Method and arrangement for feeding heat-sensitive materials to fixed-bed reactors

The invention relates to an arrangement for feeding heat-sensitive feedstock to a fixed-bed reactor system comprising means for product recycle and a fixed-bed reactor system comprising a fixed-bed reactor comprising at least one reaction zone having at least one catalyst bed and said reaction zone comprising a cold feed distributor arranged on top of each catalyst bed and a conventional distributor arranged above each cold feed distributor. Also a method is provided for feeding heat-sensitive feedstock to a fixed-bed reactor system wherein said fixed-bed reactor system comprises means for product recycle and a fixed-bed reactor comprising at least one reaction zone having at least one catalyst bed and said reaction zone comprising a cold feed distributor arranged on top of each catalyst bed and a conventional distributor arranged above each cold feed distributor.

Method and systems for making distillate fuels from biomass

The present invention provides methods, reactor systems and catalysts for converting biomass and biomass-derived feedstocks to C 8+ hydrocarbons using heterogenous catalysts. The product stream may be separated and further processed for use in chemical applications, or as a neat fuel or a blending component in jet fuel and diesel fuel, or as heavy oils for lubricant and/or fuel oil applications.

In situ radio frequency catalytic upgrading

The present invention relates to a method and system for enhancing in situ upgrading of hydrocarbon by implementing an array of radio frequency antennas that can uniformly heat the hydrocarbons within a producer well pipe, so that the optimal temperatures for different hydroprocessing reactions can be achieved.

Offshore heavy oil production

A system is provided for the production of heavy crude oil from an undersea reservoir, and for the treatment of the crude oil to facilitate its transport. A floating body ( 12 ) which produces the heavy crude oil, carries a hydrocarbon cracking station ( 32 ) that cracks the heavy crude into light liquid and gaseous hydrocarbons, and that uses heat resulting from the cracking to produce pressured steam. The pressured steam is used to drive a steam-powered engine ( 72 ) (with pistons or a turbine) that drives an electrical generator ( 74 ) whose electricity powers the system.

Energy efficient, low emissions shale oil recovery process

A process for the energy efficient, environmentally friendly recovery of liquid and gaseous products from solid or semi-solid hydrocarbon resources, in particular, oil shale or tar sands. The process involves non-oxidative pyrolysis to recover fluid energy values, oxidative combustion to recover energy values as recoverable heat, and environmental sequestration of gases produced.

Method and apparatus for producing liquid hydrocarbon fuels from coal

A method of converting coal into a liquid hydrocarbon fuel utilizes a high pressure, high temperature reactor which operates upon a blend of micronized coal, a catalyst, and steam. Microwave power is directed into the reactor. The catalyst, preferably magnetite, will act as a heating media for the microwave power and the temperature of the reactor will rise to a level to efficiently convert the coal and steam into hydrogen and carbon monoxide.

Processing Hydrocarbons

Systems and methods that include providing, e.g., obtaining or preparing, a material that includes a hydrocarbon carried by an inorganic substrate, and exposing the material to a plurality of energetic particles, such as accelerated charged particles, such as electrons or ions.

Enclosure of an FCC Unit Comprising an Inner Support Device Rigidly Connected to Cyclones

The invention relates to an enclosure () of a fluid catalytic cracking unit in which an inner space is defined by a side wall () having a longitudinal axis extending substantially in the direction of gravity, said enclosure being provided with a plurality of mechanical separation cyclones () located inside the inner space. The enclosure () comprises a supporting device () attached only to the cyclones () by: an annular peripheral support element () extending along the side wall () in a plane perpendicular to the longitudinal axis (X), separated from the side wall by a predetermined clearance; and a plurality of beams () extending in the same plane as the peripheral support element (), the beams being rigidly connected to the peripheral support element and to at least one mechanical separation cyclone by one end or by an attachment part distant from the ends thereof. 116.-. (canceled)17. A chamber of a fluid catalytic cracking unit comprising a lateral wall which delimits an internal volume having a longitudinal axis extending substantially in the direction of gravity , said chamber being provided with a plurality of mechanical separation cyclones situated inside said internal volume , characterized in that said chamber comprises , inside said internal volume , a support device secured only to the mechanical separation cyclones and comprising:a peripheral support element extending along the lateral wall in a plane perpendicular to the longitudinal axis (X), distant from the lateral wall by a predetermined clearance in the plane of the support element,a plurality of beams extending in the same plane as the peripheral support element, the beams being secured to the peripheral support element and to at least one mechanical separation cyclone by an end or by a fixing part distant from its ends.18. The chamber as claimed in claim 17 , characterized in that the support device comprises other beams extending in the same plane as the peripheral support element and chosen ...

THERMAL AND CHEMICAL UTILIZATION OF CARBONACEOUS MATERIALS, IN PARTICULAR FOR EMISSION-FREE GENERATION OF ENERGY

A process for the generation of energy and/or hydrocarbons and other products utilizing carbonaceous materials. In a first process stage (P) the carbonaceous materials are supplied and are pyrolysed, wherein pyrolysis coke (M) and pyrolysis gas (M) are formed. In a second process stage (P), the pyrolysis coke (M) from the first process stage (P) is gasified, wherein synthesis gas (M) is formed, and slag and other residues (M M M M) are removed. In a third process stage (P), the synthesis gas (M) from the second process stage (P) is converted into hydrocarbons and/or other solid, liquid, and/or gaseous products (M), which are discharged. The three process stages (P P P) form a closed cycle. Surplus gas (M) from the third process stage (P) is passed as recycle gas into the first process stage (P), and/or the second process stage (P), and pyrolysis gas (M) from the first process stage (P) is passed into the second process stage (P), and/or the third process stage (P). 1. A process for the emission-free generation of energy and/or hydrocarbons and other products by utilization of carbonaceous materials , in which in a first process stage the carbonaceous materials are supplied and pyrolysed , wherein pyrolysis coke and pyrolysis gas are formed; in a second process stage , the pyrolysis coke from the first process stage is gasified , wherein synthesis gas is formed , and slag and other residues are removed; and in a third process stage , the synthesis gas from the second process stage is converted into hydrocarbons and/or other solid , liquid and/or gaseous products , which are discharged; wherein the three process stages form a closed cycle , surplus gas from the third process stage is passed as recycle gas into the first process stage and/or the second process stage , and the pyrolysis gas of the first process stage is passed into the second process stage and/or the third process stage.2. The process according to claim 1 , wherein hydrogen is supplied in at least one ...

Extruder for Processing Hydrocarbon-Containing Materials

An extruder for processing hydrocarbon-containing material. The extruder includes a screw that is rotatably positioned in a auger barrel and a heating system positioned about at least a portion of the auger barrel that is designed to heat the hydrocarbon-containing material as the hydrocarbon-containing material moves through the auger barrel.

Catalyst activation method for fischer-tropsch synthesis

The present invention relates to: a catalyst activation method for Fischer-Tropsch synthesis; a catalyst regeneration method for Fischer-Tropsch synthesis; and a method for producing a liquid or solid hydrocarbon by using the Fischer-Tropsch synthesis reaction. The temperatures required for a metal carbide producing and activating reaction is markedly lower than existing catalyst activation temperatures, and the catalyst can be activated under conditions that are the same as Fischer-Tropsch synthesis reaction conditions, and thus there is no need for separate reduction equipment in the reactor, and a Fischer-Tropsch synthesis catalyst which has been used for a long time can be regenerated within the reactor without the catalyst being isolated or extracted from the reactor.

IMPROVEMENTS IN IN SITU UPGRADING VIA HOT FLUID INJECTION

The invention relates to systems, apparatus and methods for integrated recovery and in-situ (in reservoir) upgrading of heavy oil and oil sand bitumens. The systems, apparatus and methods enable enhanced recovery of heavy oil in a production well by introducing a hot hydrocarbon fluid from a mobile reservoir into the production well under conditions to promote hydrocarbon upgrading. The methods may further include introducing hydrogen and a catalyst together with the injection of the hot fluid into the production well to further promote hydrocarbon upgrading reactions. In addition, the invention relates to enhanced oil production methodologies within conventional oil reservoirs. 1. An apparatus for processing hydrocarbons , the apparatus comprising:an injection well, the injection well being configured to inject fluid into a subterranean reservoir;a recovery well, the recovery well being configured to recover fluid from the subterranean reservoir; andan injection well connector configured to receive heavy hydrocarbon fluid from a mobile surface reservoir and deliver the received heavy hydrocarbon fluid to the injection well to be injected into the subterranean reservoir for processing such that the fluid recovered from the subterranean reservoir via the recovery well has a different composition to the heavy hydrocarbon fluid injected via the injection well.2. The apparatus according to claim 1 , wherein the mobile surface reservoir forms part of an oil tanker ship.3. The apparatus according to claim 1 , wherein the apparatus forms part of an offshore oil rig.4. The apparatus according to claim 1 , wherein the heavy hydrocarbons comprise one or more of: bunker fuel; and fuel number 6.5. The apparatus according to claim 1 , wherein the apparatus comprises a pre-mixer configured to mix the heavy fraction with additional injection fluids and to inject the mixed fluids into the injection well.6. The apparatus according to claim 1 , wherein the injection well is ...

Relocatable Systems and Processes for Recovery of Bitumen From Oil Sands

Relocatable systems and processes for processing oil sands are described. Relocatable components are employed to permit oil sand processing to be conducted near a mine face, and relocated as the mine face recedes. Flow of the slurry in combination with appropriate water injection through the relocatable pipeline causes agglomeration of fines within the slurry. Bitumen/solvent mixtures can be filtered from the agglomerates within downstream solvent extraction system components. A high quality bitumen product is formed, having water and solids content that exceeds downstream processing and pipeline requirements. Dry tailings may be back-filled in-pit.

PROCESS FOR POLYMER MIXTURE HYDROCONVERSION

There is a process for the hydroconversion of mixtures of polymers or plastics which comprises the pre-treatment of the mixtures through methods selected from mechanical methods, chemical methods, thermal methods, or combinations thereof forming a pre-treated charge. The pre-treated charge is mixed with a hydrocarbon vacuum residue, optionally pre-heated, to form a reactant mixture. The reactant mixture is fed to a hydroconversion section in slurry phase, together with a catalyst precursor containing Molybdenum, and a stream containing hydrogen, forming a reaction effluent. The effluent is separated into at least one high-pressure and high-temperature separator in a vapour phase and a slurry phase. The separate vapour phase is sent to a gas treatment section with the function of separating a liquid fraction from the gas containing hydrogen and hydrocarbon gases having from 1 to 4 carbon atoms; said liquid fraction comprising naphtha, atmospheric gas oil (AGO), vacuum gas oil (VGO). The slurry phase is then sent to a separation section that has the function of separating the fractions of the Vacuum Gas Oil (VGO), Heavy Vacuum Gas Oil (HVGO), Light Vacuum Gas Oil (LVGO), Atmospheric Gas Oil (AGO), from a stream of heavy organic products which contains asphaltenes, unconverted charge, catalyst and solid formed during the hydroconversion reaction. This stream of heavy organic products is partly recirculated to the hydroconversion section and partly forms a purge stream. 1. A process for polymer mixture hydroconversion which comprises the following steps:pre-treating a polymer mixture through methods selected from mechanical methods, chemical methods, thermal methods, or combinations thereof, forming a pre-treated charge;mixing said pre-treated charge with a vacuum hydrocarbon residue, optionally pre-heated, to form a reactant mixture;feeding to a hydroconversion section the reactant mixture in slurry phase, a precursor of the catalyst containing Molybdenum, and a stream ...

STORAGE OF FISCHER-TROPSCH EFFLUENTS

Process for the production of middle distillates from a paraffinic feedstock produced by Fischer-Tropsch synthesis comprising at least one light fraction, known as condensate, and a heavy fraction, known as waxes, in which: 1. Process for the production of middle distillates from a paraffinic feedstock produced by Fischer-Tropsch synthesis comprising at least the following stages:{'b': 2', '3, 'a) the said paraffinic feedstock resulting from a Fischer-Tropsch unit (A) is recovered, the said paraffinic feedstock comprising at least a light fraction (), known as condensate, and a heavy fraction (), known as waxes;'}{'b': 4', '5, 'b) a least a part of the said light fraction and at least a part of the said heavy fraction which are obtained on conclusion of stage a) are sent, as a mixture (), to a hydrotreating unit (D) in the presence of hydrogen and a hydrotreating catalyst in order to obtain a first hydrotreated effluent ();'}{'b': 5', '6, 'c) at least a part of the first hydrotreated effluent () obtained on conclusion of stage b) is sent to a hydrocracking/hydroisomerization unit (E) in the presence of hydrogen and of a hydrocracking/hydroisomerization catalyst in order to obtain a second effluent ();'}{'b': 6', '7', '8', '9', '10, 'd) the second effluent () resulting from the hydrocracking/hydroisomerization unit is separated in a fractionation unit (F) in order to obtain at least a naphtha cut () having a maximum boiling point of less than 180° C., a middle distillates fraction (,) and an unconverted heavy fraction ();'}which process being characterized in that, when the hydrotreating unit (D) and/or the hydrocracking/hydroisomerization unit (E) is at shutdown, then:{'b': '2', 'the said light fraction () obtained on conclusion of stage a) is stored in a vessel (B) maintained under an inert atmosphere and in which the temperature inside the vessel is maintained at a value of less than 20° C.; and/or'}{'b': '3', 'the said heavy fraction () obtained on conclusion of ...

Thermal and chemical utilization of carbonaceous materials, in particular for emission-free generation of energy

A process for the generation of energy and/or hydrocarbons and other products utilizing carbonaceous materials. In a first process stage (P 1 ) the carbonaceous materials are supplied and are pyrolysed, wherein pyrolysis coke (M 21 ) and pyrolysis gas (M 22 ) are formed. In a second process stage (P 2 ), the pyrolysis coke (M 21 ) from the first process stage (P 1 ) is gasified, wherein synthesis gas (M 24 ) is formed, and slag and other residues (M 91 , M 92 , M 93 , M 94 ) are removed. In a third process stage (P 3 ), the synthesis gas (M 24 ) from the second process stage (P 2 ) is converted into hydrocarbons and/or other solid, liquid, and/or gaseous products (M 60 ), which are discharged. The three process stages (P 1 , P 2 , P 3 ) form a closed cycle. Surplus gas (M 25 ) from the third process stage (P 3 ) is passed as recycle gas into the first process stage (P 1 ), and/or the second process stage (P 2 ), and pyrolysis gas (M 22 ) from the first process stage (P 1 ) is passed into the second process stage (P 2 ), and/or the third process stage (P 3 ).

A METHOD FOR DESALTING PRODUCED HYDROCARBONS

A method for desalting produced hydrocarbons includes injecting reduced-salinity water into produced hydrocarbons in a production well or riser, to dilute high-salinity produced water contained in the produced hydrocarbons. 1. A method for desalting produced hydrocarbons , the method comprising:injecting reduced-salinity water into produced hydrocarbons in a production well or riser, to dilute high-salinity produced water contained in the produced hydrocarbons.2. The method of claim 1 , wherein the reduced-salinity water has a salinity lower than seawater in a body of water above a field in which the production well is located claim 1 , and/or has a salinity lower than the high-salinity produced water.3. The method of claim 1 , wherein the reduced-salinity water has a salinity of less than 60 000 mg/L claim 1 , preferably less than 55 000 mg/L claim 1 , more preferably less than 40 000 mg/L claim 1 , and still more preferably less than 31 000 mg/L.4. The method of claim 1 , wherein the reduced-salinity water is injected into the produced hydrocarbons through one or more openings in production tubing located in the production well claim 1 , or one or more openings in the riser.5. The method of claim 4 , wherein the one or more openings in the production tubing or production riser are provided with valves to control the inflow of reduced-salinity water.6. The method of claim 1 , wherein the produced hydrocarbons are contained in production tubing located in the production well claim 1 , wherein the reduced-salinity water is injected deep in the production well such that injection takes place close to a lower completion section.7. The method of claim 1 , wherein the reduced-salinity water is injected in an amount sufficient to create an oil-in-water emulsion in which the produced hydrocarbons are suspended as a dispersed phase within a continuous phase provided by the reduced-salinity water.8. The method of claim 1 , wherein the reduced-salinity water is injected in an ...

Accelerated cooling process for reactors

A process for shutting down a hydroprocessing reactor and for removing catalyst from the reactor, wherein the reactor includes a quench gas distribution system. The process comprises shutting off hydrocarbon feed to the reactor, stripping hydrocarbons from the catalyst, and cooling the reactor to a first threshold reactor temperature in the range of from 375-425° F. (190-218° C.). At least a portion of circulating gaseous medium flowing to the reactor is then routed through a temporary heat exchanger and cooling the gas to not less than 40° F. (4° C.). Once cooled, mixing the cooled gas with the circulating gaseous medium flowing to the reactor. Continuing steps routing and cooling until a second threshold temperature is reached wherein the reactor temperature is in a range between 120° F. and 250° F. (49° C.-121° C.). The reactor can then be purged with N 2 gas, followed by introducing water into the reactor via the quench gas distribution system. The catalyst can then be safely removed from the reactor.

Method to extract bitumen from oil sands

The present invention relates to an improved bitumen recovery process from oil sands. The oil sands may be surface mined and transported to a treatment area or may be treated directly by means of an in situ process of oil sand deposits that are located too deep for strip mining. Specifically, the present invention involves the step of treating oil sands with a propylene oxide capped glycol ether described by the structure: RO—(C 2 H 4 O) n —CH 2 CH(CH 3 )OH wherein R is a linear, branched, or cyclic alkyl, phenyl, alkyl phenyl group and n is 1 to 10.

METHOD AND APPARATUS FOR ENCODING AND DECODING HDR IMAGES

To encode High Dynamic Range (HDR) images, the HDR images can be converted to Low Dynamic Range (LDR) images through tone mapping operation, and the LDR images can be encoded with an LDR encoder. The present principles formulates a rate distortion minimization problem when designing the tone mapping curve. In particular, the tone mapping curve is formulated as a function of the probability distribution function of the HDR images to be encoded and a Lagrangian multiplier that depends on encoding parameters. At the decoder, based on the parameters indicative of the tone mapping function, an inverse tone mapping function can be derived to reconstruct HDR images from decoded LDR images. 1. A method comprising:determining a tone mapping function responsive to images and at least one encoding parameter;determining a lower dynamic range version of said images from said images responsive to the tone mapping function;encoding the lower dynamic range version of said images and information including a parameter used to encode the determined lower dynamic range version of said images, said parameter being intended to be used for generating an inverse ton-mapping function; andtransmitting the encoded lower dynamic range version of said images and information in one or more signals.2. The method of claim 1 , wherein the parameter used to encode the lower dynamic range version of said images is a quantization parameter.3. The method of claim 2 , wherein the tone curve estimator determines a Lagrangian multiplier responsive to the quantization parameter.4. The method of claim 1 , wherein determining a tone mapping function comprises determining at least one of the dynamic range of said images and a probability distribution function of said images.5. The method of claim 1 , wherein determining the tone mapping function is responsive to a rate distortion function.6. The method of further comprising providing said one or more signals signal for storage.7. The method of further ...

High Pressure Ethane Cracking with Small Diameter Furnace Tubes

Systems and methods are provided for performing ethane steam cracking at elevated coil inlet pressures and/or elevated coil outlet pressures in small diameter furnace coils. Instead of performing steam cracking of ethane at a coil outlet pressure of ˜22 psig or less (˜150 kPa-g or less), the steam cracking of ethane can be performed in small diameter furnace coils at a coil outlet pressure of 30 psig to 75 psig (˜200 kPa-g to ˜520 kPa-g), or 40 psig to 75 psig (˜270 kPa-g to ˜520 kPa-g). In order to achieve such higher coil outlet pressures, a correspondingly higher coil inlet pressure can also be used, such as a pressure of 45 psig (˜310 kPa-g) or more, or 50 psig (˜340 kPa-g) or more. 1. A method for performing steam cracking , comprising:pre-heating a mixture of steam and a feed comprising 50 vol % or more of ethane to a first temperature;passing the mixture into a plurality of radiant coils at a coil inlet pressure, wherein each of the furnace coils has an inner diameter of 6.0 cm or less; andexposing the mixture in the plurality of radiant coils to steam cracking conditions which include a cracking temperature of 800° C. or more and a coil outlet pressure of 200 kPa-g to 520 kPa-g or more for a residence time to produce a steam cracked effluent.2. The method of claim 1 , wherein the coil outlet pressure is in a range of from 270 kPa-g to 520 kPa-g.3. The method of claim 1 , wherein the residence time is in a range of from 0.1 second to 1.0 second.4. The method of claim 1 , wherein the coil inlet pressure is 310 kPa-g or more.5. The method of claim 1 , wherein the residence time is in a range of from 0.1 to 0.3 seconds.6. The method of claim 1 , wherein the first temperature is 675° C. or more.7. The method of claim 1 , wherein the first temperature is in a range of from 760° C. to 775° C.8. The method of claim 1 , wherein each of the furnace coils has an inner diameter in a range of from 2.5 cm to 5.0 cm.9. The method of claim 1 , wherein each of the furnace ...

Start-up method of bubble column slurry bed reactor

A start-up method of a bubble column slurry bed reactor for producing hydrocarbons includes: a first step that fills into a reactor a slurry in which a Fischer-Tropsch synthesis reaction catalyst particles are suspended in a slurry preparation oil with a 5% distillation point of 120 to 270° C., a 95% distillation point of 330 to 650° C., and a sulfur component and an aromatic component of 1 mass ppm or less, and a second step that, in a state where synthesis gas that is primarily hydrogen and carbon monoxide is introduced into the slurry filled into the reactor, raises the temperature of the reactor and starts the Fischer-Tropsch synthesis reaction. As the slurry preparation oil, one containing predetermined components in preset amounts is used. In the first step, the slurry is filled into the reactor in an amount in which airborne droplets do not flow out.

METHOD FOR STARTING UP A METHOD FOR PRODUCING KEROSENE AND DIESEL FUEL FROM HYDROCARBON COMPOUNDS PRODUCED BY FISCHER-TROPSCH SYNTHESIS

Method for starting up a method for producing kerosene and diesel fuel from hydrocarbon compounds produced by Fischer-Tropsch synthesis. 1) Method for starting up a method for producing kerosene and diesel fuel from hydrocarbon compounds produced by Fischer-Tropsch synthesis , in which the following steps are carried out:a) A catalytic reaction of Fischer-Tropsch synthesis is carried out with a synthesis gas to produce a heavy hydrocarbon fraction and a light hydrocarbon fraction,b) A reduction (RE) of a hydrotreatment catalyst is carried out by ensuring contact with a gas comprising hydrogen, and then step c) is carried out,c) The heavy hydrocarbon fraction is brought into contact (DM) with the hydrotreatment catalyst,d) During step c), the temperature (TEMP) of the hydrotreatment catalyst is increased to a temperature of between 260° C. and 360° C., and then step e) is carried out,e) A mixture comprising the heavy hydrocarbon fraction and the light hydrocarbon fraction are brought into contact (TR) with the hydrotreatment catalyst.2) Method according to claim 1 , in whichin step b), a reduction of the hydrotreatment catalyst and a hydrocracking and hydroisomerization catalyst is carried out by ensuring contact with a gas comprising hydrogen, and then step c) is carried out,in step c), the heavy hydrocarbon fraction is brought into contact with the hydrotreatment catalyst and then with the hydrocracking and hydroisomerization catalyst,in step e), the mixture comprising the heavy hydrocarbon fraction and the light hydrocarbon fraction is brought into contact with the hydrotreatment catalyst and then with the hydrocracking and hydroisomerization catalyst.3) Method according to claim 1 , in which step b) is carried out at a temperature of between 300° C. and 500° C. claim 1 , and then the hydrotreatment catalyst is cooled to a temperature of between 120° C. and 170° C. claim 1 , and then step c) is carried out.4) Method according to claim 1 , in which at the beginning ...

Method of determining renewable carbon content while producing and blending biogenic-based fuels or blendstocks with fossil fuel in a refining or blending facility

A method of monitoring renewable carbon in fuel streams in a refinery or blend facility while co-processing a bio-feedstock with a fossil feedstock or blending a renewable product with a fossil product wherein the method provides for quantification of renewable C14 carbon content to adjust the total renewable content to a targeted renewable content in situ while lowering the limit of detection.

Oxidative coupling of methane at near ambient feed temperature

Methods of performing a startup of an oxidative coupling of methane reaction to produce C2+ hydrocarbons are described. The methods can include incrementally varying startup parameters of the oxidative methane reactor and using the feed gas as a coolant such that high C2+ hydrocarbon selectivity is achieved.

System and Method for Monitoring a Reforming Catalyst

A method of monitoring catalytic performance of a catalyst used in a reforming process, comprising a) collecting gaseous component data from the reforming process; b) calculating a gaseous component ratio from the gaseous component data; and c) utilizing the gaseous component ratio to estimate an amount of catalytic activity remaining in the catalyst used in the reforming process, a number of days on stream remaining for the catalyst used in the reforming process, or both. 1. A method of monitoring catalytic performance of a catalyst used in a reforming process , the method comprising:a. collecting gaseous component data from the reforming process;b. calculating a gaseous component ratio from the gaseous component data; andc. utilizing the gaseous component ratio to estimate an amount of catalytic activity remaining in the catalyst used in the reforming process, a number of days on stream remaining for the catalyst used in the reforming process, or both.2. The method of wherein the gaseous component data comprises moles of hydrogen and moles of methane and wherein the gaseous component ratio comprises a ratio of moles of hydrogen to moles of methane.3. The method of wherein collecting gaseous component data from the reforming process further comprises collecting a gas sample from a gaseous component stream of the reforming process and subjecting the gas sample to gas chromatography.4. The method of wherein step c further comprises utilizing a correlation of baseline data for the ratio of moles of hydrogen to moles of methane and catalyst activity claim 2 , a correlation of baseline data for the ratio of moles of hydrogen to moles of methane and days on stream claim 2 , or both.5. (canceled)6. (canceled)7. (canceled)8. (canceled)9. (canceled)10. (canceled)11. (canceled)12. (canceled)13. (canceled)14. (canceled)15. A method of monitoring the catalytic performance of a catalyst used in a reforming process claim 2 , the method comprising:a. collecting a gas sample from ...

METHODS FOR ENHANCING HEAVY OIL RECOVERY

Novel catalysts comprising nickel oxide nanoparticles supported on alumina nanoparticles, methods of their manufacture, heavy oil compositions contacted by these nanocatalysts and methods of their use are disclosed. The novel nanocatalysts are useful, inter alia, in the upgrading of heavy oil fractions or as aids in oil recovery from steam-assisted well reservoirs. 1. A method for upgrading heavy oil in a steam-assisted heavy oil well , comprising: wherein said contacting of the heavy oil includes contacting with a nanocatalyst for a time and under conditions sufficient to increase the API gravity or decrease the viscosity of the heavy oil recovered from the well, wherein said nanocatalyst is steam-injected into the well injector leg or into the producer leg and injector leg;', wherein the alumina nanoparticle to nickel oxide nanoparticle weight to weight ratio in the catalyst is in a range of from about 99 to about 400;', 'wherein the particle size of the alumina nanoparticle is in a range of from about 30 to about 100 nanometers;', 'wherein the catalyst does not further comprise silver nanoparticles supported on the alumina nanoparticles; and', {'sub': 'BET', 'sup': '2', 'wherein the alumina nanoparticles are present in an amount of at least 99% by weight of the catalyst or the catalyst Ssurface area is from about 17 to about 70 m/g.'}], 'nickel oxide nanoparticles supported on alumina nanoparticles;'}, 'said nanocatalyst comprising], 'contacting the heavy oil that is contained in a rock formation associated with a steam-assisted well for producing the heavy oil, said well comprising a producer leg and an injector leg;'}2. A method according to claim 1 , wherein the alumina nanoparticles are present in an amount of at least 99% by weight of the catalyst.3. A method according to claim 1 , wherein the catalyst Sum′ surface area is from about 17 to about 70 m/g.4. A method according to claim 1 , wherein the alumina nanoparticles are present in an amount of at least ...

INTEGRATED PROCESS FOR IN-SITU ORGANIC PEROXIDE PRODUCTION AND OXIDATIVE HETEROATOM CONVERSION

An oxidative treatment process, e.g., oxidative desulfurization or denitrification, is provided in which the oxidant is produced in-situ using an aromatic-rich portion of the original liquid hydrocarbon feedstock. The process reduces or replaces the need for the separate introduction of liquid oxidants such as hydrogen peroxide, organic peroxide and organic hydroperoxide in an oxidative treatment process. 1. A process for conversion of heteroatom-containing compounds in a hydrocarbon feedstock to their oxidation products comprising:separating the hydrocarbon feedstock into an aromatic-lean fraction and an aromatic-rich fraction;contacting the aromatic-rich fraction with an effective amount of gaseous oxidant under conditions effective for organic peroxide generation in an organic peroxide generation apparatus and to produce a mixture containing organic peroxide and heteroatom-containing hydrocarbons;hydrotreating all or a portion of the aromatic-lean fraction; andpassing the mixture containing produced organic peroxide and heteroatom-containing hydrocarbons to an oxidative reaction apparatus operating under conditions effective for oxidative conversion of heteroatom-containing hydrocarbons into oxidation products of the heteroatom-containing hydrocarbons.2. The process as in claim 1 , further comprisingseparating the hydrocarbon feedstock into a first and second portion; andsubjecting only the first portion to contacting with an effective amount of gaseous oxidant under conditions effective for reaction into organic peroxide compounds;wherein contacting under conditions effective for conversion of heteroatom-containing hydrocarbons further comprises contacting the second portion for conversion of heteroatom-containing hydrocarbons in the second portion into oxidation products of those heteroatom-containing hydrocarbons.3. The process as in claim 2 , wherein separating the hydrocarbon feedstock into a first and second portion is with a diverter.4. The process as in ...

Biomass treatment for hydrothermal hydrocatalytic conversion

A selective removal of chlorine and phosphorus that are detrimental to subsequent hydrothermal hydrocatalytic conversion from the biomass feed prior to carrying out catalytic hydrogenation/hydrogenolysis/hydrodeoxygenation of the biomass in a manner that does not reduce the effectiveness of the hydrothermal hydrocatalytic treatment while minimizing the amount of water used in the process is provided

PROCESSING HYDROCARBONS

Systems and methods that include providing, e.g., obtaining or preparing, a material that includes a hydrocarbon carried by an inorganic substrate, and exposing the material to a plurality of energetic particles, such as accelerated charged particles, such as electrons or ions. 1. A method comprising:exposing oil shale comprising hydrocarbons to a beam of particles to isomerize the hydrocarbons.2. The method of claim 1 , wherein the oil shale is exposed to the beam of particles in situ in a formation.3. The method of claim 1 , wherein the beam of particles comprises an electron beam.4. The method of wherein exposing the hydrocarbon-containing material to the beam of particles reduces the molecular weight of the hydrocarbon by at least about 25%.5. The method of claim 4 , wherein the hydrocarbon initially has a molecular weight of from about 300 to about 2000 claim 4 , and after exposure the hydrocarbon has a molecular weight of from about 190 to about 1750.6. The method of claim 1 , wherein the beam of particles is used to generate bremssthrahlung x-rays.7. The method of claim 6 , wherein the beam of particles is generated by an electron gun claim 6 , and the x-rays are generated by utilizing the electron gun in combination with a metal foil.8. The method of claim 7 , wherein the metal foil comprises a tantalum foil.9. The method of claim 3 , wherein the electron beam delivers a dose of at least 5 Mrad of radiation.10. The method of claim 9 , wherein the dose is at least 10 Mrad.11. The method of claim 9 , wherein the dose is 20 Mrad or more.12. The method of claim 1 , wherein the particle beam comprises ions.13. The method of claim 1 , further comprising combining the oil shale with a catalyst material.14. The method of claim 1 , further comprising oxidizing the oil shale. This application is a continuation of pending U.S. Ser. No. 14/795,422, filed Jul. 9, 2015, which is a continuation of U.S. Ser. No. 14/314,834, filed Jun. 25, 2014, now U.S. Pat. No. 9,091,165, ...

Method and apparatus for encoding and decoding hdr images

To encode High Dynamic Range (HDR) images, the HDR images can be converted to Low Dynamic Range (LDR) images through tone mapping operation, and the LDR images can be encoded with an LDR encoder. The present principles formulates a rate distortion minimization problem when designing the tone mapping curve. In particular, the tone mapping curve is formulated as a function of the probability distribution function of the HDR images to be encoded and a Lagrangian multiplier that depends on encoding parameters. At the decoder, based on the parameters indicative of the tone mapping function, an inverse tone mapping function can be derived to reconstruct HDR images from decoded LDR images.

Process and apparatus for fluidizing a catalyst bed

A process and apparatus is disclosed for gradually starting fluidization in a bed of particulate from the top down so as to avoid thrusting the entire mass of particulates upwardly in the bed at the same time which may damage internals in the bed. The particulate bed may comprise a catalyst cooler for an FCC unit containing internals such as cooling, fluidization and support equipment.

Integrated system for in-situ organic peroxide production and oxidative heteroatom conversion

An oxidative treatment system, e.g., oxidative desulfurization or denitrification, is provided in which the oxidant is produced in-situ using an aromatic-rich portion of the original liquid hydrocarbon feedstock. The process reduces or replaces the need for the separate introduction of liquid oxidants such as hydrogen peroxide, organic peroxide and organic hydroperoxide in an oxidative treatment process.

Processing Hydrocarbons

Systems and methods that include providing, e.g., obtaining or preparing, a material that includes a hydrocarbon carried by an inorganic substrate, and exposing the material to a plurality of energetic particles, such as accelerated charged particles, such as electrons or ions.

METHOD TO EXTRACT BITUMEN FROM OIL SANDS USING AROMATIC AMINES

The present invention relates to an improved bitumen recovery process from oil sands. The oil sands may be surface mined and transported to a treatment area or may be treated directly by means of an in situ process of oil sand deposits that are located too deep for strip mining. Specifically, the present invention involves the step of treating oil sands with an aromatic amine. 1. A bitumen recovery process comprising the step of treating oil sands with an aromatic amine wherein the treatment is to oil sands recovered by surface mining or in situ production.2. The process of wherein the aromatic amine is described by the following structure:{'br': None, 'sup': 1', '2', '3, 'RRRN'}{'sup': 1', '2', '4', '4', '5', '6', '5', '6', '1', '2', '1', '2, 'sub': 1', '20', '6', '12', '1', '20, 'wherein Rand Rare independently —H, -AL where -AL is an unsubstituted Cto Calkyl group, a Cto Caromatically substituted Cto Calkyl group, or combination thereof, wherein -AL may contain one or more of a —COORwhere Ris —H, alkyl, aryl or alkylaryl, CN, —CHO, —NRRgroup where Rand Rare independently H, alkyl or aryl, —OH group, —O— group, —S— group, —N— group, —Cl, —Br, —F, or Rand Rmay form an unsubstituted or substituted imine, or Rand Rmay form a 5 to 7 atom saturated or unsaturated cyclic moiety wherein there may be one or more carbon atom, oxygen atom, nitrogen atom, or sulfur atom'}and{'sup': 3', '4', '4', '5', '6', '5', '6', '1', '2', '3, 'sub': 1', '20', '6', '14', '1', '20', '6', '14', '6', '14', '1', '20', '6', '14', '1', '20', '6', '14, 'Ris —H or -AR where -AR is an unsubstituted Cto Calkyl group, an unsubstituted Cto Caromatic group, or a Cto Calkyl group substituted with one or more Cto Caromatic group, or a Cto Caromatic group substituted with one or more Cto Calkyl group, or a Cto Caromatic group substituted with one or more Cto Calkyl group and/or one or more Cto Caromatic group, wherein -AR may contain one or more of a —COORwhere Ris —H, alkyl, aryl or alkylaryl, CN, —CHO, ...

Nanocatalysts For Hydrocracking And Methods Of Their Use

Novel catalysts comprising nickel oxide nanoparticles supported on alumina nanoparticles, methods of their manufacture, heavy oil compositions contacted by these nanocatalysts and methods of their use are disclosed. The novel nanocatalysts are useful, inter alia, in the upgrading of heavy oil fractions or as aids in oil recovery from well reservoirs or downstream processing. 1. A method for providing an upgraded heavy oil fraction in a well comprising:contacting a heavy oil in a well producing the heavy oil with a nanocatalyst for a time and under intrinsic well temperature conditions sufficient to increase the H/C ratio; nickel oxide nanoparticles supported on alumina nanoparticles;', 'wherein the alumina nanoparticle to nickel oxide nanoparticle weight to weight ratio in the catalyst is in a range of from about 99 to about 500;', 'wherein the particle size of the alumina nanoparticle is in the range of from about 30 to about 100 nanometers;', 'wherein the catalyst does not further comprise silver nanoparticles supported on the alumina nanoparticles; and', 'wherein the alumina nanoparticles are present in an amount of at least 99% by weight of catalyst., 'said nanocatalyst comprising2. A method according to claim 1 , said catalyst further comprising nanoparticles of at least one Group VIIIB metal oxide supported on the alumina nanoparticles; the Group VIIIB metal is selected from the group consisting of Pd and Pt, or combination thereof; and', 'the alumina nanoparticle to Group VIIIB metal oxide nanoparticle weight to weight ratio in the catalyst is in a range of from about 99 to about 500., 'wherein3. A method according to claim 1 , wherein the alumina nanoparticle to nickel oxide nanoparticle weight to weight ratio is in the range of from about 99 to about 400.4. A method according to claim 1 , wherein the nickel oxide (NiO) nanoparticles are present in an amount of about 0.2%to about 1% by weight of catalyst.5. A method according to claim 4 , wherein the SBET ...

FISCHER-TROPSCH PROCESS

The invention relates to a method for start-up and operation of a Fischer-Tropsch reactor comprising the steps of: providing a reactor with a fixed bed of Fischer-Tropsch catalyst precursor that comprises cobalt as catalytically active metal; supplying an initial hydrogen containing gaseous feed stream to the reactor, at a reduction temperature and pressure; supplying a further gaseous feed stream comprising carbon monoxide and hydrogen to the reactor; converting carbon monoxide and hydrogen supplied with the second gaseous feed stream to the reactor into hydrocarbons at a reaction temperature, wherein the reaction temperature is set at a value of at least 200° C. and hydrocarbons are produced. 2. A method according to claim 1 , wherein the nitrogen containing compound is provided to the fixed bed catalyst only:in step b) together with the initial hydrogen containing gaseous feed stream; orAfter completion of step (b) but preceding supplying the further gaseous feed stream in step (c).3. A method according to claim 1 , wherein the provision of catalyst precursor in step (a) comprises the step of:Oxidizing a fixed bed catalyst having a decreased activity due to the conversion of carbon monoxide and hydrogen into hydrocarbons, at a temperature between 20 and 400° C.4. A method according to claim 1 , wherein the catalyst precursor of step (a) is a fresh catalyst.5. A method according to claim 1 , wherein no nitrogen containing compound is present in the further gas stream.6. A method according to claim 1 , wherein the reduction temperature ranges from 200° C. to 500° C.7. A method according to claim 1 , wherein the pressure in step b) is in the range from 0.5 to 100 bar.8. Method A method according to claim 1 , wherein the initial gaseous feed stream is provided for a period of time ranging from 5 to 240 hours.9. A method according to l claim 1 , wherein the content of the nitrogen containing compound claim 1 , other than N2 claim 1 , in the initial gaseous feed stream ...

NANOCATALYSTS FOR HYDROCRACKING AND METHODS OF THEIR USE

Novel catalysts comprising nickel oxide nanoparticles supported on alumina nanoparticles, methods of their manufacture, heavy oil compositions contacted by these nanocatalysts and methods of their use are disclosed. The novel nanocatalysts are useful, inter alia, in the upgrading of heavy oil fractions or as aids in oil recovery from well reservoirs or downstream processing. 1. An upgraded heavy oil fraction prepared by a process comprising:contacting the heavy oil in a well producing heavy oil with a nanocatalyst for a time and under conditions sufficient to increase the H/C ratio; nickel oxide nanoparticles supported on alumina nanoparticles;', 'wherein the alumina nanoparticle to nickel oxide nanoparticle weight to weight ratio in the catalyst is in a range of from about 99 to about 500;', 'wherein the particle size of the alumina nanoparticle is in the range of from about 30 to about 100 nanometers;', 'wherein the catalyst does not further comprise silver nanoparticles supported on the alumina nanoparticles; and', 'wherein the alumina nanoparticles are present in an amount of at least 99% by weight of catalyst., 'said nanocatalyst comprising2. A heavy oil fraction according to claim 1 , said catalyst further comprising nanoparticles of at least one Group VIIIB metal oxide supported on the alumina nanoparticles; the Group VIIIB metal is selected from the group consisting of Pd and Pt, or combination thereof; and', 'the alumina nanoparticle to Group VIIIB metal oxide nanoparticle weight to weight ratio in the catalyst is in a range of from about 99 to about 500., 'wherein3. A catalyst according to claim 1 , wherein the ratio is in a range of from about 99 to about 400.4. A heavy oil fraction according to claim 1 , wherein the nickel oxide (NiO) nanoparticles are present in an amount of about 0.2% to about 1% by weight of catalyst.5. A heavy oil fraction according to claim 4 , wherein the SBET surface area is from about 17 to about 70 m/g.6. An upgraded heavy oil ...

Methods of Regenerating Aromatization Catalysts with A Decoking Step Between Chlorine and Fluorine Addition

Methods for regenerating a spent catalyst are disclosed. Such methods may employ a step of chlorinating the spent catalyst in the gas phase, followed by decoking the chlorinated spent catalyst, and then fluorinating the de-coked catalyst in a fluorine-containing solution of a fluorine-containing compound. 122-. (canceled)23. A method for regenerating a chlorinated spent catalyst comprising a transition metal and a catalyst support , the method comprising:(i) contacting the chlorinated spent catalyst with a decoking gas stream comprising oxygen to produce a de-coked chlorinated catalyst,wherein the chlorinated spent catalyst comprises from about 0.5 wt. % to about 3 wt. % of chlorine; and(ii) contacting the de-coked chlorinated catalyst with a fluorine-containing solution comprising a fluorine-containing compound in the liquid phase to produce a fluorinated catalyst; wherein:the transition metal comprises a Group 8-11 transition metal; andthe catalyst support comprises a large pore zeolite having an average pore diameter in a range of from about 7 Å to about 12 Å.24. The method of claim 23 , wherein the chlorinated spent catalyst further comprises fluorine.25. The method of claim 23 , wherein the chlorinated spent catalyst comprises at least about 1 wt. % carbon.26. The method of claim 23 , wherein the de-coked chlorinated catalyst comprises less than about 0.5 wt. % carbon.27. The method of claim 23 , wherein:step (i) is conducted at a peak decoking temperature in a range from about 300° C. to about 500° C.;the decoking gas stream comprises an inert gas and oxygen; andthe decoking gas stream is substantially free of halogen-containing compounds.28. The method of claim 23 , wherein an amount of the fluorine-containing compound in the fluorine-containing solution provides from about 0.1 to about 10 wt. % of fluorine (F) in the fluorine-containing solution.29. The method of claim 23 , wherein:step (ii) is conducted at a fluorination temperature in a range from about 20 ...

CONTINUOUS LIGNIN CONVERSION PROCESS

This specification discloses an operational continuous process to convert lignin as found in ligno-cellulosic biomass before or after converting at least some of the carbohydrates. The process comprises thermally treating the ligno-cellulosic biomass and then subjecting the thermally treated ligno-cellulosic biomass to a step of fiber shives reduction to produce a low viscosity slurry. The continuous process has been demonstrated to create slurry, raise the slurry to ultra high pressures, deoxygenate the lignin in a reactor over a catalyst which not a fixed bed without producing char. The conversion products of the carbohydrates or lignin can be further processed into polyester intermediates for use in polyester preforms and bottles. 148-. (canceled)50. The process according to claim 49 , wherein a part of the fiber shives reduction is done by separating at least a portion of the fiber shives having a shive length greater than or equal to 737 μm from the thermally treated ligno-cellulosic biomass.51. The process of claim 49 , wherein a part of the fiber shives reduction is done by converting at least a portion of the fiber shives having a shive length greater than or equal to 737 μm in the thermally treated ligno-cellulosic biomass to fibres or fines.52. The process of claim 49 , wherein at least a part of the fiber shives reduction step is done by applying a work in a form of mechanical forces to the thermally treated ligno-cellulosic biomass claim 49 , and all the work done by all the forms of mechanical forces on the thermally treated ligno-cellulosic biomass is less than 500 Wh/Kg per kg of the thermally treated ligno-cellulosic biomass on a dry basis.53. The process of claim 49 , wherein the thermally treated ligno-cellulosic biomass has been steam exploded before fiber shives reduction.54. The process of claim 49 , wherein the mechanical forces are applied using a machine selected from the group consisting of single screw extruders claim 49 , twin screw ...

PROCESS FOR VACUUM DISTILLATION OF A CRUDE HYDROCARBON STREAM

The invention relates to a process for vacuum distillation of a hydrocarbon stream comprising i) passing a hydrocarbon stream into a preflash vessel maintained under conditions to separate the hydrocarbon stream into a preflash liquid and a preflash vapor, ii) passing the preflash liquid into a vacuum furnace maintained under conditions to heat and partly vaporize the preflash liquid, iii) passing the heated furnace effluent into a zone located in the lower part of a vacuum distillation column maintained under fractionating conditions, and iv) passing the preflash vapor into the vacuum distillation column into a further zone located in the lower part of the vacuum distillation column. The invention also relates to a high vacuum unit (HVU) configured to perform the vacuum distillation process. 1. A process for distillation of a hydrocarbon stream at vacuum comprising i) passing a hydrocarbon stream into a preflash vessel maintained under conditions to separate the hydrocarbon stream into a preflash liquid and a preflash vapor , ii) passing the preflash liquid into a vacuum furnace maintained under conditions to heat and partly vaporize the preflash liquid , iii) passing the heated furnace effluent into a zone located in the lower part of a vacuum distillation column maintained under fractionating conditions , and iv) passing the preflash vapor into the vacuum distillation column into a further zone located in the lower part of the vacuum distillation column.2. The process according to claim 1 , wherein the further zone for introduction of the preflash vapor is located below the zone for introduction of the furnace effluent.3. The process according to claim 1 , wherein the further zone for introduction of the preflash vapor is located at the bottom of a stripping zone being located below the zone for introduction of the that the residue of the furnace effluent is contacted with preflash vapor in the stripping zone under conditions to strip the residue.4. The process ...

Nanocatalysts For Hydrocracking And Methods Of Their Use

Novel catalysts comprising nickel oxide nanoparticles supported on alumina nanoparticles, methods of their manufacture, heavy oil compositions contacted by these nanocatalysts and methods of their use are disclosed. The novel nanocatalysts are useful, inter alia, in the upgrading of heavy oil fractions or as aids in oil recovery from well reservoirs or downstream processing. 1. A catalyst comprising:nickel oxide nanoparticles supported on alumina nanoparticles; the alumina nanoparticle to nickel oxide nanoparticle weight to weight ratio in the catalyst is in a range of from about 99 to about 400;', 'the particle size of the alumina nanoparticle is in the range of from about 30 to about 100 nanometers;', 'the catalyst does not further comprise silver nanoparticles supported on the alumina nanoparticles;', 'the alumina nanoparticles are present in an amount of at least 99% by weight of catalyst; and', {'sub': 'BET', 'sup': '2', 'the Ssurface area is from about 17 to about 70 m/g.'}], 'wherein2. A catalyst according to claim 1 , wherein the nickel oxide (NiO) nanoparticles are present in an amount of about 0.2% to about 1% by weight of catalyst.3. A catalyst according to claim 2 , wherein the nickel oxide (NiO) nanoparticles are present in an amount of about 0.2% to about 0.6% by weight of catalyst.4. A catalyst according to claim 1 , further comprising nanoparticles of at least one Group VIIIB metal oxide supported on the alumina nanoparticles; the Group VIIIB metal is selected from the group consisting of Pd and Pt, or combination thereof; and', 'the alumina nanoparticle to Group VIIIB metal oxide nanoparticle weight to weight ratio in the catalyst is in a range of from about 99 to about 400., 'wherein5. A method for providing an upgraded heavy oil fraction in a well comprising:{'claim-ref': {'@idref': 'CLM-00001', 'claim 1'}, 'contacting a heavy oil in a well producing the heavy oil with a nanocatalyst according to for a time and under intrinsic well temperature ...

METHOD FOR STARTING UP A FISCHER TROPSCH PROCESS

The invention relates to a method to start up a Fischer-Tropsch process. A catalyst with a latent activity is used. The catalyst comprises titania, cobalt, promoter, and chlorine. The catalyst comprises more than 0.7 and less than 4 weight percent of the element chlorine, calculated on the total weight of the catalyst. 1. A Fischer-Tropsch catalyst that comprises:titaniabetween 5 to 35 weight percent cobalt, calculated on the total weight of the catalystin the range of between to 0.1 to 15 weight percent promoter, whereby the promoter comprises manganese, rhenium, Group 8-10 noble metals, or mixtures thereof;and more than 0.7 and less than 4 weight percent of the element chlorine, calculated on the total weight of the catalyst.2. A Fischer-Tropsch catalyst according to comprising 0.7 to less than 3 weight percent of the element chlorine.3. A Fischer-Tropsch catalyst according to comprising in the range of between 15 to 25 weight percent cobalt calculated on the total weight of the catalyst.4. A Fischer-Tropsch catalyst according to comprising in the range of between 0.5 to 5 weight percent manganese as a promoter claim 3 , calculated on the total weight of the catalyst.5. A process for preparing a Fischer-Tropsch catalyst comprising the steps of:(a1) providing a Fischer-Tropsch catalyst comprising:titaniaat least 5 weight percent cobalt, preferably in the range of between 5 to 35 weight percent cobalt, more preferably in the range of between 10 to 35 weight percent cobalt, even more preferably in the range of between 15 to 30 weight percent cobalt, still more preferably in the range of between 15 to 25 weight percent cobalt, calculated on the total weight of the catalystin the range of between to 0.1 to 15 weight percent promoter selected from the group consisting of manganese, rhenium, Group 8-10 noble metals, or mixtures thereof;(a2) impregnating the catalyst obtained in step (a1) with one or more solutions comprising chloride ions until the catalyst comprises ...

IN SITU COKING OF HEAVY PITCH AND OTHER FEEDSTOCKS WITH HIGH FOULING TENDENCY

Processes and systems for in situ heating of a heavy pitch within a coking drum are disclosed. The in situ heating may provide for processing of neat pitch, improving coking operations and increasing liquid yield. 1. A process for producing coke , the process comprising:heating a heavy pitch to an incipient coking temperature to produce a heated coker feedstock;feeding the heated coker feedstock to a coking drum;further heating the heated coker feedstock in situ within the coking drum via direct heat exchange; andsubjecting the heated coker feedstock in the coking drum to thermal cracking to crack a portion of the heavy pitch to produce a cracked vapor product and a coke product.2. The process of claim 1 , wherein the direct heat exchange is via contact of the heated coker feedstock with a superheating medium.3. The process of claim 1 , wherein the steps of heating via direct heat exchange and subjecting occur concurrently.4. The process of claim 1 , wherein the incipient coking temperature is between 500° F. and 750° F.5. The process of claim 1 , further comprising feeding the cracked vapor product to a coker separator for recovery of one or more light hydrocarbon fractions.6. The process of claim 1 , further comprising stopping the feed of heated coker feedstock to the coking drum and removal of the coke product from the coking drum.7. The process of claim 2 , wherein the superheating medium is contacted with the heated coker feedstock via one or more of a feed inlet upstream of the coking drum claim 2 , a superheating medium heater upstream of the coking drum claim 2 , or a feed inlet introducing the superheating medium directly into the coking drum.8. The process of claim 2 , wherein the superheating medium does not condense at coke drum operating conditions during a coking cycle.9. The process of claim 8 , wherein the superheating medium is one or more of steam claim 8 , carbon dioxide claim 8 , nitrogen and other inert gases claim 8 , or one or more light ...

A METHOD OF OPERATING A SLURRY BUBBLE COLUMN REACTOR

A method for starting a slurry bubble column reactor that includes a reactor vessel holding a settled or slumped bed of particles and a liquid phase from which the particles have settled includes introducing a flow of a re-suspension liquid into the settled or slumped bed to loosen the settled or slumped bed. The introduction of the re-suspension liquid takes place before the introduction of any gas into the settled or slumped bed, or together with feeding of gas into the settled or slumped bed, provided that, if gas is fed together with the re-suspension liquid into the settled or slumped bed before the settled or slumped bed has been loosened, the gas has a superficial gas velocity in the reactor below 10 cm/s. Once the settled or slumped bed has been loosened by at least the re-suspension liquid, gas is passed at a superficial gas velocity above 10 cm/s through the liquid phase. 115-. (canceled)16. A method for starting a slurry bubble column reactor that includes a reactor vessel holding a settled or slumped bed of particles and a liquid phase from which the particles have settled , the method including:introducing a flow of a re-suspension liquid into the settled or slumped bed to loosen the settled or slumped bed, the introduction of the re-suspension liquid taking place before the introduction of any gas into the settled or slumped bed, or together with feeding of gas into the settled or slumped bed, provided that, if gas is fed together with the re-suspension liquid into the settled or slumped bed before the settled or slumped bed has been loosened, the gas has a superficial gas velocity in the reactor below 10 cm/s; andonce the settled or slumped bed has been loosened by at least the re-suspension liquid, passing gas at a superficial gas velocity above 10 cm/s through the liquid phase.17. The method according to claim 16 , wherein the slurry bubble column reactor is used for Fischer-Tropsch synthesis and wherein the particles include solid Fischer-Tropsch ...

A METHOD OF SHUTTING DOWN AN OPERATING THREE-PHASE SLURRY BUBBLE COLUMN REACTOR

A method is provided of shutting down an operating three-phase slurry bubble column reactor () having downwardly directed gas distribution nozzles () submerged in a slurry body () of solid particulate material suspended in a suspension liquid contained inside a reactor vessel (), with the gas distribution nozzles () being in flow communication with a gas feed line () through which gas is being fed to the gas distribution nozzles () by means of which the gas is injected downwardly into the slurry body (). The method includes abruptly stopping flow of gas from the gas feed line () to the gas distribution nozzles () to trap gas in the gas distribution nozzles () thereby to inhibit slurry ingress upwardly into the gas distribution nozzles (). 1. A method of shutting down an operating three-phase slurry bubble column reactor having downwardly directed gas distribution nozzles submerged in a slurry body of solid particulate material suspended in a suspension liquid contained inside a reactor vessel , with the gas distribution nozzles being in flow communication with a gas feed line through which gas is being fed to the gas distribution nozzles by means of which the gas is injected downwardly into the slurry body , the method includingabruptly stopping flow of gas from the gas feed line to the gas distribution nozzles to trap gas in the gas distribution nozzles thereby to inhibit slurry ingress upwardly into the gas distribution nozzles.2. The method as claimed in claim 1 , wherein abruptly stopping flow of gas from the gas feed line to the gas distribution nozzles involves activating a fast response valve in the gas feed line to close off the gas feed line from the gas distribution nozzles.3. The method as claimed in claim 2 , wherein the fast response valve has a response time of between 1 and 10 seconds.4. The method as claimed in any of to claim 2 , wherein the gas distribution nozzles have outlets that are at the same elevation.5. The method as claimed in any of to ...

Methods for enhancing heavy oil recovery

Novel catalysts comprising nickel oxide nanoparticles supported on alumina nanoparticles, methods of their manufacture, heavy oil compositions contacted by these nanocatalysts and methods of their use are disclosed. The novel nanocatalysts are useful, inter alia, in the upgrading of heavy oil fractions or as aids in oil recovery from steam-assisted well reservoirs.

METHOD AND SYSTEMS FOR MAKING DISTILLATE FUELS FROM BIOMASS

The present invention provides methods, reactor systems and catalysts for converting biomass and biomass-derived feedstocks to C hydrocarbons using heterogenous catalysts. The product stream may be separated and further processed for use in chemical applications, or as a neat fuel or a blending component in jet fuel and diesel fuel, or as heavy oils for lubricant and/or fuel oil applications. 1. A method of making C compounds comprising:{'sub': 2+', '1+', 'x', 'y', 'z, 'catalytically reacting an aqueous feedstock solution that comprises a water soluble oxygenated hydrocarbon comprising a CO hydrocarbon with hydrogen in the presence of a deoxygenation catalyst comprising Pd, Mo, and Sn to produce a first reactant stream comprising molecules having a general formula CHOand a first reactant stream average oxygen to carbon ratio of between 0.2 and 1.0 and wherein x=2-12 carbon atoms and z=1-12 oxygen atoms;'}{'sub': p', 'r', 's', '7−, '(ii) adding to the first reactant stream a distinct second reactant stream to create a combined reactant stream that comprises carbon atoms from the first and second reactant streams, the second reactant stream comprising molecules having a general formula CHOand a second reactant average oxygen to carbon ratio of 0.2 or less, and wherein p=2-7 carbon atoms and s=0-1 oxygen atoms and the second reactant stream comprises a plurality of Ccompounds selected from the group consisting of alkanes, alkenes, cycloalkanes, cycloalkenes, and aryls,'}wherein, of the total number of carbon atoms in the combined reactant stream, greater than 10% are from the first reactant stream, and greater than 10% are from the second reactant stream,wherein the average oxygen to carbon ratio of the first reactant stream is higher than the average oxygen to carbon ratio of the second reactant stream; and{'sub': 8+', '8+', '8+', '8+', '8+', '8+', '8+, '(iii) catalytically reacting the combined reactant stream with hydrogen in the presence of an acid condensation ...

Methods for enhancing heavy oil recovery

Novel catalysts comprising nickel oxide nanoparticles supported on alumina nanoparticles, methods of their manufacture, heavy oil compositions contacted by these nanocatalysts and methods of their use are disclosed. The novel nanocatalysts are useful, inter alia, in the upgrading of heavy oil fractions or as aids in oil recovery from steam-assisted well reservoirs.

SYNTHESIS GAS CONVERSION PROCESS

The disclosed invention relates to a method for restarting a synthesis gas conversion process which has stopped. The synthesis gas conversion process may be conducted in a conventional reactor or a microchannel reactor. The synthesis gas conversion process may comprise a process for converting synthesis gas to methane, methanol or dimethyl ether. The synthesis gas conversion process may be a Fischer-Tropsch process. 123-. (canceled)24. A method for restarting a synthesis gas conversion process , wherein the synthesis gas conversion process comprises flowing synthesis gas into a reactor in contact with a synthesis gas conversion catalyst at a desired reaction temperature and pressure to produce a synthesis gas conversion product and flowing effluent comprising the synthesis gas conversion product out of the reactor , the method comprising:(A) stopping the flow of synthesis gas into the reactor;(B) flowing natural gas into the reactor to purge the reactor; and(C) restarting the flow of synthesis gas into the reactor.25. The method of wherein the synthesis gas comprises CO and prior to stopping the flow of synthesis gas into the reactor the conversion of CO is at a desired conversion value claim 24 , and after restarting the flow of synthesis gas into the reactor the conversion of CO at the desired conversion value is achieved within a time period of up to about 3 hours.2629-. (canceled)30. The method of wherein the reactor comprises a fixed bed reactor claim 24 , a fluidized bed reactor or a slurry phase reactor.31. The method of wherein the reactor comprises a conventional reactor.32. The method of wherein the reactor comprises a microchannel reactor.33. The method of wherein the synthesis gas conversion process comprises a process for converting synthesis gas to methane.34. The method of wherein the synthesis gas conversion process comprises a process for converting synthesis gas to methanol or dimethyl ether.35. The method of wherein the synthesis gas conversion ...

PROCESSING HYDROCARBONS

Systems and methods that include providing, e.g., obtaining or preparing, a material that includes a hydrocarbon carried by an inorganic substrate, and exposing the material to a plurality of energetic particles, such as accelerated charged particles, such as electrons or ions. 1. A method comprising:exposing a material comprising a hydrocarbon carried by an inorganic substrate to at least 0.5 megarads of radiation.2. The method of claim 1 , wherein the inorganic substrate comprises exterior surfaces claim 1 , and wherein the hydrocarbon is carried on at least some of the exterior surfaces.3. The method of claim 1 , wherein the inorganic substrate comprises interior surfaces claim 1 , and wherein the hydrocarbon is carried on at least some of the interior surfaces.4. The method of claim 1 , wherein the material comprises oil shale.5. The method of claim 1 , wherein the material comprises oil sand.6. The method of claim 1 , wherein the inorganic substrate comprises a material having a thermal conductivity of less than 5 W mK.7. The method of claim 1 , wherein the inorganic substrate comprises at least one of an aluminosilicate material claim 1 , a silica material claim 1 , and an alumina material.8. The method of claim 7 , wherein the substrate further comprises a noble metal claim 7 , such as platinum claim 7 , iridium claim 7 , or rhodium.9. The method of claim 7 , wherein the substrate comprises a zeolite material.10. The method of claim 9 , wherein the zeolite material has a base structure selected from the group consisting of ZSM-5 claim 9 , Zeolite Y claim 9 , Zeolite Beta claim 9 , mordenite claim 9 , ferrierite claim 9 , and mixtures of any two or more of these structures.11. The method of wherein the radiation is in the form of energetic particles.12. The method of wherein exposing the hydrocarbon to radiation reduces the molecular weight by at least about 25%.13. The method of wherein the hydrocarbon initially has a molecular weight of from about 300 to ...

AUTOMATIC DOSING OF SURFACTANT FOR RECOVERED HYDROCARBON ENHANCEMENT

Systems comprising a main tubular coupled to a pump and extending from a surface into a subterranean formation, wherein produced bulk fluid is pumped to the surface, and wherein the bulk fluid comprises at least water and a hydrocarbon, and has certain constituent parameters; a storage container for retaining the bulk fluid; a sampling tubular in fluid communication with the main tubular for sampling the bulk fluid, thereby forming at least one sampled fluid; and a dosing system coupled to the sampling tubular and configured to receive the sampled fluid, the dosing system configured to determine a constituent parameter of the sampled fluid, identify a type and concentration of separating surfactant to include in the bulk fluid to obtain a hydrophilic-lipophilic deviation (HLD) substantially equal to 0, and introduce the identified type and concentration of the separating surfactant into the storage container retaining the bulk fluid. 1. A method comprising:{'sub': p', 'c', 'cn, 'producing a bulk fluid from a subterranean formation, the bulk fluid comprising at least water and a hydrocarbon, and having constituent parameters selected from the group consisting of salinity (S), water volume (W), hydrocarbon concentration (x), equivalent alkane carbon number (EACN), surfactant concentration y, and ionic surfactant characteristic curvature (C) or nonionic surfactant characteristic curvature (C);'}sampling the bulk fluid produced from the subterranean formation, thereby forming at least one sampled fluid;manipulating the sampled fluid by adding at least one of a known component selected from the group consisting of added surfactant, added hydrocarbon, added salt, added water, and any combination thereof;determining at least one of the constituent parameters of the manipulated sampled fluid in combination with a surfactant composition based on obtaining a hydrophilic-lipophilic deviation (HLD) substantially equal to 0;{'sub': j,i', 'j,i', 'j,i', 'j,i', '3,i', 'c', {'sub2': ...

OXIDATIVE COUPLING OF METHANE AT NEAR AMBIENT FEED TEMPERATURE

Methods of performing a startup of an oxidative coupling of methane reaction to produce C+ hydrocarbons are described. The methods can include incrementally varying startup parameters of the oxidative methane reactor and using the feed gas as a coolant such that high C+ hydrocarbon selectivity is achieved. 112-. (canceled)13. A startup method for an oxidative coupling of methane reaction to produce C+ hydrocarbons , the method comprising the steps of:(a) preheating a catalyst bed of an adiabatic reactor with a heat source, wherein the catalyst bed comprises an oxidative coupling of methane catalyst;{'sub': 4', '2', '4', '2, '(b) introducing a gaseous feed stream comprising methane (CH) and oxygen (O) having a temperature of less than 350° C. and an initial CH:Omolar ratio to the adiabatic reactor;'}(c) igniting the oxidative coupling of methane reaction; and{'sub': 4', '2', '4', '2, '(d) incrementally reducing the initial CH:Omolar ratio of the gaseous feed stream introduced into the reactor to a final CH:Omolar ratio of 9:1 to 3:1 over steps (a) through (c).'}14. The method of claim 13 , wherein the initial CH:Omolar ratio is 5:1 to 40:1 and the final CH:Omolar ratio is 9:1 to 3:1 after incremental reduction.15. The method of claim 13 , wherein the temperature of the gaseous feed stream introduced into the reactor is 150° C. or less and the catalyst bed is preheated to 400° C. to 700° C.16. The method of claim 13 , wherein the catalyst bed is preheated to at least the ignition temperature of the oxidative coupling of methane reaction at the initial CH:Omolar ratio and the reactor is in an ignited condition.17. The method of claim 16 , wherein ignited conditions comprise a Zeldovich number (B) of greater than or equal to four and the product of a Damköhler number (Da) and Zeldovich number (B×Da) of greater than or equal to one.18. The method of claim 13 , wherein the heat source is removed in any one of steps (a)-(d) after the catalyst bed has been preheated.19. The ...

Synthesis gas conversion process

The disclosed invention relates to a method for restarting a synthesis gas conversion process which has stopped. The synthesis gas conversion process may be conducted in a conventional reactor or a microchannel reactor. The synthesis gas conversion process may comprise a process for converting synthesis gas to methane, methanol or dimethyl ether. The synthesis gas conversion process may be a Fischer-Tropsch process.

SYNTHESIS GAS CONVERSION PROCESS

The disclosed invention relates to a method for restarting a synthesis gas conversion process which has stopped. The synthesis gas conversion process may be conducted in a conventional reactor or a microchannel reactor. The synthesis gas conversion process may comprise a process for converting synthesis gas to methane, methanol or dimethyl ether. The synthesis gas conversion process may be a Fischer-Tropsch process. 1102-. (canceled)103. A method for restarting a synthesis gas conversion process , wherein the synthesis gas conversion process comprises flowing synthesis gas into a reactor in contact with a synthesis gas conversion catalyst at a desired reaction temperature and pressure to produce a synthesis gas product and flowing effluent comprising the synthesis gas conversion product out of the reactor , the method comprising:(A) stopping the flow of the synthesis gas into the reactor;(B) flowing hydrogen or natural gas into the reactor to purge the reactor; and(C) restarting the flow of synthesis gas into the reactor.104. The method of wherein the reactor is a conventional reactor.105. The method of wherein the reactor is a microchannel reactor.106. The method of wherein prior to step (A) the pressure within the reactor is at a pre-stoppage pressure claim 103 , and during step (A) the pressure within the reactor is reduced to a level lower than the pre-stoppage pressure claim 103 , and prior to step (B) the pressure within the reactor is increased to the pre-stoppage pressure.107. The method of wherein the catalyst is rejuvenated using hydrogen during step (B).108. The method of wherein during step (B) hydrogen flows into the reactor in contact with the catalyst at a temperature of up to 400° C. claim 103 , then air flows into the reactor in contact with the catalyst at a temperature in the range from 70° C. to 350° C. for a period of time in the range from 1 to 24 hours claim 103 , then hydrogen flows into the reactor in contact with the catalyst at a ...

FT GTL APPARATUS AND METHOD FOR PRODUCING SINGLE SYNTHETIC CRUDE OIL

Disclosed are a Fischer-Tropsch (FT) gas-to-liquid (GTL) apparatus for producing unitary synthetic crude oil and an FT GTL method for producing unitary synthetic crude oil. The FT GTL apparatus for producing unitary synthetic crude oil of the present invention is an FT GTL apparatus for producing unitary synthetic crude oil from floating production, storage, and off-loading (FPSO), and characterized by comprising: a gas injection stabilization unit for performing stabilization on the produced natural gas to generate a natural gas condensate; and a modification unit for modifying the natural gas, which has been treated in the gas injection stabilization unit, to produce a synthetic crude oil product. 1. A Fischer-Tropsch (FT) gas-to-liquid (GTL) apparatus for producing a single synthetic crude oil in a floating production , storage , and off-loading (FPSO) unit , comprising:a gas injection stabilization unit producing a natural gas condensate by stabilizing produced natural gas; anda reforming unit producing a synthetic crude oil product by reforming the natural gas treated in the gas injection stabilization unit.2. The FT GTL apparatus according to claim 1 , further comprising:a product treatment unit mixing the natural gas condensate with the synthetic crude oil product to produce a single synthetic crude oil.3. The FT GTL apparatus according to claim 2 , wherein the gas injection stabilization unit comprises a first three-phase separator separating CHto CHand H2O injected in the separator into CHto CH claim 2 , the natural gas condensate (CHto CH) claim 2 , and water (H2O).4. The FT GTL apparatus according to claim 3 , wherein the synthetic crude oil product is FT naphtha claim 3 , FT heavy oil claim 3 , and FT wax claim 3 , and the reforming unit comprises an FT reactor producing the FT wax and a second three-phase separator producing a first mixture of the FT naphtha and the FT heavy oil.5. The FT GTL apparatus according to claim 4 , wherein the second three- ...

Improved process for the dearomatization of petroleum cuts

A process for the continuous dearomatization of a petroleum cut to produce a hydrocarbon-containing fluid with a very low sulphur content and very low aromatic compounds content, includes at least one stage of catalytic hydrogenation at a temperature between 80 and 180° C. and at a pressure between 50 and 160 bar. The stage of catalytic hydrogenation of the dearomatization process comprises several interchangeable reactors linked in series.

Methods for enhancing heavy oil recovery

Novel catalysts comprising nickel oxide nanoparticles supported on alumina nanoparticles, methods of their manufacture, heavy oil compositions contacted by these nanocatalysts and methods of their use are disclosed. The novel nanocatalysts are useful, inter alia, in the upgrading of heavy oil fractions or as aids in oil recovery from steam-assisted well reservoirs.

FEEDING PYOIL AND STEAM AT CRACKER FURNACE CROSSOVER

Olefins are made by passing a cracker stream through a convection section of a cracker furnace; introducing steam and a stream comprising a recycle content pyrolysis oil into the cracker stream to form a combined stream, and the steam, r-pyoil stream, or both are introduced downstream of the inlet to the convection section, such as between the inlet to the coils and the radiant zone, or at the cross-over. Additionally, dilution steam can be added to a stream of r-pyrolysis to form a steam-diluted r-pyoil stream which is then introduced into a cracker furnace at any location, such as downstream of the inlets to the convection box or at a cross-over. 1. A method for making olefins , said method comprising:(a) passing a cracker stream through a convection section of a cracker furnace;(b) introducing steam and a stream comprising a recycle content pyrolysis oil composition (r-pyoil) into said cracker stream to form a combined stream, wherein at least one of said steam and the r-pyoil stream are introduced downstream of the inlet to said convection section; and(c) cracking said combined stream in said cracker furnace to form an olefin-containing effluent stream.2. The method of claim 1 , wherein r-pyoil is co-fed with steam at the location where steam is introduced into the convection zone.3. The method of claim 1 , wherein said r-pyoil is present in said combined stream in an amount of at least 5 weight percent claim 1 , based on the total weight of the combined stream.4. The method of claim 1 , wherein said combined stream has a steam-to-hydrocarbon ratio of at least 0.2:1.5. The method of claim 1 , wherein the residence time of the cracker feed in the radiant section is not more than 2 seconds.6. The method of claim 1 , wherein said r-pyoil stream is introduced downstream of the inlet to said convection section.7. The method of claim 1 , wherein said r-pyoil stream is introduced at a cross-over zone between said convection section and said radiant section.8. The ...

Start-up Procedure for a Fischer-Tropsch Process

The present invention generally relates to a Fischer-Tropsch process, in particular a Fischer-Tropsch process for converting a feed comprising a mixture of hydrogen and carbon monoxide gases, preferably in the form of a synthesis gas mixture, to hydrocarbons by contacting a cobalt-containing Fischer-Tropsch synthesis catalyst with a mixture of hydrogen and carbon monoxide in a reactor at a pressure of 4.0 MPa absolute or greater, wherein the process is initiated by a start-up procedure comprising the steps of: i) providing a feed comprising a mixture of hydrogen and carbon monoxide gases, preferably in the form of a synthesis gas mixture, to a reactor containing a cobalt-containing Fischer-Tropsch synthesis catalyst, wherein the pressure inside the reactor is 3.5 MPa absolute or below; and ii) maintaining the feed to the reactor, removing a product stream comprising hydrocarbons and maintaining the pressure inside the reactor at 3.5 MPa absolute or below for at least 15 hours, preferably for at least 50 hours.

System and Method for Monitoring a Reforming Catalyst

A method of monitoring catalytic performance of a catalyst used in a reforming process, comprising a) collecting gaseous component data from the reforming process; b) calculating a gaseous component ratio from the gaseous component data; and c) utilizing the gaseous component ratio to estimate an amount of catalytic activity remaining in the catalyst used in the reforming process, a number of days on stream remaining for the catalyst used in the reforming process, or both.

Process for hydrogenation of carbon monoxide

PROCEDURE FOR THE MANAGEMENT OF A REACTOR SUITABLE FOR HETEROGENEOUS REACTIONS IN COMBINATIONS WITH REACTIONS WHICH ARE CARRIED OUT IN THREE-PHASE SYSTEMS

一种费托合成用铁基催化剂、其制备方法和应用

本发明公开了一种费托合成用铁基催化剂及其制备方法和应用，该催化剂包括铁，还原助剂IB族金属Cu和/或Ag的氧化物，电子助剂IA族金属Li、Na、K或Rb，加氢助剂VIII族贵金属Ru、Rh、Pd或Pt，以及结构助剂SiO 2 。该催化剂的制备方法是将铁盐或铁盐与还原助剂IB族金属盐溶液混合，用碱性化合物进行快速共沉淀，沉淀洗涤后重新打浆，并在其中加入IA族金属的盐溶液和硅溶胶，或加入IA族金属的硅酸盐；将浆料喷雾干燥成型，然后在VIII族贵金属盐溶液中浸渍，经干燥焙烧后，制得本发明催化剂。该催化剂适用于低温费托合成反应生产烃的工艺过程，具有很高的重质烃产物收率，其中甲烷选择性很低，烯烃选择性也明显降低。

INTEGRATED SLURRY HYDROPROCESSING CATALYST AND PROCESS

An integrated catalytic process for upgrading a feed oil comprises the steps of introducing a catalyst precursor solution to a supercritical water (SCW) process unit, where the catalyst precursor solution comprises a catalyst precursor dissolved in liquid water; introducing a feed water to the SCW process unit; introducing the feed oil to the SCW process unit; treating the catalyst precursor solution, the feed water, and the feed oil in the SCW process unit to produce a SCW effluent, where the catalyst precursor is converted to catalyst particles; separating the SCW effluent in a separator unit to produce a SCW distillate product, a SCW residue product; introducing the SCW residue product to a slurry hydroprocessing unit, where the SCW residue product comprises the catalyst particles; treating the SCW residue product and the hydrogen gas in the slurry hydroprocessing unit to produce a product gas stream and an upgraded oil product. 1. An integrated catalytic process for upgrading a feed oil , the integrated catalytic process comprises the steps of:introducing a catalyst precursor solution to a supercritical water (SCW) process unit, where the catalyst precursor solution comprises a catalyst precursor dissolved in liquid water;introducing a feed water to the SCW process unit;introducing the feed oil to the SCW process unit;treating the catalyst precursor solution, the feed water, and the feed oil in the SCW process unit to produce a SCW effluent, where the catalyst precursor is converted to catalyst particles in the absence of added hydrogen and hydrogen sulfide;separating the SCW effluent in a separator unit to produce a SCW product gas, a SCW distillate product, a SCW residue product, and a water product;introducing the SCW residue product to a slurry hydroprocessing unit, where the SCW residue product comprises the catalyst particles;introducing a hydrogen gas to the slurry hydroprocessing unit; andtreating the SCW residue product and the hydrogen gas in the ...

Pre-treatment Process for Conversion of Residual Oils in a Delayed Coker Unit

The present invention relates to a sequential thermo-chemical treatment along with adsorption-based pre-treatment process for residual oils having a very high naphthenic acid content. First stage of the process is a thermal pre-treatment step which results into generation of hydrocarbon stream with a reduced naphthenic acid content due to high temperature. In second stage of pre-treatment, generated hydrocarbon stream from stage- 1 is subjected to esterification reaction with alcohol, such as methanol, to further reduce the TAN of hydrocarbon stream. After recovery of alcohol from the reaction mixture, depending on TAN reduction required reaction mixture may be subjected to an adsorption stage, third stage pre-treatment, where an adsorbent mixture comprising of FCC spent catalyst is used to adsorb the TAN of feed hydrocarbon stream. The treated hydrocarbon stream is then co-processed with DCU feed stock for producing lighter hydrocarbons.

Hydrocarbon-soluble molybdenum catalyst precursors and methods for making same

Hydrocarbon-soluble molybdenum catalyst precursors include a plurality of molybdenum cations that are each bonded with a plurality of organic anions to form an oil soluble molybdenum salt. A portion of the molybdenum atoms are in the 3+ oxidation state such that the plurality of molybdenum atoms has an average oxidation state of less than 4+, e.g., less than about 3.8+, especially less than about 3.5+. The catalyst precursors can form a hydroprocessing molybdenum sulfide catalyst in heavy oil feedstocks. The oil soluble molybdenum salts are manufactured in the presence of a reducing agent, such as hydrogen gas, to obtain the molybdenum in the desired oxidation state. Preferably the reaction is performed with hydrogen or an organic reducing agent and at a temperature such that the molybdenum atoms are reduced to eliminate substantially all molybdenum oxide species.

Highly stable hydrocarbon-soluble molybdenum catalyst precursors and methods for making same

Hydrocarbon-soluble molybdenum catalyst precursors include a plurality of molybdenum cations and a plurality of carboxylate anions having at least 8 carbon atoms. The carboxylate anions are alicyclic, aromatic, or branched, unsaturated and aliphatic, and can derived from carboxylic acids selected from 3-cyclopentylpropionic acid, cyclohexanebutyric acid, biphenyl-2-carboxylic acid, 4-heptylbenzoic acid, 5-phenylvaleric acid, geranic acid, 10-undecenoic acid, dodecanoic acid, and combinations thereof. The molybdenum salts have decomposition temperatures higher than 210° C. The catalyst precursors can form a hydroprocessing molybdenum sulfide catalyst in heavy oil feedstocks. Also disclosed are methods for making catalyst precursors and hydrocracking heavy oil using active catalysts.

Synthesis gas conversion process

Method to start a process for hydrocarbon synthesis

METHOD TO START A STEADY STATE PROCESS FOR PRODUCING NORMALLY GASEOUS, NORMALLY LIQUID AND OPTIONALLY NORMALLY SOLID HYDROCARBONS FROM SYNTHESIS GAS IN AT LEAST TWO CONVERSION REACTORS, WHICH PROCESS COMPRISES THE STEPS OF: (I) PROVIDING THE SYNTHESIS GAS; AND (II) CATALYTICALLY CONVERTING THE SYNTHESIS GAS OF STEP (I) AT AN ELEVATED STEADY STATE TEMPERATURE AND A STEADY STATE PRESSURE TO OBTAIN THE NORMALLY GASEOUS, NORMALLY LIQUID AND OPTIONALLY NORMALLY SOLID HYDROCARBONS; THE METHOD COMPRISING USING IN AT LEAST ONE CONVERSION REACTOR AN INITIAL PRESSURE FOR THE CATALYTIC CONVERSION OF THE SYNTHESIS GAS LOWER THAN THE STEADY STATE PRESSURE.

METHOD OF OPERATION OF THE REACTOR SUITABLE FOR HETEROGENEOUS REACTIONS IN COMBINATION WITH THE REACTIONS PROCEEDING IN THREE-PHASE SYSTEMS

Способ эксплуатации реактора, в котором реакции протекают в многофазных системах, где газовую фазу, преимущественно состоящую из СО и H, барботируют в суспензию из твердого вещества в форме частиц (катализатор) в жидкости (преимущественно продукт реакции), в соответствии с технологией Фишера-Тропша. A method of operating a reactor in which reactions take place in multiphase systems, where a gas phase, predominantly consisting of CO and H, is bubbled into a suspension of solid matter in the form of particles (catalyst) in a liquid (mainly the reaction product), in accordance with Fisher-Tropsch technology .

Method for safely and quickly shutting down and cleaning a hydroprocessing reactor of spent catalyst via a water flooding technique

Processes for shutting down a hydroprocessing reactor and for removing catalyst from the reactor may comprise shutting off hydrocarbon feed to the reactor, stripping hydrocarbons from the catalyst, cooling the reactor to a first threshold reactor temperature, purging the reactor with N 2 gas, introducing water into the reactor, and dumping the catalyst from the reactor, wherein the first threshold reactor temperature may be substantially greater than 200°F. In an embodiment, the water may be introduced into the reactor via a quench gas distribution system when the reactor is at a second threshold reactor temperature not greater than 200°F to cool the reactor to a third threshold reactor temperature not greater than 120°F.

Accelerated cooling process for reactors

A process for shutting down a hydroprocessing reactor and for removing catalyst from the reactor, wherein the reactor includes a quench gas distribution system. The process comprises shutting off hydrocarbon feed to the reactor, stripping hydrocarbons from the catalyst, and cooling the reactor to a first threshold reactor temperature in the range of from 375-425° F (190-218° C). At least a portion of circulating gaseous medium flowing to the reactor is then routed through a temporary heat exchanger and cooling the gas to not less than 40° F (4° C). Once cooled, mixing the cooled gas with the circulating gaseous medium flowing to the reactor. Continuing steps routing and cooling until a second threshold temperature is reached wherein the reactor temperature is in a range between 120° F and 250° F (49° C-121° C). The reactor can then be purged with N2 gas, followed by introducing water into the reactor via the quench gas distribution system. The catalyst can then be safely removed from the reactor.

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.

Method of regenerating flavouring catalyst using decoking step between steps of adding chlorine and fluorine

FIELD: chemistry. SUBSTANCE: invention relates to methods of spent catalyst regeneration. Described is a method of recovering a spent catalyst containing a transition metal of group 8–11 and a catalyst support, involving: (1) contacting the catalyst with a chlorine-containing stream containing a chlorine-containing compound in a gas phase to obtain a chlorinated spent catalyst; (2) contacting chlorinated spent catalyst with a coke burning gas stream containing oxygen to obtain a decanted catalyst; (3) contacting the decanted catalyst with a fluorine-containing solution containing a fluorine-containing compound in a liquid phase to obtain a fluorinated catalyst; and the catalyst support includes a zeolite with large pores, having average pore diameter of about 7 to about 12 Å. EFFECT: technical result is improved methods of reducing catalytic activity of spent catalysts. 41 cl, 3 ex, 2 tbl, 8 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) МПК B01J 38/42 B01J 32/00 B01J 38/12 B01J 38/46 B01J 38/48 B01J 29/90 ФЕДЕРАЛЬНАЯ СЛУЖБА B01J 29/62 ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ C10G 35/06 (12) (11) (13) 2 738 157 C1 (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 38/42 (2020.08); B01J 32/00 (2020.08); B01J 38/12 (2020.08); B01J 38/46 (2020.08); B01J 38/48 (2020.08); B01J 29/90 (2020.08); B01J 29/62 (2020.08); C10G 35/06 (2020.08) (21)(22) Заявка: 2019136624, 17.05.2018 17.05.2018 08.12.2020 Приоритет(ы): (30) Конвенционный приоритет: (56) Список документов, цитированных в отчете о поиске: US 2013/0231512 A1, 05.09.2013. US 2004/0259719 A1, 23.12.2004. RU 2014134746 A, 27.04.2016. US 20140213839 A1, 31.07.2014. US 9421529 B2, 23.08.2016. US 3418256 A, 24.12.1968. RU 2500476 C2, 10.12.2013. 17.05.2017 US 15/597,184 (45) Опубликовано: 08.12.2020 Бюл. № 34 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 17.12.2019 2 7 3 8 1 5 7 (73) Патентообладатель(и): ШЕВРОН ФИЛЛИПС КЕМИКАЛ КОМПАНИ ЭлПи (US) ...

Fe-BASED CATALYST FOR FISCHER-TROPSCH SYNTGHESIS, METHOD OF ITS MANUFACTURING AND APPLICATION

FIELD: chemistry. SUBSTANCE: claimed invention relates to Fe-based catalyst for Fischer-Tropsch synthesis, method of its manufacturing and application. Described is Fe-based catalyst for Fischer-Tropsch synthesis, which contains Fe as main component, with catalyst also containing: oxide(s) of Cu and/or Ag metal as reduction activator; at least, one oxide of metal M from IA group as electronic activator, with metal M from IA group being selected from Li, Na, K or Rb; at least, one noble metal M' of group VIII as hydrogenation activator, with noble metal M' of group VIII being selected from Ru, Rh, Pd or Pt; and SiO 2 as structure activator; and main component Fe is represented in form of its complete oxide, with Fe content in final catalyst constituting 30% wt - 70% wt. Described is method of manufacturing, consisting of the following stages: preparation of Fe salt solution; fast co-precipitation with alkaline compound, then, washing and repulpation; addition of group IB metal salt solution as reduction activator, group IA metal salt solution and silica sol, or addition of IB group metal salt solution as reduction activator and group IA metal silicate; after that, dehydration by drying via dispersion, impregnation in solution of salt of group VIII noble metal, drying and burning to obtain catalyst. Described is method of obtaining hydrocarbons by low-temperature Fischer-Tropsch synthesis with application of described above catalyst. EFFECT: high output of heavy hydrocarbons, low methane selectivity and decrease in olefins selectivity. 16 cl, 1 tbl, 6 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 468 863 (13) C1 (51) МПК B01J B01J B01J B01J B01J C07C ФЕДЕРАЛЬНАЯ СЛУЖБА C10G ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ B01J (12) ОПИСАНИЕ 23/745 23/72 23/89 21/08 37/03 1/04 2/00 23/78 ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2011137234/04, 09.02.2010 (24) Дата начала отсчета срока действия патента: 09.02.2010 (73) Патентообладатель(и): СИНФЬЮЭЛС ЧАЙНА ТЕКНОЛОДЖИ КО., ЛТД (CN) C 1 2 ...

Reducing pressure drop buildup in bio-oil hydroprocessing reactors

A method is provided involving reducing a pressure drop across a hydroprocessing reactor having a reactor feed and producing a hydroprocessing product, where the reactor feed includes a bio-oil feed and a hydrocarbon diluent; and the step of reducing the pressure drop comprises stopping or substantially reducing the bio-oil feed supplied to the reactor and supplying the hydrocarbon diluent to the reactor with a mass flux of at least about 1,000 lb/hr/ft 2 .

Reducing pressure drop buildup in bio-oil hydroprocessing reactors

A method is provided involving reducing a pressure drop across a hydroprocessing reactor having a reactor feed and producing a hydroprocessing product, where the reactor feed includes a bio-oil feed and a hydrocarbon diluent; and the step of reducing the pressure drop comprises stopping or substantially reducing the bio-oil feed supplied to the reactor and supplying the hydrocarbon diluent to the reactor with a mass flux of at least about 1,000 lb/hr/ft 2 .

反応器の洗浄方法

Moving hydrocarbons through portions of tar sands formations with a fluid

A method for treating a tar sands formation is disclosed. The method includes heating a first portion of a hydrocarbon layer in the formation from one or more heaters located in the first portion. The heat is controlled to increase a fluid injectivity of the first portion. A drive fluid and/or an oxidizing fluid is injected and/or created in the first portion to cause at least some hydrocarbons to move from a second portion of the hydrocarbon layer to a third portion of the hydrocarbon layer. The second portion is between the first portion and the third portion. The first, second, and third portions are horizontally displaced from each other. The third portion is heated from one or more heaters located in the third portion. Hydrocarbons are produced from the third portion of the formation. The hydrocarbons include at least some hydrocarbons from the second portion of the formation.

Method of removing carbon dioxide emissions from in-situ recovery of bitumen and heavy oil

The present invention, in one configuration, is directed to producing a methane- containing gas from a hydrocarbon fuel energy source extracted from an in-situ recovery operation, such as a SAGD or HAGD operation, and subsequently converting at least a portion of the gas into steam, electrical power and diluents for subsequent use in the aforementioned in-situ recovery operation while emitting only controlled amounts of carbon dioxide into the environment.

Partial solution mining of hydrocarbon containing layers prior to in situ heat treatment

A method for treating a hydrocarbon containing layer in a subsurface formation is described. The method may include removing at most about 20% by weight of the nahcolite from one or more intervals in the hydrocarbon containing layer that include at least about 40% by weight nahcolite. Heat may be provided from a plurality of heaters to the hydrocarbon containing layer such that at least some hydrocarbons in the hydrocarbon containing layer are mobilized. At least some mobilized hydrocarbons may be produced through at least one production well.

METHOD FOR HYDROCONTINUATION OF HYDROCARBON OIL

1. Способ гидроочистки углеводородного масла, использующий по меньшей мере первый реактор и второй реактор, включающий:(i) обеспечение первого потока водородсодержащего газа;(ii) гидроочистку углеводородного масла в первом реакторе с первым катализатором гидроочистки в присутствии первого потока водородсодержащего газа, обеспеченного на стадии (i), с получением первого выходящего потока;(iii) разделение первого выходящего потока, полученного на стадии (ii), на гидроочищенное углеводородное масло и использованный водородсодержащий газ с помощью отпарной колонны, использующей водородсодержащий газ в качестве отпарного газа;(iv) обеспечение второго потока водородсодержащего газа, который нагрет в секции нагревательного устройства, которое расположено выше по потоку от первого реактора, с получением потока нагретого водородсодержащего газа; и(v) контактирование во втором реакторе по меньшей мере части потока нагретого водородсодержащего газа, полученного на стадии (iv), необязательно в присутствии по меньшей мере части гидроочищенного углеводородного масла, полученного на стадии (iii), со вторым катализатором гидроочистки для получения потока использованного водородсодержащего газа и второго выходящего потока, который содержит дополнительно гидроочищенное углеводородное масло, в том случае, когда гидроочищенное углеводородное масло, полученное на стадии (iii), также присутствует.2. Способ по п. 1, в котором первый поток водородсодержащего газа и второй поток водородсодержащего газа происходят из одного и того же источника чистого водородсодержащего газа.3. Способ по п. 1 или 2, в котором подлежащее гидроочистке углеводородное масло представля РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (51) МПК C10G 65/02 (13) 2014 131 225 A (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2014131225, 27.12.2012 (71) Заявитель(и): ШЕЛЛ ИНТЕРНЭШНЛ РИСЕРЧ МААТСХАППИЙ Б.В. (NL) Приоритет(ы): (30) Конвенционный приоритет: 29.12.2011 EP ...

METHOD FOR THERMAL TREATMENT in situ WITH USE OF CLOSED-LOOP HEATING SYSTEM

FIELD: oil and gas industry. SUBSTANCE: system for thermal treatment in situ for hydrocarbons extraction from underground formation contains many well bores in formation; pipelines are arranged at least in two well bores. Moreover it includes the system of fluid circulation connected to the said pipelines; heat source is configured for heating liquid heat-carrier circulating with the aid of circulation system through pipelines with formation heating up to temperatures that allow extraction of hydrocarbons from formation. It also contains one or more electric heaters connected to pipelines configured for initial heating of pipelines up to the temperature exceeding the temperature of liquid heat-carrier hardening. Note that said electric heaters contain one or more conductors connected to the pipelines. Note that the said conductors are configured in such a way to provide power supply to pipelines for their resistance heating. Method for underground formation heating includes heating of liquid heat-carrier by heat exchanging with heat source. Note that the pipelines are heated up to the temperature enough for prevention of liquid heat-carrier hardening in pipelines. Hydrocarbons are extracted from formation. EFFECT: increase of hydrocarbons production efficiency. 19 cl, 10 dwg, 1 tbl РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 460 871 (13) C2 (51) МПК E21B 36/04 E21B 43/24 (2006.01) (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2009118919/03, 19.10.2007 (24) Дата начала отсчета срока действия патента: 19.10.2007 (72) Автор(ы): НГУЙЭН Скотт Винх (US), ВИНИГАР Харолд Дж. (US) R U (73) Патентообладатель(и): ШЕЛЛ ИНТЕРНЭШНЛ РИСЕРЧ МААТСХАППИЙ Б.В. (NL) Приоритет(ы): (30) Конвенционный приоритет: 20.10.2006 US 60/853,096 20.04.2007 US 60/925,685 (43) Дата публикации заявки: 27.11.2010 Бюл. № 33 2 4 6 0 8 7 1 (45) Опубликовано: 10.09.2012 Бюл. № 25 (56) Список документов, цитированных в отчете о поиске: US ...

Process for hydrotreating a hydrocarbon oil

탄화수소 오일은 (i) 수소-함유 가스의 제 1 스트림을 제공하는 단계; (ii) 상기 단계 (i) 에서 제공된 대로의 상기 수소-함유 가스의 제 1 스트림의 존재하에 상기 제 1 반응기에서 상기 탄화수소 오일을 제 1 수소화처리 촉매 (hydrotreating catalyst) 로 수소화처리하여 제 1 유출물을 수득하는 단계; (iii) 스트리핑 가스로서 수소-함유 가스를 이용하는 스트리핑 칼럼을 사용하여 상기 단계 (ii) 에서 수득된 대로의 상기 제 1 유출물을 수소화처리된 탄화수소 오일 및 사용된 수소-함유 가스로 분리시키는 단계; (iv) 상기 제 1 반응기의 상류에 배열된 가열 장치의 섹션 내에서 가열된 수소-함유 가스의 제 2 스트림을 제공하여 가열된 수소-함유 가스 스트림을 수득하는 단계; (v) 선택적으로 상기 단계 (iii) 에서 수득된 대로의 수소화처리된 탄화수소 오일의 적어도 일부의 존재하에, 상기 제 2 반응기에서 상기 단계 (iv) 에서 수득된 대로의 가열된 수소-함유 가스 스트림의 적어도 일부를 제 2 수소화처리 촉매와 접촉시켜 사용된 수소-함유 가스 스트림, 및 상기 단계 (iii) 에서 수득된 대로의 수소화처리된 탄화수소 오일이 또한 존재하는 경우에 추가의 수소화처리된 탄화수소 오일을 포함하는 제 2 유출물을 수득하는 단계를 포함하는, 적어도 제 1 반응기 및 제 2 반응기를 이용하는 탄화수소 오일의 수소화처리 방법으로 수소화처리된다.

method for treating bituminous sand formation.

Oil-water separation method, water reuse method using the same, and system thereof

Method of crude hydrocarbon flow vacuum distillation

FIELD: chemistry. SUBSTANCE: method of hydrocarbon flow high-vacuum distillation comprises: i) passing of the hydrocarbon flow, which represents a flow of residue leaving the crude oil distillation unit (CDU) having an initial boiling point of at least 230°C and lower than 500°C, to a pre single flash drum (10) where conditions of hydrocarbon flow separation into pre single flash liquid and pre single flash vapour are maintained. The pressure ranges from 0.1 atm (abs.) To 0.8 atm (abs.) and the temperature ranges from 340°C to 360°C; ii) passing of pre single flash liquid to a vacuum furnace (20), where conditions for heating and partial evaporation of the pre single flash liquid are maintained, iii) passing of the flow heated in a furnace to a zone (50) located in the lower part of the vacuum distillation column (30), where the fractionation conditions are maintained, and iv) passing of the pre single flash vapour to the vacuum distillation column (30) in the secondary zone (40) located in the lower part of the vacuum distillation column, wherein the secondary zone (40) for injecting the pre single flash vapour is located lower at the bottom of the steam-purge zone, shich is located lower than the zone (50) for injecting the flow escaping from the furnace, so that the residue of the flow escaping from the furnace makes contact with the pre single flash vapour in the steam-purge zone under the conditions of the residue steaming. The pre single flash vapour is used for steaming the flow ecaping from the furnace in the vacuum column. The use of aqueous vapour as a steaming medium is completely excluded. The invention also relates to a high vacuum unit (HVU) arranged for performing the method of vacuum distillation. EFFECT: energy saving due to exclusion of aqueous vapour consumption, reduced raw material supply to the furnace and increased output of paraffinic distillate. 5 cl, 2 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 621 042 C2 (51) МПК C10G 7/06 (2006.01) ...

Water Integration Between An In-Situ Recovery Operation And A Bitumen Mining Operation

The present invention relates to a method and system for integrating water between an in-situ bitumen recovery operation and a bitumen mining operation for improving efficiencies and synergies there between. A method of integrating water between a bitumen mining and extraction operation and an in-situ bitumen recovery operation comprises a) providing water associated with the bitumen mining and extraction operation; and b) directing the water, or boiler feed water or steam generated therefrom, to the in-situ bitumen recovery operation for use therein. Steam generated is used to assist in bitumen recovery at the in-situ facility. A basic system for integrating water between a bitumen mining and extraction operation and an in-situ bitumen recovery operation comprises a) a bitumen mining and extraction facility having a source of water; b) an in-situ bitumen recovery facility; c) a transporter for transporting the water, or boiler feed water or steam generated therefrom, to the in-situ bitumen recovery facility for use in an in-situ bitumen recovery operation.

Integration of an in-situ recovery operation with a mining operation

This description is directed to a method and system for integrating an in-situ bitumen recovery operation with a bitumen mining operation for improved efficiencies and synergies therebetween. The method comprises obtaining a production fluid from the in-situ bitumen recovery operation, directing the production fluid to the bitumen mining operation, and incorporating the production fluid into the bitumen mining operation. The basic integrated system comprises a production well for recovering production fluid from the in-situ bitumen recovery operation, a bitumen mining and extraction facility, and a transporter for directing the production fluid from the production well to the bitumen mining and extraction facility for incorporation into the mining and extraction operation. The in-situ recovery operation may be a thermal operation, such as steam-assisted gravity drainage (SAGD), cyclic steam stimulation (CSS), or a derivative thereof.

Process of incremental heating of hydrocarbon containing formation in chess-board order

FIELD: oil and gas production. SUBSTANCE: method includes stages, in the course of which with the aid of one or several primary heaters located in two or more first formation areas the heat is supplied to two or more first areas so that supplied heat makes the first hydrocarbons move that are located in two or more first areas; at least some quantity of movable first hydrocarbons is mined with the aid of producing wells located in two or more second areas of formation, note that the first and second areas are arranged according to the chess-board pattern. Note that according to the said pattern, at least, one of the first areas is surrounded by three or more second areas, and, at least, one of the second areas is surrounded by three or more first areas; note that part of, at least, one of the second areas that is close to, at least, one producing well receives heat by movable first hydrocarbons, note that the heat from the primary heaters is not supplied to the said part by thermal conductivity; the heat is supplied to the second areas with the aim of their additional heating by means of one or more second heaters arranged in the second areas; note that chess-board pattern processing is begun in the centre of the area or near it and then is moved spirally outside remaining the support areas that are not heated or heated with less amount of heat to resist geo-mechanical movement, shift and/or strain in the formation. EFFECT: increase of hydrocarbons production efficiency. 14 cl, 7 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 451 170 (13) C2 (51) МПК E21B 43/24 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2009118926/03, 19.10.2007 (24) Дата начала отсчета срока действия патента: 19.10.2007 (73) Патентообладатель(и): ШЕЛЛ ИНТЕРНЭШНЛ РИСЕРЧ МААТСХАППИЙ Б.В. (NL) R U Приоритет(ы): (30) Конвенционный приоритет: 20.10.2006 US 60/853,096 20.04.2007 US 60/925,685 (72) Автор(ы): ДЕ РУФФИНЬЯК Эрик Пьер (NL), ...

Nanocatalysts for hydrocracking and methods of their use

Novel catalysts comprising nickel oxide nanoparticles supported on alumina nanoparticles, methods of their manufacture, heavy oil compositions contacted by these nanocatalysts and methods of their use are disclosed. The novel nanocatalysts are useful, inter alia, in the upgrading of heavy oil fractions or as aids in oil recovery from well reservoirs or downstream processing.

Methods for enhancing heavy oil recovery

Novel catalysts comprising nickel oxide nanoparticles supported on alumina nanoparticles, methods of their manufacture, heavy oil compositions contacted by these nanocatalysts and methods of their use are disclosed. The novel nanocatalysts are useful, inter alia, in the upgrading of heavy oil fractions or as aids in oil recovery from steam-assisted well reservoirs.

Hydroprocessing bulk catalyst and methods of making thereof

A hydroprocessing bulk catalyst is provided. A process to prepare hydroprocessing bulk catalysts is also provided. The hydroprocessing catalyst has the formula (R p ) i (M t ) a (L u ) b (S v ) d (C w ) e (H x ) f (O y ) g (N z ) h , wherein M is at least at least a “d” block element metal; L is also at least a “d” block element metal, but different from M; t, u, v, w, x, y, z representing the total charge for each of the components (M, L, S, C, H, O and N, respectively); R is optional and in one embodiment, R is a lanthanoid element metal; 0<=i<=1; pi+ta+ub+vd+we+xf+yg+zh=0; 0<b; 0<b/a=<5; 0.5(a+b)<=d<=5(a+b); 0<e<=11(a+b); 0<f<=7(a+b); 0<g<=5(a+b); 0<h<=2(a+b). The catalyst has an X-ray powder diffraction pattern with at least three diffractions peak located at 2-θ angles of greater than 25°. In one embodiment, the catalyst is prepared by forming at least a sulfided catalyst precursors from at least two “d” block element metals; and mixing the catalyst precursor with a hydrocarbon compound to form the hydroprocessing catalyst composition. In another embodiment, the catalyst is prepared by the thermal decomposition of an oil dispersible sulfur containing organic metal precursor upon contact with a hydrocarbon oil, generating a slurry catalyst. In yet another embodiment, the catalyst is prepared from an in-situ or ex-situ sulfidation of “d block element metal precursors in a solvent carrier.

Hydrocarbon-soluble molybdenum catalyst precursors and methods for making same

Hydrocarbon-soluble molybdenum catalyst precursors include a plurality of molybdenum cations that are each bonded with a plurality of organic anions to form an oil soluble molybdenum salt. A portion of the molybdenum atoms are in the 3+ oxidation state such that the plurality of molybdenum atoms has an average oxidation state of less than 4+, e.g., less than about 3.8+, especially less than about 3.5+. The catalyst precursors can form a hydroprocessing molybdenum sulfide catalyst in heavy oil feedstocks. The oil soluble molybdenum salts are manufactured in the presence of a reducing agent, such as hydrogen gas, to obtain the molybdenum in the desired oxidation state. Preferably the reaction is performed with hydrogen or an organic reducing agent and at a temperature such that the molybdenum atoms are reduced to eliminate substantially all molybdenum oxide species.

Hydroprocessing Bulk Catalyst and Methods of Making Thereof

A hydroprocessing bulk catalyst is provided. A process to prepare hydroprocessing bulk catalysts is also provided. The hydroprocessing catalyst has the formula (R p ) i (M t ) a (L u ) b (S v ) d (C w ) e (H x ) f (O y ) g (N z ) h , wherein M is at least at least a “d” block element metal; L is also at least a “d” block element metal, but different from M; t, u, v, w, x, y, z representing the total charge for each of the components (M, L, S, C, H, O and N, respectively); R is optional and in one embodiment, R is a lanthanoid element metal; 0<=i<=1; pi+ta+ub+vd+we+xf+yg+zh=0; 0<b; 0<b/a=<5; 0.5(a+b)<=d<=5(a+b); 0<e<=11(a+b); 0<f<=7(a+b); 0<g<=5(a+b); 0<h<=2(a+b). The catalyst has an X-ray powder diffraction pattern with at least three diffractions peak located at 2-θ angles of greater than 25°. In one embodiment, the catalyst is prepared by forming at least a sulfided catalyst precursors from at least two “d” block element metals; and mixing the catalyst precursor with a hydrocarbon compound to form the hydroprocessing catalyst composition. In another embodiment, the catalyst is prepared by the thermal decomposition of an oil dispersible sulfur containing organic metal precursor upon contact with a hydrocarbon oil, generating a slurry catalyst. In yet another embodiment, the catalyst is prepared from an in-situ or ex-situ sulfidation of “d block element metal precursors in a solvent carrier.

Catalyst preparation unit for use in processing of heavy hydrocarbons

A catalyst preparation unit for producing an activated hydrocarbon-catalyst mixture. The catalyst preparation unit includes one or more catalyst reactant input conduits; a hydrocarbon input conduit; a water input conduit; one or more catalyst reactant mixing and conveyance systems for receiving and mixing catalyst reactants from the catalyst component input conduits and water provided by the water input conduit to provide one or more catalyst reactant solutions; one or more hydrocarbon mixing and conveyance systems for receiving and mixing the catalyst reactant solutions and hydrocarbons provided by the hydrocarbon input conduit to produce a hydrocarbon-catalyst reactant mixture; at least one reactor located downstream of the mixers, for receiving and activating the hydrocarbon-catalyst reactant mixture, thereby producing the activated hydrocarbon catalyst mixture; a gas/liquid separator located downstream of the reactor, for removing vapors and gas from the activated hydrocarbon-catalyst mixture; and an output conduit for transporting the activated hydrocarbon-catalyst mixture away from the catalyst preparation unit.

Hydrocarbon-soluble molybdenum catalyst precursors and methods for making same

Hydrocarbon-soluble molybdenum catalyst precursors include a plurality of molybdenum cations that are each bonded with a plurality of organic anions to form an oil soluble molybdenum salt. A portion of the molybdenum atoms are in the 3+ oxidation state such that the plurality of molybdenum atoms has an average oxidation state of less than 4+, e.g., less than about 3.8+, especially less than about 3.5+. The catalyst precursors can form a hydroprocessing molybdenum sulfide catalyst in heavy oil feedstocks. The oil soluble molybdenum salts are manufactured in the presence of a reducing agent, such as hydrogen gas, to obtain the molybdenum in the desired oxidation state. Preferably the reaction is performed with hydrogen or an organic reducing agent and at a temperature such that the molybdenum atoms are reduced to eliminate substantially all molybdenum oxide species.

PROCESS OF HYDROCONVERSION OF MIXTURES OF POLYMERS

Process for the running of a reactor suitable for heterogeneous reactions combined with reactions taking place in three-phase system

Process for the running of a reactor in which reactions take place in multiphase systems, wherein a gaseous phase prevalently consisting of CO and H 2 is bubbled into a suspension of a solid in the form of particles (catalyst) in a liquid (prevalently reaction product), according to the Fischer-Tropsch technology.