• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    Process for the manufacture of lubricating base oils (8A, 8B, 8C, 8D) wherein a hydrocarbon feedstock is catalytically treated (10) in the presence of hydrogen at elevated temperature and pressure and wherein at least part of a heavy fraction of the material obtained is subjected to dewaxing (20), in which process a hydrocarbon feedstock is used containing flashed distillate (16) produced via a residue conversion process (50).
    公开号:SU1676456A3
    申请号:SU874203841
    申请日:1987-12-09
    公开日:1991-09-07
    发明作者:Йоханнес Антониус Ван Хелден Херникус；Фабрициус Нильс；Майкл Джозеф Бийвард Хенрикус
    申请人:Шелл Интернэшнл Рисерч Маатсхаппий Б.В. (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to a process for the preparation of lubricating oils and can be used in the petroleum refining industry.
    A method of producing lubricating oils is known using dewaxing and / or processing processes 1.
    A known method for producing lubricating oils using catalytic solvent dewaxing and hydroprocessing processes 2.
    Closer to the invention is a method for producing lubricating oils by catalytic cracking in the presence of hydrogen at elevated temperature and pressure 3. The raw material used is distillate separated from the product of catalytic hydroconversion of oil residue. The hydroconversion product is subjected to
    distillation The heavy fraction of the hydrocracked product is subjected to dewaxing to obtain the desired products.
    A disadvantage of the process is the need to cool and reheat the catalytic cracking feed in the presence of hydrogen.
    The aim of the invention is to simplify the process technology.
    The drawing is a schematic diagram of the process.
    This goal is achieved by the described method of obtaining lubricating oils by catalytic hydrocracking in the presence of hydrogen at elevated temperatures and distillate pressure in the vapor phase of a single equilibrium distillation under vacuum of a catalytic hydroconversion product
    Nj o
    1 ± SL O

    with
    residue, boiling off at 320–600 ° C, or the indicated distillate and distillate in the vapor phase of a single equilibrium distillation under vacuum of the atmospheric oil residue.
    Preferably, the feedstock contains 10-50 wt.% Distillate in the vapor phase of a single equilibrium distillation under vacuum of a product of catalytic hydroconversion of oil residue boiling in the range of 320-600 ° C.
    When fractionating a hydrocracking product, kerosene and / or gas oil fractions will be obtained.
    Distinctive features of the method are the use of catalytic cracking in the presence of distillate hydrogen in the vapor phase of a single equilibrium distillation under vacuum of a catalytic hydroconversion product of oil residue boiling at 320–600 ° C, or the above distillate and distillate in the vapor phase of a single equilibrium distillation under vacuum of an atmospheric oil residue.
    In addition, the distinctive features are the use of the feedstock containing 10-50 wt.% Distillate in the vapor phase of a single equilibrium distillation under vacuum of the product of catalytic hydroconversion of oil residue boiling in the temperature range 320-600 ° C, as well as in the possibility of in the fractionation of the product of hydrocracking of kerosene and / or gas-oil fractions.
    The vacuum residue is fed through line 1, possibly after mixing with the recycled distillation residue via line 2, sent via line 3 to the unit and catalytic hydroconversion of the residue. The resulting product is fed via line 5 to the distillation unit 6. A gas oil fraction withdrawn through line 7 is obtained, and the distillate is vaporized in the vapor phase of a single flash distillation under vacuum (hereinafter the distillate). The latter is sent to the hydrocracking unit 8 via line 9, and the distillation residue is withdrawn through line 10, which can be partially recycled through line 11 to the catalytic hydroconversion unit residue or removed from the unit via line 12. Distillate fed through E-lines can be mixed with a distillate in the vapor phase of a single equilibrium distillation under vacuum of an atmospheric oil residue (not shown), as well as with a recirculated distillation residue fed through lines 13 and 14.
    The mixture through line 15 is directed to the unit 8, the resulting product is directed through line 16 to the distillation unit 17 and a kerosene fraction is obtained, discharged through
    line 18, gas oil fraction discharged through line 19, heavy gas oil fraction (boiling at 320-390 ° C), discharging through line 20, and distillation residue, which can be partially recycled through line 13, to a hydrocracking unit 15, and a portion of which, via line 21, is directed to a catalytic dewaxing unit 22. Part of the fraction (320-390 ° C) can be removed from the process through line 23, the rest or
    5, the entire fraction is directed via line 24 to a catalytic or solvent dewaxing unit 23. The product obtained (possibly after the distillation of gaseous substances) is directed along line 25 to a distillation unit 26 and various fractions of lubricant starting oils are obtained, discharged along lines 27-30.
    The catalytic hydroconversion is carried out at 300–500 ° C (preferably at 3505–450 ° C), a pressure of 50-300 rem (preferably 75-200 bar), a space velocity of 0.02-10 kg / kg-h (preferably 0.1-2 kg / kg-h) and the ratio of hydrogen / raw materials 100-5000 l / kg (preferably 500-2000 l / kg).
    0 Use catalysts containing
    at least one metal selected from the group formed by nickel and cobalt, and one metal selected from the group formed by molybdenum and tungsten,
    5 on the carrier, and the carrier contains a significant amount of alumina, for example, at least 40 wt.%. Hydrocracking is carried out at 250-500 ° C, pressures up to 300 bar and a space velocity of 0.1-10 kg / l-h.
    0 The hydrogen / gas ratio can be used in the range of 100-500 l / kg. Preferably, the process is carried out at 300-450 ° C, a pressure of 25-200 bar and a space velocity of 0.2-5 kg / l-h, the ratio of hydrogen-containing gas / feedstock 250-2000 l / kg.
    The known amorphous hydrocracking catalysts are used, as well as zeolite-based hydrocracking catalysts.
    0
    Synthetic zeolite Y and its modifications are used, such as various forms of ultra-stable zeolite Y. Preference is given to using catalysts.
    5 hydrocracking based on modified zeolite Y, where the zeolite used contains a significant amount of pores with a diameter of less than 8 nm, hydrocracking zeolite catalysts may also contain other active ingredients, such as aluminosilicates, as well as binding materials such as alumina.
    Hydrocracking catalysts contain at least one hydrogenation component from a metal of group IV and / or at least one hydrogenation component from a metal of group VIII. Catalytic compositions can include one or more components of nickel and / or cobalt, one or more components of molybdenum and / or tungsten, or one or more components of platinum and / or palladium.
    The catalytic composition contains, as a rule, 0.05-10 wt.% Metal components of group VIII and May. % of metal components of group VI, j calculated on 100 weight.h. catalyst. The hydrogenation components in the catalyst compositions may be in oxide and / or sulphide form. If the catalyst used contains a metal component of groups VI and VIII in the form of oxide, it must be sulfided before being used in hydrocracking.
    At the stage of dewaxing, both solvent and catalytic dewaxing are used (the latter is preferable). Catalytic dewaxing is carried out by contacting the fraction with a catalyst in the presence of hydrogen. Used catalysts containing crystalline aluminosilicates, such as ZSM-5, ZSM-8, ZSM-11, ZSM-23 and ZSM-35. Commonly used catalysts contain metals of the VI and / or VIII groups.
    Catalytic dewaxing is carried out at 250-500 ° C. hydrogen pressure 5-200 bar, flow rate of 0.1-5 kg / l-h and the ratio of hydrogen / raw materials 100-2500 l / kg. Preferably, the catalytic dewaxing is carried out at 275-450 ° C. hydrogen pressure 10-110 bar, volumetric rate of 0.2-3 kg / lh and the ratio of hydrogen / raw materials 200-2000 l / kg.
    Example 1. 100 weight.h. A vacuum residue of Middle Eastern origin is directed along lines 1 and 3 to a catalytic hydroconversion residue 4 installation. When this is used, the catalyst is molybdenum on silica. The hydroconversion is carried out at 435 ° C and a partial pressure of hydrogen of 150 bar. The consumption of hydrogen is 3.2 parts by weight, the volumetric feed rate of the raw material is 0.45 kg / kg-h. Obtained by catalytic hydroconversion residue product is fed through line 5 to the installation 6 distillation. At the same time get 4.7 mach. hydrogen sulphide and ammonia, 7.0 wt.h. gaseous products boiling below the boiling range
    ligroina, 8.3 ma.ch. ligroina, 18.8 ma.ch. kerosene, 30.9 mach. gas oil discharged through line 7. and 33.7 ma.h. bottom fraction. which is subjected to vacuum distillation and
    get 26.7 ma.ch. distillate in the vapor phase of a single equilibrium distillation under vacuum, discharged along line 9, and 6.0 wt.h. vacuum residue discharged along lines 10 and 12. Distil t discharged along
    0 line 9, with a density of (15/4) 0.89, contains, wt%: 12.2 hydrogen, 0.5 sulfur, 0.12 nitrogen, the content of coke residue according to Conradson “0.5 wt.%. and an average boiling point of 445 ° C. The last on line 15 is directed to
    5 a catalytic hydroprocessing unit 8 containing a nickel / tungsten based catalyst on alumina. The catalytic hydroprocessing was carried out at 405 ° C, a hydrogen partial pressure of 130 bar and a volume rate of 0.84 kg / kg.h.
    The resulting product is fed to; b is sent to an atmospheric distillation unit 17. At the same time receive 0.2 ma. hydrogen sulfide, and 1.0 ma.ch. ammonia fraction. boiling down naphtha, 4.3 mache.ch. ligroina, 8.3 ma.ch. kerosene, discharged through the line 18. 6,3 ma.ch. gas oil discharged through line 19 and 7.3 ma.ch. residue, which is sent via line 21 to the installation of 22 DPA-refineries. In catalytic dewaxing, a composite crystalline aluminosilicate dewaxing catalyst containing palladium is used. This catalytic dewaxing is carried out at 355 ° C. hydrogen partial pressure of 40 bar and a space velocity of 1.0 kg / kg.h. Raw dewaxing contains 22 wt.% Paraffin. The dewaxing product is directed along line 25 to
    0 installation 26 distillation and receive a total of 5.2 mache.h. lubricating oils, which include 30.8 wt.% neutrol 80, 26.9 wt.% neutrol 125, 23.1 wt.% neutrol 250 and 19.2 wt.% neutrol 5SO.
    The method is carried out analogously to example 1, using catalyst A: nickel and vanadium on silica, catalyst B: nickel and molybdenum on alumina, catalyst C: molybdenum on silicon dioxide, catalyst D: nickel / tungsten on alumina / zeolite Y.
    In the process of catalytic hydroconversion of an oil residue at 400 ° C, a partial hydrogen pressure of 100 bar, a space velocity of 0.2 kg / kg-h using catalyst A containing nickel and vanadium on silica, the resulting product contains 2.8 wt. % hydrogen sulfide and ammonia, 1.8 wt.% gaseous
    products boiling at a temperature lower than ligroy. 3.7% by weight of naphtha, 5.6% by weight of kerosene, 12.0% by weight of gas oil, 17.6% by weight of distillate and 56.5% by weight of the residue.
    With catalytic hydraulic conversion of the residue (boiling away at temperatures above 520 ° C) at 460 ° C, volumetric rate of 2 kg / kg-h, partial pressure of hydrogen of 250 bar, gas / feedstock ratio 3000 nl / kg using catalyst C, the resulting product contains 5.0 wt.% hydrogen sulphide and ammonia, 4.3 wt.% gaseous products boiling at a temperature below the naphtha, 6.6 wt.% ligroin, 9.6 wt.% kerosene, 18.5 wt.% gas oil , 21.5 wt.% Distillate and 34.5 wt.% Vacuum residue.
    In the hydrocracking process, the distillate used as a feedstock in the vapor phase of a single equilibrium distillation under vacuum of an oil atmospheric residue (distillate 1) with a density of (15/4) 0.94 contains 97.3 wt.% Fraction boiling at a temperature of 370 ° C. 19.7 wt.% Fraction boiling at a temperature above 540 ° C. coking with Conradson 0.9 wt.%. The distillate used in the vapor phase of single-stage equilibrium distillation under vacuum of the product of catalytic hydroconversion of oil residue (distillate 2) with a density of (15/4) 0.92, contains 86.5% by weight of the fraction boiling at a temperature above 370 ° C, 3.2 wt.% Fraction boiling at temperatures above 540 ° C. coking ability according to Conradson 0.3 wt.%. When hydrocracking a mixture containing 90 wt.% Distillate
    1 and 10 may% of distillate 2 (first option), using a catalyst B 455 ° С, gas velocity 750 nl / kg. a hydrogen pressure of 195 bar and a volumetric rate of 1.95 kg / kg h receive a product containing 2.7 wt.% hydrogen sulfide and ammonia, 21.9 wt.% of the fraction boiling at a temperature below 165 ° C, 46.5 wt.% of the fraction, boiling at a temperature of 165-370 ° C and 28.9 wt.% fraction, boiling at a temperature above 370 ° C.
    With hydrocracking of a mixture containing 50 wt.% Distillate 1 and 50 wt.% Distillate
    2 (second variant), in the presence of a fixed bed containing catalyst B and cadalizer D, at 406 ° C, a gas velocity of 3000 nl / kg and a space feed rate of 0.47 kg / kg-h, a product containing 2.2 wt. .% hydrogen sulfide and ammonia, 39.0 wt.% fraction boiling at a temperature below 165 ° C, 34.4 wt.% fraction boiling at a temperature of 165-370 ° C and 24.4 wt.% product, bale at a temperature above 370 ° С,
    The process of catalytic dewaxing (the first variant of catalytic hydrodewaxing) is carried out using a crystalline aluminosilicate catalyst composition containing palladium. Catalytic dewaxing
    carried out at 370 ° C, a hydrogen partial pressure of 135 bar and a gas velocity of 700 nl / kg. Raw dewaxing boils at temperatures above 370 ° C and contains 24 wt.% Paraffin. The resulting product is subjected
    0 Distillation yielding 24.7 May. % gaseous product, 11.4 wt.% product boiling at temperatures below 370 ° C and 63.9 wt.% lubricating oil of high quality.
    Catalytic hydrodeparaffinization (the second option) is carried out using a crystalline aluminosilicate dewaxing catalyst containing palladium. The dewaxing feedstock has an average boiling point of 426 ° C. Catalytic dewaxing was carried out at 330 ° C, 37 bar hydrogen partial pressure and 700 nl / kg gas velocity. The resulting product is subjected to distillation to obtain 72.4% by weight of lubricating oil having a yield point tem perature of –1 ° C and a viscosity of 4.7 eaten at 100 ° C.
     In solvent dewaxing, a mixture of solvents is used with a weight ratio of the feedstock and solvent mixture of 1: 3. The mixture of solvents consists of toluene and methyl ethyl ketone with a weight ratio of 2: 3. The mixture is cooled to -20 ° C and filtered to separate the wax crystals. Then the solvent is distilled off. The dewaxed lubricating oil obtained has a pour point of -10 ° C. The yield is 75.6% by weight of the feedstock. The content of paraffin oil in the resulting
    The wax content is 10% by weight.
    Thus, the proposed method allows to simplify the process flow diagram.
    权利要求:
    Claims (2)
    [1]
    Invention Formula
    5 1. A method of producing lubricating oils by catalytic hydrocracking in the presence of hydrogen at elevated temperature and pressure of the distillate isolated from the product of catalytic hydroconversion
    0 oil residue, followed by dewaxing the heavy fraction of the hydrocracking product to produce the desired oils, characterized in that. that, in order to simplify the process technology, as an initial
    5, a distillate is used in the vapor phase of a single flash distillation of the product of catalytic hydroconversion of an oil residue boiling at 320-600 ° C, or this distillate is distilled and distilled in a vapor phase of a single equilibrium distillation of an oil oil residue.
    [2]
    2. A method according to claim 1, characterized in that the feedstock contains 10-50 wt.% Distillate in the vapor phase of a single equilibrium distillation under vacuum of a catalytic hydroconversion product.
    oil residue boiling over an interval of 320 to 600 ° C
    3 The method according to claim 1. characterized in that the fractionation of a hydrocracking product produces a kerosene and / or gas oil fraction. .
    类似技术:
    公开号 | 公开日 | 专利标题
    SU1676456A3|1991-09-07|Method of producing lubricating oils
    CA2230760C|2004-07-20|Integrated lubricant upgrading process
    US6337010B1|2002-01-08|Process scheme for producing lubricating base oil with low pressure dewaxing and high pressure hydrofinishing
    US4062758A|1977-12-13|Process for the conversion of hydrocarbons in atmospheric crude residue
    US3923636A|1975-12-02|Production of lubricating oils
    US4126538A|1978-11-21|Process for the conversion of hydrocarbons
    AU2002249845B2|2006-05-04|Integrated lubricant upgrading process
    US5358627A|1994-10-25|Hydroprocessing for producing lubricating oil base stocks
    CA1119986A|1982-03-16|Process for preparing hydrocarbons
    JP2002527530A|2002-08-27|Isoparaffinic base oil produced by dewaxing Fischer-Tropsch wax hydroisomerized oil with Pt / H-mordenite
    PL202663B1|2009-07-31|Process for the production of high quality base oils
    EP0016530B1|1986-12-30|Catalytic dewaxing of hydrocarbon oils with synthetic offretite
    US20040245147A1|2004-12-09|Process to manufacture high viscosity hydrocracked base oils
    KR20010099637A|2001-11-09|Premium synthetic lubricant base stock
    US4165274A|1979-08-21|Process for the preparation of synthetic crude oil
    RU2674703C2|2018-12-12|Process for preparing hydrowax
    EA000717B1|2000-02-28|Process for the preparation of lubricating base oils
    US7727379B2|2010-06-01|Process to continuously prepare two or more base oil grades and middle distillates
    EP1581602A1|2005-10-05|Process for the preparation of a lubricant
    EP1720959B1|2008-06-04|Process to prepare a lubricating base oil
    US3929617A|1975-12-30|Hydrocracking extraction process for lubes
    US5143595A|1992-09-01|Preparation of oxidation-stable and low-temperature-stable base oils and middle distillates
    US4608151A|1986-08-26|Process for producing high quality, high molecular weight microcrystalline wax derived from undewaxed bright stock
    US5098551A|1992-03-24|Process for the manufacture of lubricating base oils
    US3790470A|1974-02-05|Production of lubricating oils
    同族专利:
    公开号 | 公开日
    JPS63161073A|1988-07-04|
    DK643187D0|1987-12-08|
    AR246551A1|1994-08-31|
    MX172340B|1993-12-14|
    GB8629476D0|1987-01-21|
    NO875134L|1988-06-13|
    FI91082C|1994-05-10|
    CN87107355A|1988-06-22|
    GR3001032T3|1992-01-20|
    EP0272729A1|1988-06-29|
    AU8200087A|1988-06-16|
    CA1293945C|1992-01-07|
    DE3765097D1|1990-10-25|
    IN170406B|1992-03-21|
    DK643187A|1988-06-11|
    FI875414A|1988-06-11|
    NO174427B|1994-01-23|
    KR880007693A|1988-08-29|
    ZA879012B|1988-05-27|
    ES2018009B3|1991-03-16|
    FI91082B|1994-01-31|
    FI875414A0|1987-12-09|
    KR960014921B1|1996-10-21|
    EP0272729B1|1990-09-19|
    CN1016181B|1992-04-08|
    NO875134D0|1987-12-09|
    AU598884B2|1990-07-05|
    US5122257A|1992-06-16|
    BR8706677A|1988-07-19|
    AT56742T|1990-10-15|
    NO174427C|1994-05-04|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    RU2674703C2|2012-12-17|2018-12-12|Шелл Интернэшнл Рисерч Маатсхаппий Б.В.|Process for preparing hydrowax|US3530062A|1967-05-19|1970-09-22|Universal Oil Prod Co|Catalytic conversion of hydrocarbon mixtures containing asphaltenes|
    BE754805A|1969-09-05|1971-02-15|Atlantic Richfield Co|PERFECTED PROCESS FOR PREPARATION OF LUBRICATING MINERAL OIL FROM NEW RAW MATERIALS|
    US3876522A|1972-06-15|1975-04-08|Ian D Campbell|Process for the preparation of lubricating oils|
    US3907667A|1973-08-22|1975-09-23|Gulf Research Development Co|Process for producing a lubricating oil from a residue feed|
    NL7510465A|1975-09-05|1977-03-08|Shell Int Research|PROCESS FOR CONVERTING HYDROCARBONS.|
    US4437975A|1977-07-20|1984-03-20|Mobil Oil Corporation|Manufacture of lube base stock oil|
    US4238316A|1978-07-06|1980-12-09|Atlantic Richfield Company|Two-stage catalytic process to produce lubricating oils|
    US4283271A|1980-06-12|1981-08-11|Mobil Oil Corporation|Manufacture of hydrocracked low pour lubricating oils|
    US4347121A|1980-10-09|1982-08-31|Chevron Research Company|Production of lubricating oils|
    US4414097A|1982-04-19|1983-11-08|Mobil Oil Corporation|Catalytic process for manufacture of low pour lubricating oils|US5714140A|1989-12-13|1998-02-03|Otsuka Pharmaceutical Co., Ltd.|Method for inhibiting the production of bioactive IL-1 by administering M-CSF|
    KR960013606B1|1993-05-17|1996-10-09|주식회사 유공|Preparation of lubricating base oil by use of unconverted oil|
    EP0697455B1|1994-07-22|2001-09-19|Shell Internationale Research Maatschappij B.V.|Process for producing a hydrowax|
    EP0712922B1|1994-11-16|2000-02-23|Shell Internationale Researchmaatschappij B.V.|Process for improving lubricating base oil quality|
    AU688610B2|1994-11-16|1998-03-12|Shell Internationale Research Maatschappij B.V.|Process for improving lubricating base oil quality|
    US6569313B1|1995-12-22|2003-05-27|Exxonmobil Research And Engineering Company|Integrated lubricant upgrading process|
    US5935416A|1996-06-28|1999-08-10|Exxon Research And Engineering Co.|Raffinate hydroconversion process|
    US6517704B1|1998-09-29|2003-02-11|Exxonmobil Research And Engineering Company|Integrated lubricant upgrading process|
    US6569312B1|1998-09-29|2003-05-27|Exxonmobil Research And Engineering Company|Integrated lubricant upgrading process|
    CN1296462C|2003-01-30|2007-01-24|中国石油化工股份有限公司|Auxiliary test device for solvent dewaxing|
    JP2007517969A|2004-01-16|2007-07-05|シントロリウムコーポレイション|Synthetic fuel and lubricant manufacturing processes|
    KR20060130675A|2004-03-02|2006-12-19|쉘 인터내셔날 리써취 마트샤피지 비.브이.|Process to continuously prepare two or more base oil grades and middle distillates|
    US7727379B2|2004-03-02|2010-06-01|Shell Oil Company|Process to continuously prepare two or more base oil grades and middle distillates|
    KR100841805B1|2007-07-26|2008-06-26|에스케이에너지 주식회사|Method for producing feedstocks of high quality lube base oil from coking gas oil|
    WO2011068666A1|2009-12-01|2011-06-09|Exxonmobil Research And Engineering Company|Two stage hydroprocessing with divided wall column fractionator|
    JP5787484B2|2010-02-25|2015-09-30|出光興産株式会社|Lubricating oil composition|
    WO2013012661A1|2011-07-20|2013-01-24|Exxonmobil Research And Engineering Company|Production of lubricating oil basestocks|
    US20140042056A1|2012-08-10|2014-02-13|Exxonmobil Research And Engineering Company|Co-production of heavy and light base oils|
    CA3009742A1|2015-12-28|2017-07-06|Exxonmobil Research And Engineering Company|Lubricant base stock production from disadvantaged feeds|
    CN107603720A|2017-09-04|2018-01-19|吴江华威特种油有限公司|A kind of antirust injection machine lubricating oil preparation method|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    GB868629476A|GB8629476D0|1986-12-10|1986-12-10|Manufacture of lubricating base oils|
    [返回顶部]