two heating fluid circuits coupled to multiple heat sources from multiple sub-units of a petrochemical refining system. The sub-units include an integrated diesel hydro-treating plant and aromatics plant. A first subset and a second subset of the heat sources includes diesel hydro-treating plant heat exchangers coupled to streams in the diesel hydro-treating plant and aromatics plant heat exchangers coupled to streams in the aromatics plant, respectively. A power generation system includes an organic Rankine cycle (ORC) including a working fluid that is thermally coupled to the two heating fluid circuits to heat the working fluid, and an expander to generate electrical power from the heated working fluid. The system includes a control system to activate a set of control valves to selectively thermally couple each heating fluid circuit to at least a portion of the heat sources.

A molecular-based equation-oriented reactor simulation system and its model reduction

Controlling production of transportation fuels from renewable feedstocks

A process for controlling the concurrent production of both diesel range hydrocarbons and aviation range hydrocarbons from renewable feedstocks such as plant oils and animal oils. The process involves determining the required specification of the desired products and the desired relative yields of the product that still meet the required specifications. The necessary isomerization and selective hydrocracking zone conditions are determined in order to create a mixture of paraffins which meet the required product specifications and yields. The necessary fractionation zone conditions are determined to separate the desired products. A renewable feedstock is treated by hydrogenating and deoxygenating to provide an effluent comprising paraffins, isomerizing and selectively hydrogenating at least a portion of the paraffins at the predetermined conditions, and separating by fractionation at the predetermined fractionation conditions to generate a diesel range hydrocarbon product and an aviation range hydrocarbon product.

Crystalline transition metal tungstate

A hydroprocessing catalyst has been developed. The catalyst is a crystalline transition metal tungstate material or metal sulfides derived therefrom, or both. The hydroprocessing using the crystalline transition metal tungstate material may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking.

Transition metal tungstate material

A hydroprocessing catalyst or catalyst precursor has been developed. The catalyst is a transition metal tungstate material or metal sulfides derived therefrom. The hydroprocessing using the crystalline ammonia transition metal tungstate material may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking.

STAGE HYDROTREATMENT PROCESS OF A HEAVY LOAD

L’invention concerne un procédé d’hydrotraitement d’une charge pétrolière lourde dans un système en lit fixe comprenant un nombre n de lits catalytiques d’hydrotraitement noté L1 à Ln disposés en série, en présence, dans lequel - la charge est divisée en un nombre n de flux partiels noté de F1 à Fn égale au nombre de lits, puis - le flux partiel F1 passe sur le lit L1, - le flux partiel F2 est mélangé avec l’effluent E1 issu du lit L1 puis est injecté sur le lit L2, - le flux partiel Fn est mélangé avec l’effluent En-1 issu du lit Ln-1 puis est injecté sur le lit Ln, n étant un entier compris entre 2 et 20.

Method for Producing Heating Oils Using Waste Oils

Disclosed is a method for manufacturing fuel oil using waste oil. Through a series of treatment processes, from waste lubricants containing polycyclic aromatic compounds and including water, heavy metals, etc., as impurities, high value-added hydrocarbon oil fractions, particularly oil fractions for fuel oil, can be produced, and blended fuel oil obtained by combining the oil fractions for fuel oil with other petroleum-based oil fractions for fuel oil can be produced.

Multistage hydrocracking of still residue

FIELD: chemistry.SUBSTANCE: invention relates to a method of improving the quality of still residue in a system, comprising the presence of a first fluidised bed reactor; first separator; of the stripping column; distillation system and solvent deasphalting system. Method includes operation of system in first mode to produce raw material for installation of residue fluid catalytic cracking (RFCC), wherein the first mode is carried out in the distribution of particles in size, which provides low pressure drop in the range of expansion of the catalyst layer from 5 to 25 %. Operation of system in second mode to maximize residue conversion in first fluidised bed reactor, wherein the second mode is carried out when particles are sized to provide a low pressure drop in the range of expansion of the catalyst layer from 40 to 60 %. Switching of the system between the first mode and the second mode, the transition involves removing the hydrotreating catalyst from the first fluidised bed reactor while simultaneously adding the hydrocracking catalyst to the first fluidised bed reactor and increasing the speed of the ebb pump; distillation of the first liquid phase in the distillation system with production of at least one atmospheric distillate and atmospheric residues.EFFECT: technical result is improvement of flexibility of residues hydrocracking processes, which provide high conversion of bottom residues, reduce total amount of equipment, reduce total size of hydrocracking reactor equipment and/or solvent deasphalting and require less frequent replacement of hydrocracking catalyst.9 cl, 1 ex, 2 tbl, 5 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 722 644 C1 (51) МПК C10G 65/12 (2006.01) C10G 67/04 (2006.01) C10G 47/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК C10G 65/12 (2019.08); C10G 67/04 (2019.08); C10G 47/00 (2019.08) (21)(22) Заявка: 2019119134, 21.12.2017 (24) Дата начала отсчета срока действия патента: ...

The real-time predicting method and its system of hydrogenolysis degree in a kind of hydrofinishing

本发明提供一种加氢精制过程中含硫和/或氮的化合物的氢解程度的实时预测方法及其系统，所述方法包括：基于所述过程的当前操作条件，利用极限学习机ELM模型实时预测所述过程中含硫和/或氮的化合物的氢解程度。本发明根据加氢裂化流程在线可检测的过程变量利用ELM实时预测加氢精制过程含硫和/或氮的化合物的氢解程度，可为加氢裂化流程精制反应器的运行优化提供重要的状态信息。

Thermowell compound apparatus of high shell for residue Hydrogen desulfurization

본 발명은 중질유 중의 황 성분을 탈황하기 위해 고압반응기의 내부에 충전되어 있는 촉매의 반응온도를 측정하기 위한 열전대의 예상치 못한 손상으로 내부의 고온, 고압 유독가스가 누출될 경우 신속하게 누출피해를 해소할 수 있는 탈황공정용 고압반응기의 열전대 차폐장치에 관한 것으로, 촉매의 화학반응에 의한 유동으로 열전대와 보호관의 용접부위가 손상될 경우 누출차폐수단을 이용하여 유독가스가 누출되는 누출경로를 신속하게 차폐하게 됨으로써, 탈황공정의 운휴에 따른 경제적 손실을 예방함은 물론, 인명 및 환경피해 등 간접피해의 발생을 방지할 수 있게 되는 등의 매우 유용한 발명인 것이다. The present invention solves the leakage damage quickly when the internal high temperature and high pressure toxic gas leaks due to the unexpected damage of the thermocouple for measuring the reaction temperature of the catalyst charged inside the high pressure reactor to desulfurize the sulfur component in the heavy oil. The present invention relates to a thermocouple shielding device of a high-pressure reactor for desulfurization process, and when a welded part of a thermocouple and a protective tube is damaged due to the flow of a chemical reaction of a catalyst, a leak path for leaking toxic gas is quickly used. By shielding, it is a very useful invention, such as to prevent economic losses due to the operation of the desulfurization process, as well as to prevent the occurrence of indirect damage such as human life and environmental damage. 탈황공정, 반응기, 촉매, 열전대, 차폐장치, 압축차단, 실링캡 Desulfurization Process, Reactor, Catalyst, Thermocouple, Shielding Device, Compression Block, Sealing Cap

Obtaining flavouring catalyst in presence of alkali metal at washing step

FIELD: chemistry.SUBSTANCE: invention relates to methods of producing catalysts on a support, comprising a transition metal and a bound zeolite base, a reforming catalyst and reforming methods involving contacting the hydrocarbon feedstock with the catalyst in reforming conditions in a reactor apparatus in order to obtain an aromatic product. Method of producing supported catalyst includes: (a) preparing a bound zeolite base containing bound zeolite of type L; (b) washing the bound zeolite base with an aqueous solution containing rubidium, caesium or a combination thereof to obtain a zeolite support enriched with an alkali metal; or washing the bound zeolite base with an aqueous solution containing potassium in order to obtain a potassium-enriched zeolite support, wherein concentration of potassium in aqueous solution ranges from about 0.1 M to about 0.45 M; and (c) impregnating a zeolite support rich in an alkali metal with Group 8–10 transition metal and halogen to obtain a catalyst on a support.EFFECT: obtaining an unexpected combination of high selectivity of the catalyst on the product (for example, benzene or toluene), but with a lower specific surface area of the catalyst and a smaller volume of micropores of the catalyst.75 cl, 3 tbl, 5 ex, 4 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) МПК B01J 37/06 B01J 29/62 B01J 27/13 B01J 23/04 C10G 35/06 (11) (13) 2 725 671 C1 (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 37/06 (2020.02); B01J 29/62 (2020.02); B01J 27/13 (2020.02); B01J 23/04 (2020.02); C10G 35/06 (2020.02) (21)(22) Заявка: 2019118883, 14.12.2017 14.12.2017 (73) Патентообладатель(и): ШЕВРОН ФИЛЛИПС КЕМИКАЛ КОМПАНИ ЭлПи (US) Дата регистрации: 03.07.2020 (56) Список документов, цитированных в отчете о поиске: US 6190539 B1, 20.02.2001. US 4987109 A, 22.01.1991. EP 201856 A1, 20.11.1986. EP 2170509 B1, 19.08.2015. US 4448891 A, 15.05.1984. RU 2549836 C1, ...

Method for selective hydrogenation of an olefin feedstock using one main reactor and a reduced-size safety reactor

Настоящее изобретение относится к способу селективного гидрирования углеводородного сырья, содержащего полиненасыщенные молекулы, содержащие, по меньшей мере, 3 атома углерода, в котором гидрирование проводят в условиях, при которых упомянутое сырье и газовую фазу, содержащую водород, пропускают через катализатор гидрирования, находящийся в единственном основном реакторе с фиксированным слоем, содержащим, по меньшей мере, два каталитических слоя, и в имеющем меньший размер предохранительном реакторе, содержащем, по меньшей мере, один каталитический слой, причем упомянутые реакторы установлены последовательно, для использования циклическим образом, с последовательным повторением этапов a), b), c), c '), d) и d'): этап a), в ходе которого сырье последовательно проходит все каталитические слои основного реактора; с момента начала дезактивации первого каталитического слоя основного реактора - этап b), в ходе которого сырье вводят в предохранительный реактор, затем, минуя первый, частично дезактивированный каталитический слой основного реактора, - в ближайший, не дезактивированный каталитический слой упомянутого основного реактора, расположенный непосредственно ниже по потоку относительно циркуляции сырья; этап c), в ходе которого сырье проходит однократно и последовательно все каталитические слои основного реактора; этап c'), одновременно с этапом c), в ходе которого дезактивированный катализатор каталитического слоя или слоев предохранительного реактора подвергают регенерации или замене свежим катализатором; этап d), в ходе которого сырье пропускают только через предохранительный реактор; этап d'), одновременно с этапом d), в ходе которого дезактивированный катализатор, по меньшей мере, двух каталитических слоев основного реактора подвергают регенерации или замене свежим катализатором. Предлагаемый способ позволяет устранить нежелательные полиненасыщенные соединения из углеводородного сырья. 14 з.п. ф-лы, 2 ил., 4 табл., 2 пр. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) ...

Method for optimizing catalyst loading for hydrocracking process

The invention relates to a method for optimizing layered catalytic processes. This is accomplished by testing various catalysts with a compound found in a feedstock to be tested, to determine the facility of the catalyst in hydrogenating, hydrosulfurizing, or hydrodenitrogenating the molecule, and hence the feedstock. In a preferred embodiment, the Double Bond Equivalence of the feedstock and molecule are determined, and catalysts are pre-selected based upon their known ability to work with materials of this DBE value. In preferred embodiments, the layered catalysts include a demetallization catalyst, used before hydrocracking. In additional preferred embodiments, the test feedstock contains 500 ppmw or less asphaltenes, preferably C5-asphaltenes.

Imms method for petroleum feedstock evaluation

An ion mobility mass spectrometry (IMMS) method is disclosed for evaluating petroleum feedstock compositions. The method is useful to determine, e.g., nitrogen speciation in chemical components of a petroleum composition and may be used to evaluate hydroprocessing catalyst performance.

METHOD OF MULTISTRIBUTED SELECTIVE HYDRAULIC CLEANING OF OIL FRACTIONS

Hydrofining method for much production of middle distillate obtained from low-temperature Fischer-Tropsch full-range oil

本发明的低温费托全馏分油多产中间馏分油的加氢精制方法步骤如下：1)将低温费托全馏分油多产中间馏分油分成轻馏分油、重馏分油及中间馏分油三种；2)所述的轻馏分油、重馏分油及中间馏分油经计量泵计量后分别进入加氢反应器，加氢反应器内全部装填精制催化剂，加氢反应器由上部至中部依次设第一进料口、第二进料口、第三进料口，轻组分从第一进料口进料，重组分从第二进料口进料，中间组分从第三进料口进料；同时，循环氢由氢气进入口分别与轻馏分油、重馏分油及中间馏分油混合由第一进料口、第二进料口、第三进料口进入加氢反应器内反应；3)步骤2)反应的产物依次进入气液分离器和分馏塔分离。本发明可以保持精制反应床层温度控制平稳，又降低了重组分进料的温度，降低了能耗，同时缩短了中间组分的停留时间，减轻了二次裂化。

Controlling temperature within a catalyst bed in a reactor vessel

A quenching medium is delivered directly to selected regions or locations within a catalyst bed in a hydroprocessing reactor vessel in order to control the reactivity of a hydroprocess occurring in the selected regions or locations separately from other regions or locations. Temperature sensors for providing temperature indications and conduits for delivering the quench medium are distributed throughout the catalyst bed. One or more conduits can be selected for delivery of the quenching medium to selected regions or locations so that separate control of the level of reactivity in each of various regions or locations throughout the bed can be achieved.

Disc having impact absorbing action and creating uniform flow and reactor

FIELD: chemistry; technological processes.SUBSTANCE: present invention relates to chemical processing equipment and describes a disc for uniform distribution of material flow and a reactor. Said disc contains plate (100) of column, pipe (200) for the discharge of material passing through plate (100) of column, and device (300) which attenuates impact. Said attenuating impact device is configured to absorb the kinetic energy of an obliquely dropping material flow. Said device (300) has a guide surface made with the possibility of directing an obliquely dropping stream of material for its passage along the guide surface and falling towards plate (100) of column. On the part of nozzle (200) above plate (100) of column overflow holes (201) are located. Said disc contains plurality of nozzles (200) and plurality of devices (300), made to ensure the function of absorbing the impact of the dropping material for specified set of nozzles (200). Using the device, the kinetic energy of the flow of material can be absorbed. And a flow of the dropping material can be formed.EFFECT: invention provides a uniform distribution of gas-liquid material in a hydrogenation reactor.31 cl, 38 dwg, 9 tbl РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 672 742 C1 (51) МПК B01J 8/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 8/00 (2006.01); B01J 8/008 (2006.01); B01J 8/0453 (2006.01); B01J 19/2415 (2006.01); B01J 19/006 (2006.01) (21)(22) Заявка: 2017140962, 24.11.2017 24.11.2017 Дата регистрации: 19.11.2018 C 1 2 6 7 2 7 4 2 R U CN CN CN CN CN CN CN CN CN 201611051739.0; 201611051740.3; 201611052855.4; 201611052869.6; 201611083261.X; 201611083262.4; 201611083960.4; 201611084901.9; 201611084902.3 (56) Список документов, цитированных в отчете о поиске: FR 2982172 B1, 01.11.2013. SU 1098559 A1, 23.06.1984. RU 2386473 C2, 20.04.2010. RU 2415903 C2, 10.04.2011. US 8409521 B2, 02.04.2013. US 3958952 A1, 25.05.1976. US 6221133 B1, 24.04 ...

Initial temperature excursion mitigation and control

本发明公开了用于检测化工厂或石化厂或精炼厂中的温度剧增的系统和方法。本公开的各方面提供了用于反应器的增强的控制系统，诸如在加氢处理时使用。所述增强的控制系统可提供对即将发生的非期望事件的早期警示，直接或间接地操纵某些过程变量以减少非期望结果，并且/或者直接或间接地操纵某些过程变量以便将反应器单元置于“安全停放”状态。这可避免高温跳闸、降压、相关联的操作风险，允许更快地从温度剧增状态恢复正常，并且/或者避免所述反应器、化学过程、工厂或精炼厂的非计划紧急关闭。

How to Optimize Catalyst Loading for Hydrocracking Processes

본 발명은 층상화된 촉매 공정을 최적화하는 방법에 관한 것이다. 이것은 시험되는 공급원료에서 발견되는 화합물로 다양한 촉매를 시험하여, 분자, 및 따라서 공급원료를 수소화, 수소화황화, 또는 수소화탈질소화하는데 있어서 촉매의 설비를 결정함으로써 달성된다. 바람직한 구현예에서, 공급원료 및 분자의 이중 결합 당량 (DBE)은 결정되고, 촉매가 이 DBE 값의 물질과 작업하는 그의 알려진 능력에 기초하여 미리-선택된다. 바람직한 구현예에서, 층상화된 촉매는 수소화분해 전에 사용되는 탈금속화 촉매를 포함한다. 추가의 바람직한 구현예에서, 시험 공급원료는 500 ppmw 이하의 아스팔텐, 바람직하게는 C 5 -아스팔텐을 함유한다.

Catalyst reaction layer with separate raw material feeding in the hydraulic cleaning plant

FIELD: oil and gas industry. SUBSTANCE: invention relates to the plant with hydrotreating reactor and to the naphtha mixture stream hydrotreating method. Plant comprises the reaction chamber, in which the first layer and the second layer are arranged, and which comprises first input arranged so, that to provide the hydrocarbons stream supply to the first layer, and the second input arranged so, that to bypass the first layer and direct the hydrocarbons flow to the second layer, regulator for the temperature differences measuring across the first layer height, installed near the second inlet and connected to the regulator control valve, configured to control the supplied through the second inlet hydrocarbon stream flow rate, based on the measured by the regulator temperature difference, raw material heater, from which a hydrocarbon stream exits through the output line, which contains branching, at that, the output line first branch is connected to the first input and in fluid communication with the first layer, and the output line second branch is connected to the second input and in fluid communication with the second layer, and throttle device installed downstream of the output line branching point between the raw material heater and the first input and serving to monitor the differential pressure at the first input. EFFECT: invention enables temperature control over the first layer height without disturbing the other layers functioning. 10 cl, 1 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 659 263 C2 (51) МПК B01J 8/24 (2006.01) B01J 19/24 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 8/24 (2018.02); B01J 19/24 (2018.02) (21)(22) Заявка: 2016112530, 03.09.2014 (24) Дата начала отсчета срока действия патента: Дата регистрации: 29.06.2018 10.09.2013 US 14/022,543 (43) Дата публикации заявки: 05.10.2017 Бюл. № 28 (56) Список документов, цитированных в отчете о поиске: US 2012/0273394 A1, 01.11.2012. ...

Fisher-tropsh low-temperature distillate hydraulic cleaning method having the medium distillates high output

FIELD: technological processes.SUBSTANCE: invention relates to the Fischer-Tropsch synthetic distillates full range middle distillates hydrotreatment method, wherein the method comprises the steps of: 1) separating the Fischer-Tropsch synthetic distillates full-range middle distillates, to provide the light distillates, heavy distillate and intermediate distillate output, wherein the light distillates boiling ranges are below the 180 °C; the intermediate distillates boiling points are between 180 °C and 360 °C; and the heavy distillates boiling ranges are above the 360 °C; 2) using a metering pump measuring the light distillates, heavy distillates and intermediate distillates; providing the hydrogenation reactor (1) filled with a hydrotreating catalyst and containing a first feed opening (1a), second feed opening (1b) and the third feed opening (1c) from top to bottom, wherein each feed opening is communicating with the hydrogen input; mixing the hydrogen and the light distillates, the heavy distillates and the intermediate distillates, respectively, and introducing the resulting mixtures into the hydrogenation reactor through the first feed opening (1a), the second feed opening (1b) and the third feed opening (1c), respectively; wherein the reaction pressure in the hydrogenation reactor (1) is between 4 MPa and 8 MPa, the hydrogen to distillates ratio is between 100:1 and 2,000:1, the liquid hourly space velocity is between 0.1 hand 5.0 hand the reaction temperature is between 300 °C and 420 °C; and 3) introducing the products from 2) into the gas-liquid separator to ensure the hydrogen and liquid products output, returning the hydrogen to the hydrogenation reactor (1) through the first feed opening (1a), the second feed opening (1b) and the third feed opening (1c), respectively, to mix with the liquid distillates, the heavy distillates and the intermediate distillates, and introducing liquid products into the distillation column for further separation, wherein the ...

The manufacture method of monocyclic aromatic hydrocarbon

本发明的单环芳香族烃的制造方法具有：裂化重整反应工序，在该工序中，使原料油与含有结晶性铝硅酸盐的单环芳香族烃制造用催化剂接触、反应，从而得到包含碳原子数为6～8的单环芳香族烃的产物；加氢反应工序，在该工序中，对裂化重整反应工序中生成的产物进行加氢；单环芳香族烃回收工序，在该工序中，对从加氢反应工序中得到的加氢反应物分离出的碳原子数为6～8的单环芳香族烃进行回收；和循环利用工序，在该工序中，将从加氢反应工序中得到的加氢反应物分离出的碳原子数为9以上的重质馏分返回至所述裂化重整反应工序。