WO2011067634A2 - Procédé d'hydrotraitement de fractions lourdes de pétrole mélangées à de l'huile végétale - Google Patents

Procédé d'hydrotraitement de fractions lourdes de pétrole mélangées à de l'huile végétale Download PDF

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Publication number
WO2011067634A2
WO2011067634A2 PCT/IB2010/002149 IB2010002149W WO2011067634A2 WO 2011067634 A2 WO2011067634 A2 WO 2011067634A2 IB 2010002149 W IB2010002149 W IB 2010002149W WO 2011067634 A2 WO2011067634 A2 WO 2011067634A2
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Prior art keywords
oil
mixture
hydrotreatment
heavy
hydrotreated
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English (en)
Spanish (es)
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WO2011067634A3 (fr
Inventor
Manuel Laureano NUÑEZ ISAZA
Cesar Augusto Maecha Bohorquez
Hernando Delgado Gamboa
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Ecopetrol SA
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Ecopetrol SA
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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C10G3/42—Catalytic treatment
    • C10G3/44—Catalytic treatment characterised by the catalyst used
    • C10G3/45—Catalytic treatment characterised by the catalyst used containing iron group metals or compounds thereof
    • C10G3/46—Catalytic treatment characterised by the catalyst used containing iron group metals or compounds thereof in combination with chromium, molybdenum, tungsten metals or compounds thereof
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C10G3/50—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids in the presence of hydrogen, hydrogen donors or hydrogen generating compounds
    • C10G3/52—Hydrogen in a special composition or from a special source
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
    • C10G45/06—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
    • C10G45/08—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1011—Biomass
    • C10G2300/1014—Biomass of vegetal origin
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1011—Biomass
    • C10G2300/1018—Biomass of animal origin
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4006—Temperature
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4012—Pressure
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4018—Spatial velocity, e.g. LHSV, WHSV
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock

Definitions

  • This invention relates to the hydrotreatment (HDT) of heavy petroleum fractions using hydrotreatment plants normally used in oil refineries for this purpose.
  • the application refers to the coprocessing of heavy oil fractions with natural oils of organic origin.
  • the process described in this invention allows to coprocess the natural oil of organic origin together with the heavy derivatives of the refining process, and subsequently recover most of the engine fuel from the hydrotreated organic oil separately from the rest of the products, using the same equipment for hydrotreatment of heavy fractions
  • Heavy fractions of petroleum are the non-distillable part of petroleum and consist of high molecular weight molecules, especially aromatic, with high content of heteroatoms, such as sulfur, nitrogen and metals, including nickel and vanadium.
  • the H / C ratio is higher, since the current with GV-HDT was hydrotreated before being mixed with sunflower oil.
  • the increase in the H / C ratio is much greater for mixtures with larger quantities of biocomponents (70/30), indicating that co-processing affects the heavy hydrocarbon molecules of the sunflower oil in the mixture.
  • the results show that the presence of sunflower oil inhibits the conversion of hydrocracking (especially when using non-hydrotreated GV).
  • a +3 increase in the cetane number of the 10% mixture of cottonseed and diesel oil is obtained by Sebos, A. Matsoukas, V. Apostolopoulos, N. Papayannakos. "Catalytic hydroprocessing of cottonseed oil with diesel oil blends for the production of renewable diesel”. Fuel 88. 145-149. 2009. These authors evaluate the conversion of esters present in the refined oil of cottonseed with desulphurized petroleum diesel by hydrotreatment with C0M0 / AI 2 O 3 catalyst. The conversion of esters is determined in the temperature range of 305 ° C- 345 ° C, at 30 bar pressure and 5 h "1 ⁇ VE ⁇ 25 h " 1 . The hydrogen feed is 23-24 NL / h.
  • the results of simulated distillation for the hydrotreatment of APV - sunflower oil mixtures ranging from 5 to 50% by weight hydrotreated at reaction temperatures between 300 ° C to 450 ° C.
  • the yield of the 50 ° C to 60 ° C fractions increases with increasing temperature and sunflower oil content in the mixture. This fraction is mainly (more than 40%) CO, C0 2 and propane.
  • the yields of the other two low boiling cuts (65 ° C -150 ° C and 150 ° C -250 ° C) also increase with temperature and only slightly increase with the increase of sunflower oil.
  • the percentage of linear chain alloys in the cut of 150 ° C - 250 ° C is less than 16%, but increases with the increase in vegetable oil content.
  • the yield of the fraction of 250 ° C -380 ° C (which is the fraction containing n-Ci 5 - n-Ci 8 ) increases with the increase in sunflower oil content. This cut also increases with the increase in temperature when the mixture contains less than 30% by weight sunflower oil. For the mixture with 50% by weight sunflower oil this fraction increases with the increase in the reaction temperature from 300 ° C to 350 ° C, and then decreases with the increase in the reaction temperature to 450 ° C.
  • WO2008084145 describes the use of two HDT plants at different conditions for the co-treatment of a mixture of oils of vegetable or animal origin (1 to 99% v / v) and cuts of medium petroleum distillates (99 to 1% v / v) with an intermediate offal to produce fuel oil bases with standard specifications in terms of sulfur, density and cold properties.
  • the first plant (HDT1) is used for the reactions of oils of vegetable or animal origin while the hydrocarbon load is pretreated.
  • the second plant (HDS2) works under more severe conditions to obtain diesel fuel according to standards (sulfur content, density and cold properties).
  • the HDT1 plant operates at temperatures between 180 ° C and 360 ° C, pressure from 0.5 to 20 MPa, space velocity between 0.2 h "1 to 5 h " 1 , hydrogen / feed ratio of 50 to 2000 NL / L.
  • the HDS2 plant works at temperatures between 180 ° C and 450 ° C, pressure from 0.5 to 50 MPa, space velocity between 0.1 to 20 h "1 , hydrogen / food ratio of 50 to 2000 NL / L.
  • WO2008087269 discloses hydrotreatment using two series catalytic beds (HDS1 and HDT2).
  • HDS1 a deep hydrodesulfurization of oil cuts (diesel cuts and medium distillates) is performed, to obtain a product with standard specifications in the sulfur content.
  • a stream of vegetable or animal oil (1 to 99% v / v) mixed with part of the effluent from the HDS1 plant (99 to 1% v / v) is introduced.
  • the oil and effluent mixture of HDS1 is subjected to gentle hydrotreatment (HDT2) to obtain a diesel with the required specifications, in terms of sulfur content (less than 50 mg / kg), density and cold properties.
  • HDT2 gentle hydrotreatment
  • the deep hydrodesulfurization stage is carried out at temperatures between 250 ° C and 440 ° C, pressure between 1 and 25 MPa, spatial velocity of 0.2 h “1 to 4 h “ 1 , Hydrogen feed ratio between 50 to 2000 NUL
  • US patent application 20080229654 describes an integrated process for the production of fuels, including jet fuel, gasoline and diesel.
  • the process involves thermal decarboxylation of fatty acids derived from triglyceride hydrolysis to form a product, which is combined with a fraction of low molecular weight olefins, such as those obtained in the Fischer-Tropsch synthesis and subjected to reactions molecular.
  • the products can be subjected to hydrocracking or isomerization reactions, and are separated into the ranges of gasoline, diesel fuel and / or jet.
  • the resulting composition has relatively high octane values and low sulfur concentration.
  • US patent application 20070260102 describes the conversion of vegetable oils for the production of n-paraffins, by hydrotreating vegetable oil and / or natural fats in a pure state or mixed with hydrocarbon (kerosene). This mixture is subjected to a hydrotreatment process, obtaining a product with a high content of n-paraffins in the range C 10 -C13. Hydrotreatment is performed at a pressure between 7 to 15 MPa, a spatial velocity of 0.5 h "1 to 2 h " 1 , at a hydrogen / mixture ratio between 200 to 1000 NL of hydrogen / L mixture.
  • Patent application EP 1693432 describes the hydroconversion process of vegetable oils including the hydrotreatment of oils and / or natural fats in a proportion between 1 and 75% by weight combined with a hydrocarbon flow between 99 and 25% by weight, in a hydrotreatment reactor under pressures of 4 to 10 MPa, with a bed temperature between 320 ° C and 400 ° C, the space velocity is 0.5 h "1 to 2 h " 1 and NiMo catalysts are used or CoMo, the hydrogen charge ratio between 200 to 1000 NL of hydrogen / liter charged. Heavy diesel, light diesel and a mixture of light cycle oil and / or diesel were used as hydrocarbon fillers. The product obtained has a boiling point in the diesel range, an improved cetane number and a density lower than that obtained by hydrotreating the pure hydrocarbon charge.
  • the above US20080244962 teaches a method to produce a soparaffinic product useful as jet fuel and a fraction of liquefied petroleum gas (LPG) from a renewable raw material.
  • the method includes a hydrotreatment unit of the renewable raw material to produce a heavy fraction that includes n-paraffins.
  • Another hydroisomerization unit produces iso-paraffins from the n-paraffin stream.
  • the method also includes recycling of the hydroisomerized heavy fraction to have a soparaffinic product that can be fractionated into the fuel fractions for jet and LPG.
  • the jet fuel obtained has improved cold flow properties.
  • US 20080281134 discloses a method for producing C10-C30 hydrocarbons from fatty compounds in which at least a portion of the hydrogen required to carry out the conversion is generated from the by-products of the conversion process.
  • Light hydrocarbons, especially propane, produced during the conversion of triglycerides are used to generate hydrogen, which is used in the conversion process and thus reduce the need for external hydrogen sources.
  • WO2009068981 relates to a process that consists in obtaining diesel fuel from vegetable or animal oils by adding hydrogen in the presence of catalysts at appropriate temperature and pressure conditions.
  • the process disclosed here differs from similar ones in that it presents spatial speeds between 5.1 h-1 and 9.0 h-1, which reduces the size of the reactor and the consumption of hydrogen, also reducing the costs of construction of equipment and operation.
  • the products obtained by this process are part of the invention, which have shown that in additions, even below 10%, they improve the performance of diesel engines, thus lowering fuel consumption.
  • the process of the invention consists in the hydrotreatment of mixtures of heavy petroleum fractions, such as vacuum bottoms, atmospheric bottoms and defaulted bottoms (BMD) with natural oils of organic origin, using the catalyst used for fraction hydrotreatment.
  • the transport fuel thus obtained can also be used as raw material to produce jet fuel after being subjected to an isomerization step.
  • the present process is based on the simultaneous treatment of heavy fractions of oil and natural oil of organic origin in order to reduce the total consumption of hydrogen and energy required, compared to the consumption for separate hydrotreatment processes for each One of the compounds.
  • Figure 1 shows the general diagram of the invention process.
  • Figure 2 shows the simulated distillation curve of the hydrotreated heavy fraction, the simulated distillation curve of the natural oil of hydrotreated organic origin and the simulated distillation curve of the theoretical mixture (15% hydrotreated oil + 85% DMOH) constructed from of simulated distillation curves of pure currents.
  • Figure 3 shows the comparison of the actual distillation curve of the mixture of 15% hydrotreated oil + 85% DMOH and the simulated distillation curve of the theoretical mixture (15% hydrotreated oil + 85% DMOH) constructed from the curves simulated distillation of pure streams.
  • Figure 4 shows the theoretical distillation curves of mixtures with different percentages of hydrotreated oil and DMOH compared to the actual distillation curve of the mixture of 15% oil + 85% DMOH.
  • Figure 1 shows the flow diagram of the equipment involved in the processing of the natural oil mixture of organic origin and the heavy oil fractions.
  • Natural oil of organic origin from the tank (1) is pumped by the pump (3) through the line (101) to the mixer (5) where it is combined with the heavy fraction taken from the tank (2) by the pump (4) ) through the line (102).
  • the line (103) takes the mixture of the natural oil of organic origin and the heavy fraction, combining it with the hydrogen coming from the line (110), to the oven (6) where the preheated mixture from the line (104) leaves to the reactor of h id rotation (7).
  • the products of the reactor (7) are taken along the line (105) to a separation system (8), from which a stream (107) containing water (A), a stream of hydrogen-rich gases flows through the line ( 106), this is treated in a purification system (10) before being recycled along the line (108) and compressed in a compression system (11). Hydrogen The tablet is mixed with fresh hydrogen (12) that is transported along the line (109) forming the current (110) that enters the process again.
  • the stream (111) is taken to a distillation tower (9) where hydrotreated oil (B) is obtained from the top (112) and hydrotreated heavy fractions (C) from the bottom (113).
  • the mixture is formed by an amount of natural oil of organic origin between 5% v / va 50% v / v, preferably between 10% v / va 20% v / v and the amount of heavy fraction ranges from 50 to 95% v / v, preferably between 80% v / va 90% v / v.
  • Operational hydrotreatment conditions are pressures between 4 MPa and 15 MPa, reactor inlet temperature from 250 ° C to 350 ° C, reaction temperature from 300 ° C to 400 C, space velocity from 0.5 h 1 to 2 h 1 and H 2 / load ratio between 140 and 840 LN / L.
  • the catalyst used is formed by metal sulphides of the groups Vl-B (Mo and W) and VII (Co and Ni). Said catalyst can be fresh or used.
  • Natural oil of organic origin is mixed with heavy fractions of oil and is passed through the reactors.
  • the triglyceride components of the oil are divided into three smaller molecules that are in the diesel range and have the facility of being separated from the heavy current using flash and subsequent distillation systems.
  • the catalysts used in hydrotreatment are basically partially or totally sulfurized metal oxides for activation.
  • the active phases of the catalyst carry out the hydrogenolysis and hydrogenation processes.
  • the catalyst support provides a high surface area, mechanical resistance, thermal stability, preventing sintering.
  • There is a synergy effect between the metal sulphides of the groups Vl-B (Mo and W) and VII (Co and Ni) in reactions involved in the hydrotreatment process thus the activity of the catalysts containing sulphides of both groups is higher compared to the activity of individual sulphides.
  • the process set forth in this invention consists of the mixing steps of the natural oil and the heavy fraction, the heating of the mixture, the reaction and the distillation separation, as shown in Figure 1.
  • F. Lead the mixture to a second separation system (9) to obtain by distillation the two main products, hydrotreated oil and hydrotreated heavy fractions.
  • g. Process the recovered hydrogen in the first separation system by purifying it in the system (10), compressing it in the system (11) and mixing it with fresh hydrogen from the stream (109) coming from the tank (12) before being recirculated to the process in the current (103).
  • Natural oils of organic origin that can be used for said process are selected from the group consisting of vegetable oils, seaweed oils, animal oils, animal fats or mixtures thereof.
  • Figure 3 represents a comparison between the distillation curves of the mixture 15% organic natural oil + 85% DMOH with the theoretically obtained curve by adding the two distillation curves of hydrotreated oil and DMOH. It is observed that the behavior of the two curves is very similar, which allows us to assume that the behavior of the different mixtures, both real and theoretical, will present this same trend.
  • Figure 4 shows the trend of distillation curves of different mixtures with a variation of 5%, 10% and 20% in the percentage of natural oil hydrotreated and compared with the distillation curves of the mixture 15% natural oil hydrotreated + 85% real and theoretical DMOH. It is observed that the mixtures with 5% and 20% of hydrotreated natural oil move a little away from the actual distillation curve, which allows to conclude that above or below these values it is not possible to separate at the established conditions of the process.
  • Table 1 shows the properties of natural oil of organic origin and heavy defaulted fractions (BMD) used as raw material in the hydrotreatment process.
  • Vanadium content (mg / Kg) 16.51 -
  • Table 2 shows the properties of the mixture of hydrotreated natural oil + hydrotreated heavy fraction compared to the hydrotreated oil obtained from the hydrotreatment of 100% natural oil of organic origin. It is observed that the product obtained after the hydrotreatment of the mixture contains a higher proportion of hydrotreated oil with light fractions, a high cetane number, good lubricity, low sulfur content and aromatics which allows it to be used as fuel oil for diesel engines .

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention concerne l'hydrotraitement (HDT) de fractions lourdes de pétrole par utilisation pour ce faire des installations d'hydrotraitement qui sont normalement utilisées dans les raffineries de pétrole. Plus spécifiquement, l'invention concerne le co-traitement de fractions lourdes de pétrole avec des huiles naturelles d'origine organique. Le procédé décrit dans l'invention permet de co-traiter l'huile naturelle d'origine organique ainsi que les dérivés lourds issus du procédé de raffinage, et ultérieurement de récupérer la majeure partie du combustible pour moteurs provenant de l'huile organique hydrotraitée séparément du reste des produits, en utilisant les mêmes équipements pour l'hydrotraitement des fractions lourdes.
PCT/IB2010/002149 2009-12-03 2010-07-23 Procédé d'hydrotraitement de fractions lourdes de pétrole mélangées à de l'huile végétale Ceased WO2011067634A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CO09138358A CO6290087A1 (es) 2009-12-03 2009-12-03 Proceso para hidrotratar fracciones pesadas de petroleo mezcladas con aceite vegetal
CO09-138358 2009-12-03

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Publication Number Publication Date
WO2011067634A2 true WO2011067634A2 (fr) 2011-06-09
WO2011067634A3 WO2011067634A3 (fr) 2011-08-18

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CO (1) CO6290087A1 (fr)
WO (1) WO2011067634A2 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2021119786A1 (fr) 2019-12-20 2021-06-24 Petróleo Brasileiro S.A. - Petrobras Procédé sélectif et catalyseurs pour la production de carburants et de distillats renouvelables à poids moléculaire élevé

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BRPI0500591A (pt) * 2005-02-18 2006-10-03 Petroleo Brasileiro Sa processo para a hidroconversão de óleos vegetais
BRPI0601460B1 (pt) * 2006-04-26 2015-11-10 Petroleo Brasileiro Sa processo para hidroconversão de mistura de óleos orgânicos de diferentes origens
WO2008124607A1 (fr) * 2007-04-06 2008-10-16 Syntroleum Corporation Procédé de coproduction de carburant pour moteur à réaction et de gaz de pétrole liquéfiés à partir de sources renouvelables
FR2935982B1 (fr) * 2008-09-15 2010-12-17 Total France Procede de pretraitement de fcc par hydrocraquage doux incluant une dilution de la charge par une charge d'origine biologique

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2021119786A1 (fr) 2019-12-20 2021-06-24 Petróleo Brasileiro S.A. - Petrobras Procédé sélectif et catalyseurs pour la production de carburants et de distillats renouvelables à poids moléculaire élevé
US11939535B2 (en) 2019-12-20 2024-03-26 Petróleo Brasileiro S.A.—Petrobras Selective process and catalysts for the production of renewable fuels and distillates of high molecular weight

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