83results about "Bed hydrotreatment processes apparatus" patented technology

Electrical power derived from a renewable energy source is used to perform water electrolysis to produce oxygen and hydrogen. A flue gas and heat are produced from combustion of a fuel using at least a portion of the oxygen generated by electrolysis. A feed stream including hydrocarbon oil is hydroprocessed using the generated heat and at least a portion of the hydrogen generated by electrolysis to produce a product including a saturated hydrocarbon. At least a portion of the flue gas is hydrogenated using at least a portion of the hydrogen generated by electrolysis to produce a second product stream including a hydrocarbon, an oxygenate, or both.

A method for treating mixed plastic waste, the method comprising: (I) pyrolyzing the mixed plastic waste in a pyrolysis reactor at a temperature of 250 DEG C to 700 DEG C and a pressure of 1.0 bar to 100 bar to form a pyrolysis oil; (II) optionally transferring the pyrolysis oil directly to a hydrotreating unit via a filter, and subjecting the pyrolysis oil to hydrotreating with a catalyst in the presence of hydrogen at a temperature of 250 DEG C to 700 DEG C and a pressure of 1.0 bar to 100 bar to form a hydrotreated pyrolysis oil; (III) regenerating a portion of the hydrotreated pyrolysis oil directly from the hydrotreating unit to the pyrolysis reactor.

A method for enabling gas exchange and chemical reactions with one or more liquid streams contained in a reactive process vessel are provided. One or more exchange layers within the process vessel can be composed of both collector media and releaser media. The exchange layers allow elements to facilitate increased performance of vessel operations by promoting gas component mixing and diffusion. Improved rates of gas component exchange mean less coking and more gas components available for reaction.

The present invention provides a process for producing C2-C4 olefins from methanol and ethanol, comprising: A) feeding a feed stream A containing methanol, with or without ethanol, to a dimethyl ether fixed-bed reactor to catalytically convert the methanol to dimethyl ether to obtain a product stream A1 containing dimethyl ether, methanol, ethanol, and water vapor; B) Stream A1 is mixed with at least one hydrocarbon recycle stream R containing C2-C6 hydrocarbons and treated in an olefin fixed bed reactor to produce C2-C4 olefins, C5-C6 hydrocarbons and C7 + catalytically converting the hydrocarbon-containing crude product stream B into a crude product stream B comprising hydrocarbons; C) cooling crude product stream B to obtain hydrocarbon crude product stream C; D) separating the hydrocarbon crude product stream C into a valuable product stream comprising propylene, optionally a valuable product stream comprising ethylene, a valuable product stream comprising butenes, at least one C5-C6 hydrocarbon-containing recycle stream, and a C6 + separating the hydrocarbon-containing by-product stream into at least one by-product stream; E) recycling a portion of the C2-C4 olefins and at least a portion of the C5-C6 hydrocarbons to step B) as one or more hydrocarbon recycle streams; F) obtaining a valuable product stream comprising propylene, a valuable product stream comprising ethylene, and optionally a valuable product stream comprising butenes; G)C6 + disposing of said by-product stream comprising hydrocarbons; Including, the methanol- and ethanol-based stream A contains less than 1% by weight or 30% to 50% by weight of ethanol, in which case 30% to 60% by weight of ethylene, 30% to 60% by weight of propylene and 0% to 30% by weight of butenes are obtained as valuable products, based on 100% by weight of C2-C4 olefins, and furthermore 0% to 40% of said ethylene, 40% to 90% of said propylene and 0% to 100% of said butenes, based on the C2-C4 olefins present in the crude product stream B, are recycled to step B); Alternatively, the methanol and ethanol based stream A comprises 1% to 30% by weight of ethanol, in which case 0% to 20% by weight of ethylene, 70% to 100% by weight of propylene and 1% to 20% by weight of butenes are obtained as valuable products, based on 100% by weight of C2-C4 olefins, and further 0% to 100% by weight of said ethylene, 0% to 20% by weight of said propylene and 40% to 100% by weight of said butenes, based on the C2-C4 olefins present in the crude product stream B, are recycled to step B).

The present invention relates to a method for treating plastic pyrolysis oil, the method comprising: a) treating a plastic pyrolysis oil in the presence of hydrogen and at least one selective hydrogenation catalyst at a temperature of 100-150°C, a hydrogen partial pressure of 1.0-10.0 MPa (absolute), and an hourly space velocity of 1.0-10.0 h -1 a) selectively hydrogenating a feedstock at a temperature between 250 and 370°C and a hydrogen partial pressure between 1.0 and 10.0 MPa (absolute) to obtain a hydrogen effluent; b) hydrotreating the hydrogen effluent in the presence of hydrogen and at least one hydrotreating catalyst at a temperature between 250 and 370°C and a hydrogen partial pressure between 1.0 and 10.0 MPa (absolute) to obtain a hydrotreated effluent; c) separating the hydrotreated effluent originating from step b) in the presence of an aqueous stream at a temperature between 50 and 370°C to obtain at least one gaseous effluent, one aqueous liquid effluent and one hydrocarbon liquid effluent.

A liquid / gas reactor comprises: a primary catalyst bed having an inlet and outlet end; means for supplying a primary feed stream to the inlet end; a secondary catalyst bed having an inlet and outlet end; means for supplying a secondary feed stream to the inlet end; means for collecting at least partially converted liquid product from the outlet end of the primary catalyst bed and recycling at least a portion of the liquid product to the inlet end of the primary catalyst bed and secondary catalyst bed; a separating wall between the primary catalyst bed and secondary catalyst bed; means for supplying a primary gas stream only to the inlet end of the primary catalyst bed; and means for supplying a secondary gas stream only to the inlet end of the secondary catalyst bed. A process for carrying out a gas / liquid reaction using the reactor is also disclosed.

The present invention relates to a method and process plant for producing a hydrocarbon composition useful as a transportation fuel in accordance with commercial transportation fuel specifications from a hydrocarbonaceous feedstock containing at least 0.5% by weight of oxygen and at least 25% by weight of carbon in cyclic structures, the method and process plant comprising the steps of: a. subjecting a hydrocarbonaceous feedstock to hydroprocessing in one or more steps to provide an intermediate product containing less than 0.1 wt. % oxygen and, for fractions boiling in the range established by said commercial transportation fuel specifications, a specific gravity exceeding the upper specific gravity limit of said commercial transportation fuel specifications; b. providing from said intermediate product, optionally by fractionation, a hydrotreated hydrocarbon stream for hydroconversion, said fraction for hydroconversion meeting or exceeding the T 0 of said commercial transportation fuel specifications. 95 Less than T 50 4. The method of claim 3, c. directing said hydroconversion stream into contact with a hydroconversion catalyst under hydroconversion conditions to provide a hydroconverted hydrocarbon stream; d. Fractionating said hydroconverted hydrocarbon stream to provide at least said hydrocarbon composition useful as a transportation fuel.

The invention relates to a process and plant for hydrotreating a liquid oil stream such as pyrolysis oil stream by, in continuous operation in a fixed bed reactor, reacting the liquid oil stream with hydrogen in the presence of a reduced nickel (Ni) catalyst at a temperature of 80-250°C, a pressure of 10-200 barg, a liquid hourly space velocity (LHSV) of 0.1-6.0 h-1, and a hydrogen to liquid oil ratio, defined as the volume ratio of hydrogen to the flow of the liquid oil stream, of 100-8000 NL / L, thereby forming a stabilized liquid oil stream.

The invention relates to a process for treating a plastics and / or solid recovery fuel pyrolysis oil, comprising:a) optionally, selective hydrogenation of the feedstock;b) hydroconversion in an ebullated bed, in an entrained bed and / or in a moving bed, to obtain a hydroconverted effluent;c) hydrotreatment of said hydroconverted effluent from step b) to obtain a hydrotreated effluent, without any intermediate separation step between steps b) and c),c′) optionally, hydrocracking of said effluent from step c),c) separation of the effluent from step c) or c′) in the presence of an aqueous stream, to obtain a gaseous effluent, an aqueous liquid effluent and a liquid hydrocarbon effluent;d) optionally a fractionation to obtain at least one gas stream and one cut with a boiling point of less than or equal to 175° C. and one cut with a boiling point of greater than 175° C.

The present invention relates to a process and an apparatus for hydrotreating a liquid oil stream, such as a pyrolysis oil stream, by continuously operating in a fixed bed reactor, in the presence of a reduced nickel (Ni) catalyst, the liquid oil stream is reacted with hydrogen at a temperature of 80-250 DEG C, a pressure of 10-200 barg, a liquid hourly space velocity (LHSV) of 0.1-6.0 h <-1 >, and a hydrogen / liquid oil ratio (defined as the volume ratio of hydrogen to liquid oil stream flow) of 100-8000 NL / L to form a stabilized liquid oil stream.

The present invention provides a combined process method for treating coal tar, which comprises the following steps: (1) coal tar raw material enters a fractionation unit to obtain light distillate oil and heavy distillate oil; (2) the light distillate oil obtained in step (1) is mixed with a first hydrogen stream and then enters a microbubble generator to obtain a first mixed stream; the heavy distillate oil is mixed with a second hydrogen stream to obtain a second mixed stream; (3) the first mixed stream and the second mixed stream obtained in step (2) respectively enter an ebullating bed hydrogenation reaction zone through a gas-liquid distribution plate, undergo hydrogenation reaction in the presence of hydrogen, and the reaction effluent is subjected to gas-liquid separation to obtain a gas phase effluent and a liquid phase effluent; (4) the liquid phase effluent obtained in step (3) enters a fixed bed hydrogenation reaction zone, and the reaction effluent is separated to obtain products such as liquefied gas, naphtha, and crude white oil. The method has a high hydrogenation conversion rate and low production cost, and can also inhibit the condensation and coking reaction of unsaturated olefins contained in the coal tar, thereby achieving long-term stable operation of the device.

The present invention is a method for producing a catalyst-free olefin by continuous operation in a fixed-bed reactor at a temperature of 80 to 250°C, a total pressure of 10 to 200 barg, and a liquid hourly space velocity (LHSV) of 0.1 to 6 h -1 and a method for hydrotreating a nitrogen-enriched liquid oil stream by reacting said nitrogen-enriched liquid oil stream with hydrogen, thereby producing a stabilized liquid oil stream.

The present invention provides a multistage single reactor system for hydroprocessing and a process of carrying out multistage hydroprocessing in the said reactor assembly consisting of, a fixed bed solid catalyst system, a feed injection system enabling axial flow of hydrogen saturated hydrocarbon feed, a hydrogen dispensing system inside the reactor enabling minimum required hydrogen flow in cross-flow pattern, also using multitudes of integrated separation and withdrawal limbs for continuous staging. The innovative reactor disclosed in the present invention enables continuous separation and withdrawal of gaseous products along the reactor length by means of combined horizontal reactor orientation and vertical separation limbs provided at the top of the horizontally oriented reactor. The advantage of the reactor assembly includes effective heat sink of exothermic reactions and lower severity of operation due to removal of inhibitory gaseous products.

Provided is waste plastic pyrolysis oil refining equipment including: a guard bed 100 where a waste plastic pyrolysis oil and a hydrogen gas are introduced and hydrotreated at a first temperature in the presence of a hydrotreating catalyst to produce a fluid from which chlorine has been removed; a main bed 200 where the fluid and the hydrogen gas are introduced from the guard bed 100 and hydrotreated at a second temperature higher than the first temperature in the presence of a hydrotreating catalyst to produce a refined oil from which impurities have been removed; and a recovery tank 300 where the refined oil from which impurities have been removed is recovered from the main bed 200, wherein a temperature before the refined oil is recovered to the recovery tank 300 is maintained at 290°C or higher and lower than 350°C.

The gas-liquid distributor comprises a feeding distribution structure, a mixing main pipe (7), a transition section (8) and an outlet (10) which are communicated in sequence from bottom to top; the feed distribution structure is composed of a bubble cap (3), a flow baffle (2) and a liquid inlet pipe (4) from bottom to top, an opening in the bottom of the liquid inlet pipe is formed below the flow baffle, an opening in the top of the liquid inlet pipe is formed in the mixing main pipe, and an annular space between the side wall of the bubble cap and the main pipe is a liquid inlet (1); an air inlet (6) is formed in the pipe wall of the mixing main pipe, and a distribution component (9) is arranged in the transition section. According to the gas-liquid distributor provided by the invention, the gas phase is efficiently dispersed in the liquid phase in the form of tiny bubbles by forming jet flow and shearing at a high speed, the gas-liquid mass transfer efficiency can be remarkably improved, the reaction efficiency is further promoted, and the gas-liquid distributor is particularly suitable for a hydrocarbon oil liquid phase hydrogenation process device.

A method for preparing a hydrodemetallization catalyst, belonging to the field of catalyst preparation technology, includes the following steps: impregnating spherical carbon particles with an iron-containing solution and drying them; mixing the dried carbon particles uniformly with alumina sol and forming droplets; drying and calcining the formed products to obtain an iron-modified alumina support; immersing the iron-modified alumina support in an organic ammonium solution for a first and second hydrothermal treatment; drying and calcining the treated products to obtain a treated alumina support; impregnating the treated alumina support with an active component impregnation solution; drying and calcining the impregnated support to obtain the hydrodemetallization catalyst. The catalyst prepared by this method exhibits high dehydrogenation, Ni removal, and V removal activity, while also possessing high tolerance for metal impurities. This catalyst is particularly suitable for the hydrotreating of heavy oil with high Ni impurity content.

The present invention relates to an integrated hydro-processing reaction vessel which comprises of all the reactor, separator and stabilization sections integrated in a single vessel or system for hydro-processing of low boiling vapour phase hydrocarbon feed; as primary stream undergoing multitude of mass transfer stages with the heavy boiling liquid phase hydrocarbon feed; as secondary stream.

A process for the treatment of a mixed plastic waste comprising: (I) pyrolyzing a mixed plastic waste in a pyrolysis reactor at a temperature of 250 to 700ºC and a pressure of 1.0 to 100 bar to form a pyoil; (II) directly transferring the pyoil to a hydrotreatment unit, optionally via a filter, and subjecting said pyoil to hydrotreatment with a catalyst in the presence of hydrogen at a temperature of 250 to 700ºC and a pressure of 1.0 to 100 bar to form a hydrotreated pyoil; (III) recycling a portion of the hydrotreated pyoil directly from the hydrotreatment unit to the pyrolysis reactor.

The present disclosure relates to systems and methods for producing hydrogen among other products. In some embodiments, the method includes continuously performing a cracking step in a fixed bed mode and a flowing step in a fluidized bed mode. Such a continuous process may provide several advantages, including, for example, a step of regenerating a catalyst during the fluidized bed mode so that useful heat is generated for use in the endothermic cracking step.

The present invention relates to a process for hydrotreating a nitrogen-rich liquid oil stream by reacting the nitrogen-rich liquid oil stream with hydrogen in a continuous operation in a fixed bed reactor in the presence of a catalyst at a temperature of 80-250 DEG C, a pressure of 10-200 barg, a liquid hourly space velocity (LHSV) of 0.1-6 h <-1 > to form a stable liquid oil stream.

The present disclosure provides a method for producing aviation fuel, the method including: a first step of subjecting waste plastic pyrolysis oil to an olefin migration reaction; a second step of subjecting a product obtained in the first step to an olefin branching reaction; a third step of hydrotreating a product obtained in the second step in the presence of a hydrotreating catalyst; and a fourth step of hydrocracking a product obtained in the third step in the presence of a hydrocracking catalyst.

A liquid / gas reactor is disclosed, which includes a primary catalyst bed having an inlet end and an outlet end, a means for feeding a primary feed stream to the inlet end of the primary catalyst bed, the primary feed stream including fresh feed and recycled at least partially converted liquid product, a secondary catalyst bed having an inlet end and an outlet end, the secondary catalyst bed extending substantially vertically through the primary catalyst bed, a means for feeding a secondary feed stream to the inlet end of the secondary catalyst bed, the secondary feed stream including recycled at least partially converted liquid product, a means for collecting the at least partially converted liquid product from the outlet end of the primary catalyst bed and recycling at least a portion of the at least partially converted liquid product to the inlet ends of the primary catalyst bed and the secondary catalyst bed, a separating wall between the primary and secondary catalyst beds, a means for feeding a primary gas stream only to the inlet end of the primary catalyst bed, and a means for feeding a secondary gas stream only to the inlet end of the secondary catalyst bed. A method for carrying out a gas-liquid reaction using the reactor is also disclosed.

The invention belongs to the technical field of catalyst unloading protection, and particularly relates to a hydrogenation catalyst film-forming flame retardant and a preparation method and application thereof.The hydrogenation catalyst film-forming flame retardant is prepared from, by weight, 90-95 parts of oxygen-containing hydrocarbon, 1-5 parts of cross-linked grafted nano-silica, 5-10 parts of anionic surfactant, 0.5-1 part of dispersing agent and 5-10 parts of cosolvent. The cross-linked grafted nano silicon dioxide is dispersed in oxygen-containing hydrocarbon to form a nano fluid, so that the permeability of the film-forming flame retardant is improved, and the cross-linked grafted nano silicon dioxide quickly permeates into a caked catalyst to form a more uniform and compact passive film.

The invention relates to the technical field of Fischer-Tropsch synthetic oil hydrocracking, and discloses a Fischer-Tropsch synthetic oil hydrogenation catalyst grading method and a Fischer-Tropsch synthetic oil hydrocracking method. The method comprises the steps that a replaceable area and a main reaction area which are connected in series are sequentially arranged in the material flow direction, the replaceable area is provided with two rotation areas which are connected in parallel, during normal operation of the device, at least one rotation area and the main reaction area operate online at the same time, and the single rotation area is sequentially filled with protective agents A1, A2 and A3 in the material flow direction; and the main reaction zone is filled with a cracking catalyst B1. According to the method, various protective agents are adopted for grading, and impurities in Fischer-Tropsch oil are intercepted step by step; meanwhile, the active center of the protective agent is adjusted, the alkali metal adsorption-interception capability is improved, and the toxicity of alkali metal to the cracking main agent is reduced.

The present invention relates to multi-bed catalytic reactor with a cylindrical shape comprising a distribution device further comprising a feed distributor which is separate from a recycle fluid distributor and thus protects the feed against the higher recycle fluid temperatures.

The present invention is directed to an upwardly convex fixed-bed catalyst support (18) for a hydroprocessing reactor (10). The catalyst bed support (18) includes an upwardly convex annular-shaped perforated plate having an outer end in communication with the reactor inner surface (14), and an inner end in communication with a horizontal hub assembly.

The present invention relates to a process for hydrotreating a nitrogen rich liquid oil stream by, in a continuous operation in a fixed bed reactor, reacting the nitrogen rich liquid oil stream with hydrogen in the presence of catalyst at a temperature of 80-250°C, a pressure of 10-200 barg, a liquid hourly space velocity (LHSV) of 0.1 - 6 h-1, thereby forming a stabilized liquid oil stream.

The present disclosure provides a method for producing aviation fuel, the method including a first step of subjecting waste plastic pyrolysis oil to an olefin transfer reaction, a second step of subjecting the product of the first step to an olefin branching reaction, a third step of hydrotreating the product of the second step in the presence of a hydrotreating catalyst, and a fourth step of hydrocracking the product of the third step in the presence of a hydrocracking catalyst.

There is provided a process for hydrotreating a liquid oil stream in a continuous operation in a fixed bed reactor; wherein the liquid stream is a thermochemical decomposition oil stream, and contains polymerisable reactive compounds; wherein the fixed bed reactor comprises at least a first reactor bed containing a first hydrotreatment catalyst and a second reactor bed containing a second hydrotreatment catalyst; the process comprising the steps of: (i) in a first operation period, passing at least 50 vol.% of the liquid oil stream through the first reactor bed and subsequently through the second reactor bed; (ii) in a second operation period, on determination of deposition of material formed from the polymerisable reactive compounds on the first reactor bed, passing a reduced proportion of the liquid oil stream through the first reactor bed, and passing an increased proportion of the liquid oil stream through the second reactor bed having not passed through the first reactor bed.

A method for enabling gas exchange and chemical reactions with one or more liquid streams contained in a reactive process vessel are provided. One or more exchange layers within the process vessel can be composed of both collector media and releaser media. The exchange layers allow elements to facilitate increased performance of vessel operations by promoting gas component mixing and diffusion. Improved rates of gas component exchange mean less coking and more gas components available for reaction.