232results about "Refining by selective hydrogenation" patented technology

A process for preparing middle distillates from an olefinic feedstock, bya) oligomerization fed with the olefinic feedstock, a first recycle and a second recycle, and operated in the presence of at least one oligomerization catalyst, to produce a reaction effluent containing dimers, trimers and oligomers;b) fractionating the reaction effluent into:a light fraction containing at least part of the unconverted olefinic feedstock;an intermediate fraction containing at least part of the dimers and trimers; anda heavy fraction containing the oligomers;c) recycling by the preparation of a first recycle containing at least part of the light fraction; and a second recycle containing at least part of the intermediate fraction; and transfer of the first recycle and the second recycle to step a);d) hydrogenating at least part of the heavy fraction.

Disclosed is a process for producing a jet fuel, comprising a step of converting an alcohol stream in a fluidized bed, a jet fuel and a plant associated with said process. The process involves the following steps:(a) converting a C1 to C6 alcohol stream to produce a mixture containing paraffins, olefins, aromatics, and water;(b) separating water from the mixture;(c) oligomerizing olefins; and(d) alkylating aromatics from the mixture;(e) forming a stream of hydrocarbons to be hydrogenated;(f) hydrogenating the stream of hydrocarbons to be hydrogenated;(g) recovering at least one jet fuel fraction from the hydrogenated hydrocarbon stream.Conversion step (a) is carried out in a reaction zone comprising at least one fluidized catalytic bed.In the mixture of paraffins, olefins, aromatics and water produced in conversion step (a), the ratio of the mass of C3+ olefins to the total mass of olefins is greater than or equal to 0.8.

The present invention relates to a method for treating plastic pyrolysis oil, comprising: a) hydrogenating said feedstock in a mixture with at least a portion of the liquid effluent obtained from step c) in the presence of hydrogen and a catalyst at a temperature of 140-340° C.; b) hydrotreating said hydrogenated effluent in the presence of hydrogen and a catalyst; c) separating the hydrotreated effluent, said separation being carried out at high temperature and under high pressure to obtain a gaseous effluent and a liquid effluent, and recycling a portion of the liquid effluent upstream of step a); d) feeding at low temperature and under high pressure the other portion of the gaseous and liquid effluents obtained from step c) and an aqueous solution to carry out the separation and obtain a hydrocarbon-based effluent.

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.

The present invention provides a method for producing biodiesel fuel containing saturated hydrocarbons as a main component under relatively mild conditions using vegetable oils or animal fats as a raw material. [Solution] This is a method for producing biodiesel fuel from vegetable oils or animal fats, comprising a decarboxylation step in which carbon dioxide is removed from ester groups in the vegetable oils or animal fats using a decarboxylation catalyst to produce hydrocarbons, and a hydrogenation step in which the resulting hydrocarbons are hydrogenated using a hydrogenation catalyst to produce diesel fuel consisting of saturated hydrocarbons, wherein the decarboxylation step and the hydrogenation step are carried out in the stated order, and each of the decarboxylation step and the hydrogenation step is carried out under a pressure of 0.2 MPa or less.

The invention relates to a hydrocarbon fluid comprising 75 to 95% by weight of isoparaffins and less than 500 ppm by weight of aromatics relative to the total weight of the hydrocarbon fluid, said fluid having an initial boiling point and a final boiling point in the range of 120 to 240°C and a flash point of less than 90°C. The invention also relates to the use of the hydrocarbon fluid according to the invention as a solvent, for example in a paint, material coating, material treatment, sealant, polymerization, aerosol, cleaning or water treatment composition.

This invention discloses a Mg-modified hydrogenation catalyst and its preparation method. The Mg-modified hydrogenation catalyst is a sulfide-state catalyst, comprising a support, active metals Mo and Ni, and Mg. Characterized by TEM-EDS, the Mg content distributed in the Ni-Mo-S active phase region accounts for 65%-90% of the total Mg content. The modified hydrogenation catalyst of this invention can be used to treat low-quality secondary processed heavy oils, exhibiting good processing capacity and stability, especially for feedstocks with high olefin content.

The present application provides a kind of acetylene selective hydrogenation catalyst and its preparation method and application, the catalyst can be converted into ethylene by the selective hydrogenation of acetylene in carbon dioxide fraction.The catalyst comprises main active component, auxiliary active component and carrier, by regulating the type, quantity and density of carrier oxygen-containing group, the distribution of metal active component is controlled, the metal utilization is improved while the green oil generation is reduced to obtain better ethylene selectivity.

The present invention discloses a reformate hydrogenation olefin removal method, which comprises: (1) feeding a reformate raw material into a divided wall rectifying tower to obtain a tower top material C7 and components below, a side line material C8 component and a tower bottom material C9 + component; (2) respectively mixing tower top material C7 and components below and a side line material C8 component with hydrogen to obtain a first material flow and a second material flow, and carrying out contact reaction on the two material flows and a catalyst bed layer in a first hydrogenation reactor from bottom to top to obtain a first hydrogenation reaction effluent; and (3) separating the first hydrogenation reaction effluent to obtain a light component and a heavy component, mixing the heavy component with a tower bottom material C9 + component and hydrogen, feeding the mixture into a second hydrogenation reactor to obtain a second hydrogenation reaction effluent, and mixing the light component with the second hydrogenation reaction effluent to obtain a refined product. Two-stage hydrotreatment is carried out according to different fraction stage olefin removal difficulty, the olefin content in the reformate is effectively reduced, aromatic hydrocarbon saturation is reduced, and the reaction operation period is prolonged.

To provide a process for dehydrogenating normal paraffins derived from natural oils to olefins.SOLUTION: A feed stream is passed through an adsorbent bed comprising alkaline or alkaline earth cation exchange X-zeolite to remove essentially all oxygenates and aromatics from the feed stream. One or more additional adsorbent beds having different adsorbents can also be included to remove additional oxygenates and aromatics as well as sulfur compounds, nitrogen compounds, phosphorous compounds, or combinations thereof. The dehydrogenation process can be part of a process for producing alkylbenzenes from natural oils.SELECTED DRAWING: Figure 2

The invention relates to a process for hydrogenating olefins contained in an olefinic feed of the middle distillate type, derived at least in part from a renewable source, in the presence of a catalyst comprising nickel and copper, at a rate of 10% and 50% by weight of nickel relative to the total weight of the catalyst, and at a rate of 0.15% and 1.3% by weight of copper relative to the total weight of the catalyst, and a support comprising alumina.

Methods for producing olefins through hydrocarbon steam cracking include passing a hydrocarbon feed that includes one or more hydrocarbons to a hydrocarbon cracking unit and passing one or more sulfur-containing compounds to the hydrocarbon cracking unit. The sulfur-containing compounds include at least hydrogen sulfide gas, and a flow rate of the sulfur-containing compounds to the hydrocarbon cracking unit is sufficient to produce a molar concentration of elemental sulfur in the hydrocarbon cracking unit of from 10 ppm to 200 ppm. The methods include cracking the hydrocarbon feed in the hydrocarbon cracking unit to produce a cracker effluent and contacting the cracker effluent with a quench fluid in a quench unit to produce at least a cracked gas and a first pygas. The first pygas has a concentration of carbon disulfide less than 50 ppmw based on the total mass flow rate of the first pygas.

Methods for producing olefins through hydrocarbon steam cracking include passing a hydrocarbon feed that includes one or more hydrocarbons to a hydrocarbon cracking unit and passing one or more sulfur-containing compounds to the hydrocarbon cracking unit. The sulfur-containing compounds include at least hydrogen sulfide gas, and a flow rate of the sulfur-containing compounds to the hydrocarbon cracking unit is sufficient to produce a molar concentration of elemental sulfur in the hydrocarbon cracking unit of from 10 ppm to 200 ppm. The methods include cracking the hydrocarbon feed in the hydrocarbon cracking unit to produce a cracker effluent and contacting the cracker effluent with a quench fluid in a quench unit to produce at least a cracked gas and a first pygas. The first pygas has a concentration of carbon disulfide less than 50 ppmw based on the total mass flow rate of the first pygas.

The present invention provides a method for efficiently manufacturing a chemical product from a waste material including waste tires by improving each step in a series of processes. A method for producing a chemical product, the method comprising: a thermal cracking step for obtaining a first gas component, a thermally cracked oil, and a residue component by thermal cracking of a crushed product of a waste material including a waste tire; a low-temperature hydrogenation step in which a low-temperature hydrogenated oil is obtained by subjecting a starting material oil containing at least a portion of the pyrolysis oil to a low-temperature hydrogenation treatment at 180-350 DEG C; a hydrocracking step in which a raw oil containing at least a portion of the low-temperature hydrogenated oil is hydrocracked at a temperature higher than the low-temperature hydrotreating temperature to obtain a second gas component, a light component having a boiling point of 350 DEG C or less, and a heavy component having a boiling point of more than 350 DEG C; and a steam cracking step for obtaining a chemical product by subjecting the steam cracking raw oil containing at least a portion of the light component to a steam cracking treatment. In the thermal cracking step, the amount of the thermal cracked oil is 40 mass% or more with respect to the total amount of the first gas component, the thermal cracked oil, and the residue component.

A system for hydrotreating a hydrocarbon feedstock has a first stage including one or more first reactors capable of receiving the hydrocarbon feedstock and converting the hydrocarbon feedstock into an intermediate product. The feedstock has a total chlorine (Cl) content greater than 3 parts per million by weight (ppmw), and the intermediate product includes hydrogen chloride (HCl), ammonia (NH), and ammonium salts. The system also includes a heating system having a plurality of heat exchangers arranged in a loop and a heat transfer fluid capable of recovering and distributing heat to one or more fluids in the first stage. At least one heat exchanger of the plurality of heat exchangers is disposed between the first stage and the separation section, and the at least one heat exchanger is capable of maintaining a temperature of the intermediate product above the sublimation temperature of ammonia and hydrogen halide.

The invention relates to a process for producing olefins by steam cracking, in particular from feedstocks originating from plastic waste, in particular from a composition comprising a plastic liquefaction oil, said composition comprising paraffins, olefins, aromatics and heteroatoms.The process comprises: (a) a step of separating a portion of the paraffins and olefins contained in said composition comprising at least one step of crystallization (i) of said composition by lowering the temperature from 10°C to 60°C from an initial temperature at which said composition is entirely liquid and obtaining a mixture comprising a solid product enriched in paraffins and depleted in olefins, aromatics and heteroatoms and an effluent depleted in paraffins and enriched in olefins, aromatics and heteroatoms, followed by at least one step of separation (ii) of said solid product and said effluent, (b) a step of hydrotreatment of the solid product of step (a) and obtaining a hydrotreated effluent having a reduced content of olefins, and optionally a reduced content of heteroatoms and aromatics, (c) a step of steam cracking the hydrotreated effluent and obtaining an effluent containing olefins.Abstract figure: without.

A method for preparing a hydrocarbon stream for oligomerization is provided. The method uses a stripping column to strip dimethyl ether from an olefin stream. Lighter olefins, such as C3-olefins, are also removed. The C4+ olefins can then be sent for further processing, including selective hydrogenation followed by oligomerization.

1. A method for converting a hydrocarbonaceous feed containing at least 20 ppmw, at least 100 ppmw, or at least 500 ppmw and less than 1000 ppmw, 5000 ppmw, or 10000 ppmw of halides by hydrotreating in the presence of a material catalytically active in hydrotreating and an amount of hydrogen, comprising: the hydrocarbon product stream comprises an amount of ionic halides; the hydrocarbon product stream is combined with a quantity of wash water, the mass ratio of wash water to hydrocarbon product stream being greater than 1:10, greater than 1:5, or greater than 1:2, and less than 1:1, less than 2:1, or less than 10:1; wherein the combined hydrocarbon product stream and wash water are separated into a non-polar stream of hydrocarbon product and a polar stream of wash water containing ionic halides such that 50%, 90%, or 99% to 100% of the ionic halides are transferred from the hydrocarbon product stream to a polar stream of wash water containing ionic halides; An advantage associated with such a process, wherein the polar stream of wash water containing ionic halides is directed to a concentration means to provide a purified water stream and a brine stream, wherein the brine stream is characterized by having an ionic halide concentration that is more than 2 times, more than 5 times, or more than 10 times, and less than 50 times, or less than 100 times, that of the polar stream of wash water containing ionic halides, is the ability to receive a hydrocarbon mixture containing high amounts of halides and purify it into a hydrocarbon product of consistent quality while minimizing water consumption.

Provided is a process for processing circular feedstocks, renewable feedstocks, or a mix of both renewable and circular feedstocks in an ebullated bed (EB) reactor. At least a portion of the renewable and / or circular feedstocks is added to the EB reactor above its catalyst grid, while a sufficient amount of the feedstocks is injected at the bottom of the EB reactor to create the fluidized bed.

A method of producing a fuel additive includes passing a feed stream comprising C4 hydrocarbons through a hydrogenation unit producing a hydrogenated stream; passing the hydrogenated stream through a distillation unit producing a first stream and a second stream; producing an isobutylene stream by passing the first stream through a molecular sieve unit; passing the isobutylene stream to a hydration unit as a feedstock for the fuel additive; and forming the fuel additive in the hydration unit.

Finishing hydrodesulfurization catalyst comprising an active phase comprising at least one group VIB metal and at least one group VIII metal, phosphorus, and a porous support comprising alpha alumina, the content of group VIB metal, measured in oxide form, being between 1 and 8% by weight relative to the total weight of the catalyst, the content of group VIII metal, measured in oxide form, being between 0.2 and 5% by weight relative to the total weight of the catalyst, and the content of phosphorus, measured in its P2O5 form, being between 0.1 and 3% by weight relative to the total weight of the catalyst, said catalyst having a specific surface area greater than or equal to 1 m2 / g and less than 20 m2 / g. The catalyst of one example contains oxides of Co, Mo and P on alpha alumina.

Provided is a method for efficiently manufacturing a chemical product from a waste material including waste tires, which enables long-term operation of a process by improving each step in a series of processes. A method for producing a chemical product, the method comprising: a thermal cracking step for obtaining a first gas component, a pyrolytic oil, and a residue component by thermally cracking a crushed waste material including a waste tire; a low-temperature hydrogenation step in which a low-temperature hydrogenated oil is obtained by subjecting a raw oil containing at least a portion of the pyrolytic oil to low-temperature hydrogenation at 180-350 DEG C; a separation step for separating into a naphtha fraction and another fraction by atmospheric distillation of a raw oil for atmospheric distillation containing at least a portion of the low-temperature hydrogenated oil and crude oil; and a steam cracking step for obtaining a chemical product by subjecting a steam cracking raw oil containing at least a portion of the naphtha fraction to a steam cracking treatment. In the thermal cracking step, the amount of the pyrolytic oil is 40% by mass or more with respect to the total amount of the first gas component, the pyrolytic oil, and the residue component.

The present invention relates to a method for processing plastic pyrolysis oil, the method comprising: (a) selectively hydrogenating the feedstock to obtain a hydrogenated effluent; (b) hydrotreating the hydrogenated effluent to obtain a hydrotreated effluent; (c) performing a first hydrocracking step on the hydrogenated effluent to obtain a first hydrocracked effluent; (d) separating the hydrogenated effluent in the presence of an aqueous stream to obtain a gaseous effluent, a liquid aqueous effluent, and a liquid hydrocarbon effluent; (e) fractionating the liquid hydrocarbon effluent to obtain at least one gas stream, at least one naphtha fraction, and a heavier fraction; (f) performing a second hydrocracking step on the heavier fraction to obtain a second hydrocracked effluent; and (g) recycling at least a portion of the second hydrogenated effluent to the separation step (d).

The invention relates to a method for preparing a catalyst containing nickel and copper and a porous alumina support, comprising the following steps of : a) bringing the alumina support into contact with a solution containing a nickel precursor and a first organic compound having at least one carboxylic acid function; b) drying at a temperature below 250°C, then calcining at a temperature of between 250°C and 550°C; c) bringing the calcined catalyst precursor obtained at the end of step b) into contact with a solution containing a nickel precursor, a copper precursor and a second organic compound having at least one carboxylic acid function; d) drying at a temperature below 250°C.

Systems and methods for pretreating a raw mixed plastic waste pyrolysis oil using a solid adsorbent, a solid acid, a solid base and / or an ion exchange resin and then processing the pretreated mixed plastic waste pyrolysis oil by hydrotreating processes.

The invention discloses a pyrolysis gasoline first-stage catalyst and a preparation method thereof. The catalyst comprises an alumina and calcium phosphate composite carrier and a hydrogenation active component nickel, based on the weight of the catalyst, the content of nickel in terms of oxide is 10.0%-25.0%, the content of calcium phosphate is 2.5%-18.0%, and the content of alumina is 57.0%-87.5%. And the total infrared acid content of the catalyst is 0.45-0.75 mmol / g. The preparation method comprises the following steps: (1) adding calcium oxide into bottom water of a reactor, then adding an aluminum salt aqueous solution and a precipitant for gelling reaction, and then adding phosphoric acid for aging to obtain a filter cake; (2) pulping the filter cake, then adding the active metal impregnation liquid, and then adding organic acid to obtain active metal-containing modified alumina dry glue powder; and (3) uniformly mixing the active metal-containing modified alumina dry glue powder obtained in the step (2), a peptizing agent and an extrusion aid, carrying out extrusion molding, drying and roasting to obtain the catalyst product. The catalyst disclosed by the invention is applied to a pyrolysis gasoline first-stage selective hydrogenation process and has relatively high hydrogenation activity and selectivity.

A method of making a selective hydrogenation catalyst includes forming a mixed phase alumina support having a BET surface area in the range of between approximately 30 to approximately 60 square meters / gram (m2 / g). The mixed phase alumina support includes alpha alumina and theta alumina. The method also includes impregnating the mixed phase alumina support with an impregnation solution having one or more metals selected from Group VIIIB, Group IB, or both of the Periodic Table of Elements to form an impregnated support, drying the impregnated support at a temperature in the range of between approximately 100 degrees Celsius (°C) and 150 °C to form a dried impregnated support, calcining the dried impregnated support at a temperature range of between 350 °C and approximately 500 °C to form a calcined impregnated support, and reducing the one or more metals on the calcined impregnated support at a temperature in the range of between approximately 400 °C and approximately 600 °C in the presence of hydrogen to form the selective hydrogenation catalyst.

A process for producing light olefins from a hydrocarbon feed comprising arsenic at an initial quantity. The process can comprise one of more of: introducing the hydrocarbon feed to a desalter to produce a desalted hydrocarbon feed having a reduced quantity of arsenic: preheating the desalted hydrocarbon feed; introducing the preheated hydrocarbon feed to a flash separation vessel to produce an overhead fraction and a bottoms fraction; introducing the overhead fraction and steam to a radiant section of the steam cracker operated under steam cracking conditions to produce a. steam cracked effluent; and separating the steam cracked effluent to obtain a steam cracker tar, a steam cracker gas oil, a naphtha, cut, and a process gas stream; and recovering an olefin product stream from the process gas stream. Arsenic quantities in various streams in the process can be calculated and controlled.

The invention relates to the field of hydroprocessing of liquid oils such as pyrolysis oils, more specifically to the stabilization of the liquid oil by hydrotreating prior to being upgraded by further hydroprocessing. More particularly, the invention relates to the stabilization of pyrolysis oil containing polymerisable reactive compounds.