WO2007063879A1 - Procede d'hydroraffinage et huile hydroraffinee - Google Patents

Procede d'hydroraffinage et huile hydroraffinee Download PDF

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Publication number
WO2007063879A1
WO2007063879A1 PCT/JP2006/323782 JP2006323782W WO2007063879A1 WO 2007063879 A1 WO2007063879 A1 WO 2007063879A1 JP 2006323782 W JP2006323782 W JP 2006323782W WO 2007063879 A1 WO2007063879 A1 WO 2007063879A1
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Prior art keywords
oil
mass
content
fraction
catalyst
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PCT/JP2006/323782
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English (en)
Japanese (ja)
Inventor
Hideshi Iki
Shinya Takahashi
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Nippon Oil Corporation
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Priority to CN2006800450539A priority Critical patent/CN101321847B/zh
Priority to KR1020087015667A priority patent/KR101301459B1/ko
Publication of WO2007063879A1 publication Critical patent/WO2007063879A1/fr

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    • 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
    • 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
    • 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
    • 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
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
    • 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
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/202—Heteroatoms content, i.e. S, N, O, P
    • 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
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/30—Physical properties of feedstocks or products
    • C10G2300/301—Boiling range
    • 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

  • the present invention relates to a hydrorefining method, and more particularly to a hydrorefining method for oil to be treated containing an oil component derived from animal and vegetable oils.
  • the present invention also relates to a hydrorefined oil produced by the hydrorefining method.
  • biomass energy derived from plants does not lead to an increase in carbon dioxide in the atmosphere from the viewpoint of life cycle because hydrocarbons converted from carbon dioxide by photosynthesis can be used effectively in the growth process of plants. In other words, it has a carbon-eutral nature.
  • Fatty acid methyl ester oil (Fat Acid Methyl Ester) is known as a diesel fuel that uses oil and fat components derived from animal and vegetable oils.
  • Fatty acid methyl ester oil is produced by transesterification with methanol with an alkali or the like for a triglyceride structure, which is a general structure of fat components derived from animal and vegetable oils.
  • Patent Document 1 Japanese Patent Laid-Open No. 2005-154647
  • Oils and fats derived from animal and vegetable oils and fuels produced from these components as diesel In order to use it as a fuel, there are the following problems in addition to the above problems.
  • fat components derived from animal and vegetable oils generally have an oxygen atom in the molecule, there is a concern that this oxygen content may adversely affect engine materials. Moreover, it is generally difficult to remove the oxygen content to a very low concentration.
  • both the oxygen content in the oil and fat components and the sulfur content in the petroleum hydrocarbon fractions are used. could not be reduced sufficiently.
  • the present invention provides hydrogenation in which both oxygen content and sulfur content are sufficiently reduced when oils and fats derived from animal and vegetable oils and oils to be treated containing petroleum hydrocarbon fractions are used. It is an object of the present invention to provide a hydrorefining method capable of refining refined oil economically and extremely effectively. Another object of the present invention is to provide a hydrorefined oil obtained by the hydrorefining method.
  • the hydrorefining method of the present invention comprises a petroleum hydrocarbon fraction containing a fraction having a boiling point of 300 ° C or higher and a sulfur content of 0.5 to 4.5 mass% in the presence of hydrogen. And an oil to be treated containing an oil component of 0.3 to 13% by mass derived from animal and vegetable oils and one or more metals selected from Group 6A and Group 8 elements in the periodic table, And a catalyst containing a porous inorganic oxide containing at least acid-aluminum.
  • deoxygenation activity and desulfurization activity can be stably maintained in hydrorefining.
  • This is a mixture of an oil and fat component derived from animal and vegetable oils containing 0.3 to 13% by mass of oxygen and a petroleum hydrocarbon having the above properties as the oil to be treated.
  • the proportion of the compound having a triglyceride structure in the fat and oil components derived from animal and vegetable oils is preferably 80 mol% or more. This is because the energy required for processing raw materials can be reduced.
  • the petroleum hydrocarbon fraction those containing 400 to 1800 mass ppm of nitrogen are preferred, and those containing 180 to 600 mass ppm of basic nitrogen are preferred. Stable in hydrorefining This is to maintain the deoxygenation activity and desulfurization activity for a long time.
  • the porous inorganic oxide in the present invention preferably contains at least one element selected from silicon, boron, phosphorus, titanium, and zirconium oxide and acid aluminum.
  • the metal selected from Group 6A and Group 8 elements of the periodic table is two or more metals selected from cobalt, molybdenum, nickel, and tungsten force, and the metal is supported on a porous inorganic oxide. I like to do it!
  • the oil to be treated and the catalyst are brought into contact under the conditions of a hydrogen pressure of 5 to 20 MPa and a liquid space speed of 0.1 to 2.2 h " ⁇ hydrogen oil ratio of 300 to 1500 NLZL. Is preferred.
  • the hydrorefined oil of the present invention is produced by the hydrorefining method of the present invention described above.
  • Such hydrorefined oil can be suitably used as, for example, a catalytic cracking feedstock or a hydrocracking feedstock.
  • the gas oil fraction base material of the present invention is a hydrorefined oil according to the present invention, which contains a hydrorefined oil having a boiling point of 260 to 300 ° C. It is preferable that the sulfur content of such a gas oil fraction base material is 15 mass ppm or less and the oxygen content is 0.5 mass% or less.
  • the catalytic cracking feedstock of the present invention contains the hydrorefined oil according to the present invention, and has a sulfur content of 0.1% by mass or less and an oxygen content of 1% by mass or less.
  • the hydrocracking raw material oil of the present invention contains the hydrorefined oil according to the present invention, and has a sulfur content of 0.1% by mass or less and an oxygen content of Is less than 1% by mass.
  • FIG. 1 is a flow diagram showing an example of a hydrorefining apparatus suitable for carrying out the hydrotreating method according to the present invention.
  • FIG. 2 is a flow diagram showing another example of a hydrorefining apparatus suitable for carrying out the hydrorefining method according to the present invention.
  • an oil and fat component derived from animal and vegetable oils containing 0.3 to 13% by mass of oxygen and a sulfur content of 0.5 to 4.5% by mass and having a boiling point of 300 ° C or higher.
  • a mixture of petroleum hydrocarbon fractions containing fractions is used as the oil to be treated.
  • the oil to be treated must be a hydrocarbon containing an oil and fat component derived from animal and vegetable oils.
  • the fat and oil component derived from animals and plants in the present invention is a concept that encompasses not only animal and plant fats and oils that are naturally or artificially produced and manufactured, but also fat and oil components that are produced and manufactured using such animal and plant fats and oils as raw materials.
  • the oil / fat component used in the present invention may be formulated with additives for maintaining and improving the quality or performance of various oil / fat products.
  • Examples of fat components derived from animal and vegetable oils include beef tallow, rapeseed oil, soybean oil, palm oil and the like.
  • any oil and fat may be used as the oil and fat component derived from animal and vegetable oils, and waste oil after using these oils and fats may be used.
  • rapeseed oil, soybean oil, and palm oil are more preferable from the viewpoint of carbon-eutral, from the viewpoint of the number of fatty acid alkyl chain carbons preferred by vegetable oils and their reactivity.
  • the above fats and oils may be used singly or in combination of two or more.
  • Oils and fats derived from animal and vegetable oils generally have a fatty acid triglyceride structure, but may contain other oils and fats processed into esters such as fatty acids and fatty acid methyl esters.
  • esters such as fatty acids and fatty acid methyl esters.
  • diacid-carbon is generated. Therefore, from the viewpoint of reducing the amount of diacid-carbon emissions, ingredients having a triglyceride structure as vegetable fats and oils Is preferred to be the subject.
  • the proportion of the compound having a triglyceride structure in the fat and oil components derived from animal and vegetable oils is preferably 80 mol% or more, more preferably 85 mol% or more, and more preferably 90 mol% or more. More preferably it is.
  • the oil and fat component derived from animal and vegetable oils has an oxygen content of 0. 0 based on the mass of the oil and fat component.
  • the force that is contained by 3 to 13% by mass The content of oxygen is 0.3 to 12% by mass, preferably S, and more preferably 0.5 to 1% by mass. If the oxygen content is less than 0.3% by mass, it becomes difficult to stably maintain the deoxygenation activity and desulfurization activity. On the other hand, if the oxygen content exceeds 13% by mass, the equipment required to treat the by-product water is required. In addition, the interaction between water and the catalyst carrier becomes excessive, reducing the activity and reducing the strength of the catalyst.
  • the oxygen content can be measured with a general elemental analyzer. For example, the sample was converted to monoxide-carbon on platinum carbon, or further converted to diacid-carbon. It can be measured later using a thermal conductivity detector.
  • the petroleum hydrocarbon fraction a fraction obtained in a general petroleum refining process can be used.
  • a fraction corresponding to a predetermined boiling range obtained by an atmospheric distillation apparatus or a vacuum distillation apparatus can be used.
  • a fraction corresponding to a predetermined boiling range obtained from a hydrodesulfurization apparatus, a hydrocracking apparatus, a residual oil direct desulfurization apparatus, a fluid catalytic cracking apparatus, or the like may be used.
  • the fractions obtained from the above apparatus capabilities may be used singly or in combination of two or more.
  • the petroleum hydrocarbon fraction contains at least a fraction having a boiling point of 300 ° C or higher, but preferably contains a heavy fraction having a boiling point exceeding 700 ° C. If the petroleum hydrocarbon fraction does not contain a fraction having a boiling point of 300 ° C or higher, it is difficult to obtain a sufficient yield due to excessive decomposition. On the other hand, if a heavy fraction having a boiling point exceeding 700 ° C is included, carbon deposition in the catalyst is promoted by the heavy components, and the activity tends to decrease.
  • the boiling range in the present invention is a value measured according to the method described in JIS K 2254 “Distillation test method” or ASTM-D86.
  • the petroleum hydrocarbon fraction contains 0.5 to 4.5 mass% of the sulfur content based on the mass of the fraction, and the sulfur content is 1.0 to 3 It is preferably 0% by mass. If the sulfur content is less than 0.5% by mass, the balance between deoxygenation reaction and desulfurization reaction Collapses and excessive hydrogenation increases hydrogen consumption. On the other hand, if the sulfur content exceeds 4.5% by mass, it will be difficult to reduce the sulfur content of the resulting hydrorefined oil to a predetermined level.
  • the sulfur content in the present invention is the mass content of sulfur measured according to the method described in JIS K 2541 “Sulfur content test method” or ASTM-D5453.
  • the amount of nitrogen contained in the petroleum hydrocarbon fraction is preferably within a predetermined range. This is to maintain stable deoxygenation activity and desulfurization activity for a long time.
  • the details of the mechanism that can maintain stable deoxygenation activity and desulfurization activity for a long time when the nitrogen content is within the specified range are unknown, but the interaction of nitrogen content, oxygen content and sulfur content It is assumed that the activity is maintained.
  • the range of the amount of nitrogen contained in petroleum hydrocarbon fractions is preferably 400 to 1800 mass ppm, more preferably 400 to 1200 mass ppm force, more preferably 400 to 800 mass ppm force ⁇ / ,.
  • the content of honey is less than 400 ppm by mass, it tends to be difficult to stably maintain deoxygenation activity and desulfurization activity.
  • the nitrogen content exceeds 1800 ppm by mass, the nitrogen content poisons the active sites of the catalyst, and there is a tendency that sufficient deoxygenation activity and desulfurization activity cannot be obtained.
  • the amount of basic nitrogen contained in the petroleum hydrocarbon fraction is preferably within a predetermined range. This is to maintain stable deoxygenation activity and desulfurization activity for a long time.
  • the range of the basic nitrogen content contained in the petroleum hydrocarbon fraction is preferably 180 to 600 mass ppm force S, more preferably 180 to 500 mass ppm force S, and still more preferably 180 to 400 mass ppm. If the basic nitrogen content is less than 180 mass ppm, the oxidation point on the catalyst is not stabilized, and the deoxygenation activity and desulfurization activity tend to decrease. On the other hand, when the basic nitrogen content exceeds 600 mass ppm, the basic nitrogen content poisons the active sites of the catalyst, and there is a tendency that sufficient deoxygenation activity and desulfurization activity cannot be obtained.
  • the nitrogen content is a value measured according to the method described in JIS K 2609 “Crude oil and petroleum products—Test method for nitrogen content”.
  • the basic nitrogen content can be determined by titration using a perchloric acid acetic acid solution or the like.
  • the basic nitrogen content can be determined in accordance with the method described in UOP 269-70T.
  • the mixing ratio of the oil and fat component derived from the animal and vegetable oil and the petroleum hydrocarbon fraction constituting the oil to be treated is not particularly limited.
  • the mixing ratio is preferably 80% by volume or less, more preferably 60% by volume or less, and still more preferably 40% by volume or less.
  • the mixing ratio of the fat and oil components derived from animal and vegetable oils exceeds 80% by volume, the amount of water produced as a by-product tends to increase and the deoxidation activity and desulfurization activity tend to decrease.
  • the mixing ratio of the fat and oil components derived from animal and vegetable oils to the total volume of the oil to be treated is preferably 1% by volume or more. More preferably, it is 10% or more by volume.
  • the hydrorefining conditions are preferably a hydrogen pressure of 5 to 20 MPa, a liquid space velocity (LHSV) of O. 1 to 2.2 h " ⁇ hydrogen oil ratio (hydrogen Z oil ratio) of 300 to 1500 NLZL. Hydrogen pressure 5.5-18 MPa, space velocity 0.2-2. Hydrocarbon oils ratio 300 ⁇ 1500NL / L in a more Konomashigu hydrogen pressure 6 ⁇ 15MPa, space velocity 0. 3 ⁇ 1. 5h _1, and more preferably a hydrogen oil ratio 350 ⁇ 100 ONLZL. These conditions are factors that influence the reaction activity.For example, when the hydrogen pressure and the hydrogen oil ratio do not satisfy the above lower limit values, the reactivity tends to decrease or the activity tends to decrease rapidly. There is.
  • a fixed bed system can be adopted.
  • hydrogen can adopt either a countercurrent or a cocurrent flow with respect to the oil to be treated.
  • a general type of reactor for example, a gas-liquid co-current type reactor in which oil to be treated and hydrogen flow from top to bottom can be employed.
  • the reactors may be used alone or in combination.
  • a structure in which one reactor is divided into a plurality of catalyst beds may be employed, or a combination of counterflow and cocurrent flow may be employed by using a plurality of reactors.
  • the hydrorefined oil hydrorefined in the reactor is subjected to a gas-liquid separation process, a rectification process, and the like.
  • a hydrorefined oil containing a predetermined fraction For example, hydrorefined hydrorefined oil is fractionated into gas oil fractions and residual fractions, and further fractionated into gas, naphtha fractions, and kerosene fractions as necessary.
  • moisture and hydrogen sulfide may be generated with the reaction of oxygen and sulfur contained in the oil to be treated.
  • gas-liquid separation equipment and other by-product gas removal devices may be installed between the plurality of reactors and product recovery means.
  • Hydrogen gas is generally introduced at the inlet of the first reactor in association with the oil to be treated before or after passing through the heating furnace. Separately, the temperature inside the reactor is controlled. In addition, hydrogen gas may be introduced between the catalyst beds or between the reactors in order to maintain the hydrogen pressure throughout the reactor.
  • the hydrogen introduced in this way is generally called Taenti hydrogen.
  • the ratio of Taenthi hydrogen to the hydrogen gas introduced along with the oil to be treated is preferably 10 to 60% by volume, more preferably 15 to 50% by volume. If the proportion of Taenti hydrogen is less than 10 volumes, the reaction at the subsequent reaction site tends not to proceed sufficiently. If the proportion of Taenti hydrogen exceeds 60% by volume, the reaction near the reactor inlet proceeds sufficiently. There is a tendency not to.
  • the reaction temperature can be arbitrarily set according to the target desulfurization depth.
  • the average temperature of the entire reactor is set to a force generally in the range of 330 to 480 ° C, preferably 350 to 450 ° C, more preferably 360 to 430 ° C. If the average temperature of the entire reactor is less than 330 ° C, the reaction tends not to proceed sufficiently, and if it exceeds 480 ° C, carbon deposition in the catalyst accompanying the polycondensation reaction is promoted and the activity tends to decrease. There is.
  • the active metal of the hydrorefining catalyst is an elemental force of Group 6A and Group 8 of the periodic table. Force that is at least one metal selected from among these elements Among these elements, cobalt, molybdenum, nickel and Tungsten power is preferred to be two or more metals selected. Examples of suitable combinations of these include cobalt molybdenum, nickel molybdenum, nickel-cobalt molybdenum, and nickel tungsten. Of these, the combination of nickel-molybdenum, nickel-cobalt molybdenum and nickel-tungsten is more preferred. In hydrorefining, these metals are converted into sulfides and used.
  • a porous inorganic oxide can be used as a carrier for the hydrotreating catalyst, and in particular, a porous inorganic oxide mainly composed of aluminum oxide is preferably used.
  • the porous inorganic oxide is a complex oxide containing one or more elements selected from the group consisting of silicon, boron, phosphorus, titanium and zirconium as components other than aluminum.
  • the total content of components other than the acid aluminum is preferably 1 to 80% by mass, more preferably 2 to 70% by mass based on the mass of the carrier. If the total content of components other than acid aluminum is less than 1% by mass, the catalyst surface area becomes insufficient and the activity tends to be low.
  • the content is preferably 1 to 8% by mass in terms of oxide, more preferably 2 to 5% by mass.
  • carrier constituents other than aluminum oxide such as silicon, boron, phosphorus, titanium, and zirconium
  • solutions containing these elements can be used as raw materials. That's fine.
  • the key key, water glass, silica sol and the like can be used.
  • boric acid or the like can be used.
  • phosphorus phosphoric acid and alkali metal salts of phosphoric acid can be used.
  • titanium sulphurized titanium, tetrasalt titanium, various alkoxide salts, and the like can be used.
  • zirconium various types of alkoxide salts such as zirconium sulfate can be used.
  • the raw materials of the carrier constituents other than the above aluminum oxide are preferably added in a step prior to the firing of the carrier.
  • the above raw materials are added to a prepared hydroxy sodium aluminum gel which may be prepared from a hydroxyaluminum gel containing these components. May be.
  • the above raw materials may be added in a step of adding water or an acidic aqueous solution to a commercially available aluminum oxide intermediate or basemite powder and kneading. In this case, it is more preferable that aluminum oxide and other carrier constituent materials coexist at the stage of preparing the aluminum hydroxide aluminum gel.
  • carrier constituents other than aluminum oxide Although the mechanism of the effect of carrier constituents other than aluminum oxide has not necessarily been elucidated, it is presumed that it forms a complex oxide state with aluminum, which increases the surface area of the carrier and the active metal. By interacting with It is thought that it affects the activity.
  • the preferred range of the content (supported amount) of the active metal based on the catalyst mass is as follows.
  • the range of the total supported amount of tungsten and molybdenum is preferably 15 to 30% by mass, preferably 12 to 35% by mass in terms of oxide. If the total supported amount of tungsten and molybdenum is less than 12% by mass, the active sites tend to decrease and sufficient activity cannot be obtained. On the other hand, if it exceeds 35% by mass, the metal is not effectively dispersed and sufficient activity tends not to be obtained.
  • the total supported amount ranging from cobalt and nickel, preferably tool 2 to 15 mass from 1.5 to 18 mass 0/0 in terms of the oxide is more preferable.
  • the total supported amount of cobalt and nickel is less than 1.5% by mass, a sufficient promoter effect cannot be obtained, and the activity tends to decrease. On the other hand, if it exceeds 10% by mass, the metal is not effectively dispersed and sufficient activity tends not to be obtained.
  • a method of incorporating these active metals into the catalyst is not particularly limited, and a known method applied when producing a normal desulfurization catalyst can be used.
  • a method of impregnating a catalyst carrier with a solution containing a salt of an active metal is preferably employed.
  • an equilibrium adsorption method, a pore filling method, an incipient-wetness method and the like are preferably employed.
  • the pore filling method is a method in which the pore volume of a support is measured in advance and impregnated with a metal salt solution having the same volume.
  • the impregnation method is not particularly limited, and it can be impregnated by an appropriate method depending on the amount of metal supported and the physical properties of the catalyst carrier.
  • the number of hydrorefining catalysts to be used is not particularly limited.
  • a single type of catalyst may be used alone, or a plurality of catalysts having different active metal species or different carrier components may be used.
  • Suitable combinations in the case of using a plurality of different catalysts include, for example, a catalyst containing cobalt molybdenum after the catalyst containing nickel molybdenum, a catalyst containing nickel cobalt molybdenum after the catalyst containing nickel molybdenum, for example, a catalyst containing nickel cobalt molybdenum is used in the latter stage of the catalyst containing nickel tungsten, and a catalyst containing cobalt molybdenum is used in the rear stage of the catalyst containing nickel cobalt molybdenum.
  • a nickel molybdenum catalyst may be further combined before and Z or after these combinations.
  • a catalyst having an acid-aluminum content of 30% by mass or more and less than 80% by mass based on the total mass of the support is used.
  • a catalyst having an aluminum oxide content in the range of 80 to 99% by mass may be used.
  • a guard is provided for the purpose of trapping the scale that flows in along with the oil to be treated, if necessary, or supporting the hydrorefining catalyst at the separation part of the catalyst bed.
  • Catalysts, metal removal catalysts, and inert fillers may be used. These can be used alone or in combination.
  • the hydrorefined oil produced by the present invention when used as a light oil fraction base, the hydrorefined oil contains a fraction having a boiling point of at least 260 to 300 ° C and contains a sulfur content.
  • the amount of oxygen is 15 mass ppm or less and the oxygen content is 0.5 mass% or less.
  • the preferred sulfur content is 12 mass ppm or less and the oxygen content is 0.3 mass%. More preferred to be, If the sulfur content and oxygen content exceed the above upper limit values, it may affect the filters, catalysts, engines and other materials used in the exhaust gas treatment equipment of diesel engines.
  • the hydrorefined oil described above may be used alone as a diesel light oil or heavy oil base material.
  • Power can be used as a diesel light oil or heavy base material mixed with components such as other base materials.
  • a light oil fraction and Z or kerosene fraction obtained in a general petroleum refining process, and a residual fraction obtained by the hydrorefining method of the present invention can be mixed.
  • synthetic light oil or synthetic kerosene obtained through a Fischer-Tropsch reaction using so-called synthesis gas composed of hydrogen and carbon monoxide as a raw material.
  • These synthetic light oils and kerosene contain few aromatics, are characterized by saturated hydrocarbons as the main component and high cetane number.
  • a known method can be used as a method for producing the synthesis gas, and it is not particularly limited.
  • the residual fraction obtained by the hydrorefining method of the present invention has a sulfur content of 0.1% by mass or less, an oxygen content of 1% by mass or less, and a low sulfur heavy content. It can be used as a substrate.
  • the residual fraction is suitable as a feedstock for catalytic cracking. In this way, a low sulfur level residual fraction is supplied to a catalytic cracking device, thereby reducing the sulfur content.
  • Sorin substrates and other fuel oil substrates can be produced.
  • the residual fraction can be used as a feedstock for hydrocracking. By using these residual fractions in a hydrocracking apparatus, it is possible to improve the cracking activity and achieve high quality of the properties of each fraction of the product oil.
  • FIG. 1 is a flowchart showing an example of a hydrorefining apparatus suitable for carrying out the hydrorefining method of the present invention.
  • the reaction tower 10 of the hydrorefining apparatus 100 shown in FIG. 1 is a fixed bed type reaction tower, in which a hydrotreating catalyst layer 12 is provided.
  • a line L1 for supplying the oil to be treated into the reaction tower 10 is connected to the top of the reaction tower 10, and hydrogen is supplied to the upstream side of the connection with the reaction tower 10 in the line L1.
  • Line L2 for supply is connected.
  • a line L3 for extracting a reaction product from the reaction tower 10 is connected to the bottom of the reaction tower 10, and the other end of the line L3 is connected to an atmospheric distillation device 40.
  • the distillation apparatus 40 is for fractionating the reaction product produced by the reaction in the reaction tower 10 into each fraction having a specific boiling range. For example, it is fractionated into a gas fraction, a naphtha fraction, a kerosene fraction, a light oil fraction and a wax fraction by the distillation apparatus 40.
  • the fractions fractionated in the distillation apparatus 40 are transferred to the subsequent processes by lines (L4 to L8) connected to the distillation apparatus 40, respectively.
  • FIG. 2 is a flowchart showing another example of a hydrorefining apparatus suitable for carrying out the hydrorefining method according to the present invention.
  • a hydrorefining apparatus 200 shown in FIG. 2 includes two reaction towers 20 and 30 connected in series via a transfer line L9 in place of the reaction tower 10 in the hydrorefining apparatus 100. Other than that, it has the same configuration as the hydrorefining apparatus 100.
  • a line L2a for supplying hydrogen is connected to the upstream side of the line L9 connected to the reaction tower 30.
  • the reaction tower 20 includes a hydrotreating catalyst layer 22 therein, and the reaction tower 30 includes a hydrotreating catalyst layer 32 therein.
  • the hydrotreating catalyst constituting the hydrotreating catalyst layer 22 and the hydrotreating catalyst layer 32 may be the same or different from each other. Hydrotreating treatment with these two reaction towers 20, 30 Is implemented.
  • the cake-like slurry was transferred to a container equipped with a reflux condenser, 150 ml of distilled water and 10 g of 27% aqueous ammonia solution were added, and the mixture was heated and stirred at 80 ° C for 24 hours. Thereafter, the slurry was put into a kneading apparatus, heated to 80 ° C. or higher and kneaded while removing moisture, and a clay-like kneaded product was obtained. The obtained kneaded product was extruded into a cylinder having a diameter of 1.5 mm by an extrusion molding machine, dried at 110 ° C. for 1 hour, and then fired at 550 ° C. to obtain a molded carrier.
  • 300 g of water glass No. 3 was added to 3000 g of sodium aluminate aqueous solution with a concentration of 5 mass% in the container, and the temperature of the contents of the container was adjusted to 65 ° C.
  • 3000 g of an aluminum sulfate aqueous solution (concentration 2.5% by mass) was prepared in another container and adjusted so that the temperature of the contents of the container was 65 ° C.
  • the above-mentioned aluminum A solution containing sodium acid and water glass was added dropwise. The end point was when the pH of the mixed solution reached 7.0, and the resulting slurry-like product was filtered through a filter to obtain a cake-like slurry.
  • the cake-like slurry was transferred to a container equipped with a reflux condenser, 150 ml of distilled water and 10 g of 27% aqueous ammonia solution were added, and the mixture was heated and stirred at 80 ° C for 24 hours.
  • the slurry was put in a kneading apparatus, heated to 80 ° C. or higher and kneaded while removing moisture to obtain a clay-like kneaded product.
  • the obtained kneaded product was extruded into a shape of a cylinder having a diameter of 1.5 mm by an extrusion molding machine, dried at 110 ° C. for 1 hour, and then fired at 550 ° C. to obtain a molded carrier.
  • mixed oil 1 a mixed oil obtained by mixing the following palm oil and a Middle Eastern vacuum gas oil fraction in a volume ratio of 20:80 as the oil to be treated is used. Hydrorefining was performed.
  • Palm oil 15 ° C density 0.916gZml, oxygen content 11.4% by mass;
  • Middle-eastern vacuum gas oil fraction 15 ° C density 0.919 gZml, sulfur content 2.41 mass%, nitrogen content 61 0 mass ppm, basic nitrogen content 240 mass ppm, initial boiling point 285 ° C, end point 540 ° C
  • the mixed oil 1 and hydrogen were introduced into the reaction apparatus from the first reaction tube side so that the fluid to be treated passed through the first reaction tube and the second reaction tube in this order.
  • the volume ratio of hydrogen gas introduced between the first reaction pipe and the second reaction pipe (Taenti hydrogen ratio) is 20% by volume of the total hydrogen introduced, and the hydrogen Z oil ratio obtained from the total hydrogen introduced is 430N LZL. It was.
  • the reaction conditions are summarized in Table 2, and the test results are summarized in Table 3.
  • the first reaction tube (inner diameter 20 mm) filled with catalyst A (50 ml) and the second reaction tube (inner diameter 20 mm) filled with catalyst C (50 ml) were attached in series to the fixed bed flow reactor. Then, hydrorefining was carried out in the same manner as in Example 1.
  • the reaction conditions are summarized in Table 2, and the test results are summarized in Table 3.
  • Example 4 The first reaction tube (inner diameter 20 mm) filled with catalyst B (30 ml) and the second reaction tube (inner diameter 20 mm) filled with catalyst C (70 ml) were attached in series to the fixed bed flow reactor. Then, hydrorefining was carried out in the same manner as in Example 1. The reaction conditions are summarized in Table 2, and the test results are summarized in Table 3. [0064] (Example 4)
  • mixed oil 2 in which the palm oil used in Example 1 and the following vacuum gas oil fraction were mixed at a volume ratio of 20:80 was used as the oil to be treated. Hydrorefining was performed in the same manner as in Example 1.
  • the reaction conditions are summarized in Table 2, and the test results are summarized in Table 3.
  • Vacuum oil fraction 15 ° C density 0.910 gZml, sulfur 2.10 mass%, nitrogen 360 mass pp m, basic nitrogen 140 mass ppm, initial boiling point 270 ° C, end point 536 ° C
  • the hydrorefined oil in which both the oxygen content and the sulfur content are sufficiently reduced can be economically used.
  • a hydrorefining method that can be purified extremely effectively is provided.
  • the hydrorefined oil obtained by the said hydrorefining method is provided.

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  • Engineering & Computer Science (AREA)
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  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Catalysts (AREA)

Abstract

L'invention concerne un procédé d'hydroraffinage caractérisé par la mise en contact d'une huile devant être traitée comprenant une fraction d'hydrocarbure de pétrole comportant une fraction dont le point d'ébullition est supérieur ou égal à 300 °C et dont la teneur en soufre est comprise entre 0,5 et 4,5 % en masse et d'une composante de graisse dérivée d'une graisse animale ou végétale et dont la teneur en oxygène est comprise entre 0,3 et 13 % en masse avec un catalyseur comprenant à la fois au moins un métal choisi parmi les éléments des groupes 6A et 8 du tableau périodique et une composante d'oxyde inorganique poreux contenant de l'oxyde d'aluminium en tant que composante essentielle, en présence d'hydrogène.
PCT/JP2006/323782 2005-11-30 2006-11-29 Procede d'hydroraffinage et huile hydroraffinee WO2007063879A1 (fr)

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CN103130600B (zh) * 2011-11-24 2016-01-20 中国石油化工股份有限公司 一种利用动植物油脂及其废弃油生产低碳烯烃的方法
CN103374379B (zh) * 2012-04-29 2015-11-18 中国石油化工股份有限公司 生产优质柴油的加氢方法
CN103374405B (zh) * 2012-04-29 2015-11-18 中国石油化工股份有限公司 一种生物油脂生产优质低凝点柴油的加氢组合方法
CN103374400B (zh) * 2012-04-29 2016-01-06 中国石油化工股份有限公司 加氢法生产优质煤油的组合方法
CN103666519B (zh) * 2012-09-04 2015-09-23 中国石油天然气股份有限公司 非食用动植物油加氢脱氧制备烷烃的方法
CN102989462B (zh) * 2012-10-24 2014-06-04 中国海洋石油总公司 一种高活性油脂加氢催化剂的制法

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