140 results about "Distillates petroleum" patented technology

A multi-stage catalytic hydrogenation and hydroconversion process for heavy hydrocarbon feed materials such as coal, heavy petroleum fractions, and plastic waste materials. In the process, the feedstock is reacted in a first-stage, back-mixed catalytic reactor with a highly dispersed iron-based catalyst having a powder, gel or liquid form. The reactor effluent is pressure-reduced, vapors and light distillate fractions are removed overhead, and the heavier liquid fraction is fed to a second stage back-mixed catalytic reactor. The first and second stage catalytic reactors are operated at 700-850.degree. F. temperature, 1000-3500 psig hydrogen partial pressure and 20-80 lb./hr per ft.sup.3 reactor space velocity. The vapor and light distillates liquid fractions removed from both the first and second stage reactor effluent streams are combined and passed to an in-line, fixed-bed catalytic hydrotreater for heteroatom removal and for producing high quality naphtha and mid-distillate or a full-range distillate product. The remaining separator bottoms liquid fractions are distilled at successive atmospheric and vacuum pressures, low and intermediate-boiling hydrocarbon liquid products are withdrawn, and heavier distillate fractions are recycled and further upgraded to provide additional low-boiling hydrocarbon liquid products. This catalytic multistage hydrogenation process provides improved flexibility for hydroprocessing the various carbonaceous feedstocks and adjusting to desired product structures and for improved economy of operations.

Production of biological diesel oil by integrated hydrogenation is carried out by mixing straight-run diesel oil with soya-bean, hydrogenation refinery reacting at 3.0-8.0MPa and 250-400degree and under existence of catalyst and converting vegetable oil into biological diesel oil. It's simple and cheap.

A hydrotreating method uses two catalyst beds with the introduction, on the last catalyst bed, of oils of animal or vegetable origin for co-treating a mixture made up of oils of vegetable or animal origin and of petroleum cuts (gas oil cuts (GO) and middle distillates) in order to produce gas oil effluents meeting specifications with an improved cetane number. The first catalyst bed is dedicated to only the deep desulfurization reactions (HDS1) of a petroleum type feed. The effluents of the first catalyst bed having an effluent sulfur content below or equal to 50 mg/kg are separated into two streams. The first stream, which is predominant, is sent to the gas oil pool. The second stream is mixed with oils of vegetable or animal origin. The resultant oil-petroleum cut mixture is then subjected to a milder hydrotreatment (HDT2). The effluents obtained at the outlet of the second catalyst bed can optionally be mixed with the predominant stream from the first bed. The process economy, the tolerance to the specifications relative to oils of animal or vegetable origin and the quality of the products obtained are thus greatly improved.

It is a purpose of this invention to accurately measure the properties of petroleum and petroleum fractions from a small volume of sample oil in a short period of time with less cost and energy for the analysis by vaporizing and distilling the respective components contained in the sample to be measured by a distillation apparatus. The components in the sample oil are first separated and vaporized by the distillation apparatus and the boiling point distribution of the respective components is measured. The property estimation means is equipped with a property estimation model for evaluating the property estimate value outputted from the property estimation model. The method is incorporated into standard or otherwise any distillation test apparatus to provide accurate measure of the thermodynamic and transport properties of undefined multicomponent mixtures such as crude oil, petroleum fractions, gas condensates and the like.

Foaming of a lube oil comprising a base stock derived from wax isomeration and an additive package is effectively reduced to within specification limits of 50 ml/ml over a temperature range of from at least 24 DEG C. to 93.5 DEG C. by adding to the oil an effective amount of an antifoamant exhibiting a spreading coefficient of at least about 2 mN/m. This has been found to be particularly effective in reducing foaming of lube oils containing a mixture of a wax isomerate oil and a petroleum oil fraction. Antifoamants typically used with conventional lube oils containing one or more petroleum fraction base stocks, but which do not exhibit a spreading coefficient of at least 2 mN/m with the wax isomerate containing oil, have been found not to be effective in reducing the foaming of the oil.

This invention relates to a process and an installation for treatment of a heavy petroleum feedstock, of which at least 80% by weight has a boiling point of greater than 340° C., whereby the process comprises the following stages:

• • (a) Hydroconversion in a fixed-bed reactor operating with an upward flow of liquid and gas, whereby the net conversion in products boiling below 360° C. is from 10 to 99% by weight;
  • (b) Separation of the effluent obtained from stage (a) into a gas containing hydrogen and H₂S, a fraction comprising the gas oil, and optionally a fraction that is heavier than the gas oil and a naphtha fraction;
  • c) Hydrotreatment by contact with at least one catalyst of at least the fraction comprising the gas oil obtained in stage (b);
  • d) Separation of the effluent obtained at the end of stage (c) into a gas containing hydrogen and at least one gas oil fraction having a sulfur content of less than 50 ppm, preferably less than 20 ppm, and more preferably still less than 10 ppm,

the hydroconversion stage (a) being conducted at a pressure P1 and the hydrotreatment stage (c) being conducted at a pressure P2, the difference ΔP=P1−P2 being at least 2 MPa, the hydrogen supply for the hydroconversion (a) and hydrotreatment (c) stages being ensured by a single compression system with n stages.

The invention relates to a process for the desulfurization of a gasoline fraction with high recovery of olefins and reduced loss of Research Octane Number (RON). A petroleum fraction is contacted with hydrogen and a commercially available hydrodesulfurization catalyst under mild conditions with to remove a first portion of the sulfur present, and is then contacted with an adsorbent for the removal of additional sulfur.

This invention relates to a process and an installation for treatment of a heavy petroleum feedstock, of which at least 80% by weight has a boiling point of greater than 340° C., whereby the process comprises the following stages: (a) hydroconversion in a boiling-bed reactor operating with a rising flow of liquid and gas, conversion in % by weight of the fraction having a boiling point of greater than 540° C. being from 10 to 98% by weight;

• • (b) separation of the effluent obtained from stage (a) into a gas containing hydrogen and H₂S, a fraction comprising the gas oil and optionally a fraction that is heavier than gas oil and a naphtha fraction; c) hydrotreatment by contact with at least one catalyst of at least the fraction comprising the gas oil obtained in stage (b); d) separation of the effluent obtained at the end of stage (c) into a gas containing hydrogen and at least one gas oil fraction having a sulfur content of less than 50 ppm, preferably less than 20 ppm, and more preferably less than 10 ppm,

the hydroconversion stage (a) being conducted at a pressure P1 and the hydrotreatment stage (c) being conducted at a pressure P2, the difference ΔP=P1−P2 being at least 3 MPa, hydrogen supply for the hydroconversion (a) and hydrotreatment (c) stages being ensured by a single compression system with n stages.

The preparation process of fraction oil hydrogenation treatment catalyst includes assistant adding modification of gamma-alumina precursor and subsequent conventional preparation process. The fraction oil hydrogenation treatment catalyst includes gamma-alumina precursoe prepared through carbonation process, aluminum nitrate process, aluminum sulfate process or aluminum chloride process; F an/or Bas assistant and W and Ni as active component. Compared with available technology, the present invention has the advantages of simple preparation process, low cost, low power consumption, and excellent catalyst performance. The catalyst of the present invention is suitable for hydrogenation treatment of 130-390 deg.c fraction oil.

A process of the present invention for producing a hydrotreated gas oil has a step for obtaining a product oil having a total aromatic content of 3% by volume or less by hydrogenating a hydrotreated oil including 95% by volume or more of fraction having a boiling point range of 150-380° C., a sulfur content of 2-15 ppm by mass, a total aromatic content of 10-25% by volume, and a naphthene of 20-60% by volume in the presence of a hydrogenation catalyst; and a step for obtaining, by hydrogenating the above-described product oil in the presence of a hydrogenation catalyst containing a crystalline molecular sieve component, a product oil satisfying the conditions that the content of petroleum fraction having a boiling point range of lower than 150° C. is 16% by volume or less, and the sum of the total aromatic content and the total naphthene content is 80% or less relative to the sum of these in the hydrotreated oil.

A heteropoly acid / ordered meso-porous silicon oxide catalyst used for removing the S-contained benzothiophenium compounds from the fractional oil of petroleum is prepared through such steps as dissolving heteropoly acid in the mixture of absolute alcohol and distilled water, adding ethyl n-silicate, magnetic stirring to obtain solution A, dissolving the polyoxyethene-polyoxypropene-polyoxyethene triblock copolymer in the mixture of absolute alcohol and distilled water to obtain solution B, slowly adding B to A, magnetic stirring to obtain sol, culturing it at 38-42 deg.C for 6-8 days, pulverizing, and calcining in N2.

The invention discloses a preparing method of coal direct liquefied initial solvent, which comprises the following steps: adopting oil distillate with distillation range at 220-538 deg.c, specific gravity at 1.01-1.10 g per cm3 and condensed-nuclei aromatics content over 70 percent; preparing coal direct liquefied initial solvent with distillation range at 220-480 deg.c, specific gravity at 0.95-0.99 g per cm3 and condensed-nuclei aromatics content over 80 percent through catalytic hydrogenation course. The method possesses excellent hydrogen supplying property and fitful viscosity, which can satisfy the direct liquefied need for coal slurry.

The invention relates to a method which can combine coal and petroleum to produce good quality fuel of a motor, which comprises the following steps: (1) the coal powder and the solvent oil are prepared into coal slurry; (2) the coal slurry is subject to hydrocracking reaction; (3) the oil products of the step (2) are subject to hydrogenation reaction after experiencing solid removal; (4) the liquefied whole fraction produced by the step (3) is subject to fractionation to get three fractions, that is, naphtha fraction, diesel fraction and fraction oil higher than 350 DEG C; (5) the diesel fraction of the step (4) is subject to depth hydrofining; (6) the high cetane value diesel produced in the process of petroleum and the products produced by the step (5) are mixed according to the needed ratio, thus obtaining motor fuel with good quality; wherein, the solvent oil of the step (1) comprises the petroleum fraction oil. The method can fully transfer heavy oil, maintain high coal slurry concentration and improve the yield of motor fuel with good quality. .

The invention relates to a method for producing high-octane gasoline by hydrocracking distillate oil of low-grade petroleum, which belongs to the technical field of petroleum refining. The method is as follows: carrying out hydrocracking ring opening and cracking reaction on distillate raw materials including straight-run distillate oil produced by atmospheric and vacuum distillation one-time processing production of the petroleum, light cycle oil produced by a catalytic cracking device, the distillate oil produced by a delayed coking device, light deasphalted oil which removes asphalt in solvent and the like of low-grade petroleum in the presence of hydrogen partial pressure and a bifunctional catalyst, and then producing blended components of the high-octane gasoline which is rich in mononuclear aromatics and the research octane number RON of 80-96, wherein the distillation range of the distillate raw materials is 160-450 DEG C. The invention provides a brand new way for upgrading the quality of the gasoline and diesel to the standard which is equivalent to European Union IV (the sulfur content in the finished product gasoline is below 50ppm, and the sulfur content in the diesel is below 50ppm) and European Union V (the sulfur content in the finished product gasoline is below 10ppm, and the sulfur content in the diesel is below 30ppm).

The invention relates to a method of hydrogenation to improve quality of solvent oil. The invention takes one or more petroleum fractions from petrol, coal oil, diesel oil as raw materials, contactly reacting with hydrogenation catalysis containing ª

A hydrogenation dearomatization catalyst containing molecular sieve consists of alumina 20.0í½80.0wt% and lucinite molecular sieve 0.5í½50.0wt%. It takes at least one Fe, Co and Ni metal of ó° family and Mo and W metal of ó÷B family as active component. It can be used for hydrogenation refining of petroleum distillate and hydrogenation dearomatization hydrocarbon of diesel oil.

The invention discloses the hydrotreatment catalyst and preparing method. The catalyst contains the 1wt%-10wt% organic auxiliary agent, using the inorganic refractory oxide compound containing the Y-molecular screen as carrier, and using the metals in the VIB and VIII as active metal componemt. The method comprises the following steps: using the inorganic refractory oxide compound containing the Y-molecular screen as carrier, after soaking the catalyst carrier in the active metal and organic auxiliary agent, drying at the 200íµ, and getting the catalyst. The said catalyst can be used for hydrotreating process of fraction of petroleum, especially for hydrodesulphurization and hydrodenitrification process of middle distillate oil.

In one exemplary embodiment, a system for reacting a first feed can include a petroleum fraction having at least about 90%, by volume, with a boiling point of at least about 300° C. The system can include a bubble column reactor. The bubble column reactor, in turn, can include a first inlet for the first feed and a second inlet for a second feed including a gas rich in hydrogen. In addition, the petroleum fraction may be in counter-current flow with respect to the gas rich in hydrogen inside the bubble column reactor.

Heavy crude transportation optimization method wherein at least one solvent consisting of a petroleum cut is added to said crude. According to the method, the polar component δ_p of the Hildebrand parameter of the solvent is increased, and the contribution of hydrogen bond δ_h of the Hildebrand parameter of the solvent is controlled, by adding a predetermined amount of at least one specific additive.

The invention relates to a coke drawing and drying method for industrial production of needle coke. The coke drawing and drying method is characterized by comprising the following steps: carrying outdelayed coking on coal tar fractions or petroleum fractions as a coking raw material from a pretreatment section by main equipment of two furnaces and three towers; respectively and continuously feeding the coking raw material into the three coking towers by a coking heating furnace; carrying out alternate circulated operation on the three coking towers. When raw materials heated by the coking heating furnace are switched from a first coking tower to a second coking tower, drawn coke and drying oil which are heated by a coke drawing and drying heating furnace are introduced into the first coking tower for drawing coke and drying, and the three coking towers carry out alternate circulated operations. According to the coke drawing and drying method disclosed by the invention, a two-furnace and three-tower industrial production flow is adopted, i.e., one coking heating furnace always heats the raw materials for the three coking towers, and the other coke drawing and drying heating furnaceheats the drawn coke and the drying oil for the three coking towers; the properties of the materials heated by the two heating furnaces are always consistent; the coke drawing and drying method has the advantages that the operation is simple and stable, coke drawing and drying are sufficient, and the quality and the yield of a product are improved.