EP3081623B1 - Procédé de production de composants à base d'huile - Google Patents

Procédé de production de composants à base d'huile Download PDF

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Publication number
EP3081623B1
EP3081623B1 EP15163663.6A EP15163663A EP3081623B1 EP 3081623 B1 EP3081623 B1 EP 3081623B1 EP 15163663 A EP15163663 A EP 15163663A EP 3081623 B1 EP3081623 B1 EP 3081623B1
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EP
European Patent Office
Prior art keywords
feedstock
hydrocracking
vgo
wax
dewaxing
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EP15163663.6A
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German (de)
English (en)
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EP3081623A1 (fr
Inventor
Jaana Makkonen
Mika P. Kettunen
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Neste Oyj
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Neste Oyj
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Priority to PL15163663T priority Critical patent/PL3081623T3/pl
Application filed by Neste Oyj filed Critical Neste Oyj
Priority to DK15163663.6T priority patent/DK3081623T3/da
Priority to ES15163663T priority patent/ES2740837T3/es
Priority to EP15163663.6A priority patent/EP3081623B1/fr
Priority to CA2981556A priority patent/CA2981556C/fr
Priority to US15/566,396 priority patent/US20180112140A1/en
Priority to PCT/EP2016/058365 priority patent/WO2016166293A1/fr
Priority to BR112017021764-3A priority patent/BR112017021764B1/pt
Priority to CN201680021515.7A priority patent/CN107532093B/zh
Publication of EP3081623A1 publication Critical patent/EP3081623A1/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
    • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
    • C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
    • C10G65/12—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
    • 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
    • C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
    • 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
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling 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
    • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
    • C10G49/002—Apparatus for fixed bed hydrotreatment processes
    • 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
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
    • C10G67/0454—Solvent desasphalting
    • C10G67/0481—The hydrotreatment being an aromatics saturation
    • 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
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
    • C10G67/0454—Solvent desasphalting
    • C10G67/049—The hydrotreatment being a hydrocracking
    • 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
    • C10G73/00—Recovery or refining of mineral waxes, e.g. montan wax
    • C10G73/02—Recovery of petroleum waxes from hydrocarbon oils; Dewaxing of hydrocarbon oils
    • C10G73/06—Recovery of petroleum waxes from hydrocarbon oils; Dewaxing of hydrocarbon oils with the use of solvents
    • 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
    • C10G2300/1074—Vacuum distillates
    • 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
    • C10G2300/302—Viscosity
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/10—Lubricating oil

Definitions

  • the present invention relates to the field of producing traffic fuels and base oil components. More particularly, the invention relates to a method including hydrocracking and dewaxing of waxy feedstock for producing middle distillate fuel and lubricant base oil.
  • Cracking, and especially hydrocracking, is a well-known process in refinery used for cleaving larger hydrocarbon components into smaller short-chain hydrocarbons which are usable as traffic fuel components. Cracking is achieved by breaking the carbon-carbon bonds in the hydrocarbon chain of C15 to C45 typically in the presence of a cracking catalyst. The nature of the end products is dependent on the nature of the feed and on the process conditions under which the process is carried out, such as temperature, pressure and the nature of the catalyst.
  • a widely used method for carrying out catalytic cracking of high-boiling, high-molecular weight hydrocarbon fractions of petroleum crude oils is a fluid catalytic cracking (FCC) process, in which a powdered catalyst is employed.
  • the catalyst particles are suspended in a rising flow of a heavy gas oil feed to form a fluidized bed.
  • the feed is typically pre-heated and then sprayed into the base of the riser via feed nozzles to bring the feed in contact with the hot fluidized catalyst.
  • the temperature of a FCC cracker is typically between 500°C and 800°C.
  • Hydrocracking of heavy hydrocarbons can also be achieved in a fixed bed hydrocracker.
  • the feedstock is fed downward through the catalyst bed together with hydrogen gas.
  • the catalyst is fixed onto particles, which can be of various sizes and forms providing an even and homogenous distribution of the feedstock and hydrogen gas and, further, maximum contact with the active catalyst.
  • the catalyst containing particles are fixed in layer or bed and the feedstock and hydrogen gas run through the layer.
  • fixed bed reactors typically contain several catalyst layers.
  • VGO vacuum gas oil
  • Hydrocarbon cracking is usually accompanied by a hydrogenation process, also called as hydrotreatment process.
  • the purpose of the hydrogenation is to remove heteroatoms, such as oxygen, sulphur and/or nitrogen, and also to saturate aromatics typically present in the hydrocarbon feed.
  • the hydrogenation process is typically performed before the actual hydrocracking process in order to ensure removal of heteroatoms and saturation of aromatics. In some cases hydrogenation also includes ring-opening functions. However, no substantial cleavage of hydrocarbons takes place in the hydrogenation step.
  • the preceding hydrogenation of the feedstock before hydrocracking ensures good hydrocracking performance and improves the yield of the products produced in the hydrocracking.
  • Waxes and slack waxes is a general term for feedstock comprising mainly paraffins.
  • the paraffins in waxes are typically saturated C15-C45 linear hydrocarbons (normal or n-paraffins). Waxes may also contain to some extent branched (isomerized or i-paraffins) and cyclic hydrocarbons.
  • Slack waxes are typically formed by a solvent dewaxing process of a waxy petroleum feed, such as a VGO stream. The solvent dewaxing process is typically performed by mixing a suitable solvent with the waxy petroleum feed, then cooling the mixture and separating the waxes as solid wax crystals, for example by filtration.
  • Waxes can also be produced by Fischer-Tropsch (F-T) process, in which gas containing carbon monoxide and hydrogen is reacted to form hydrocarbon of various chain lengths.
  • F-T process is widely used in gas-to-liquid (GTL) technologies where natural gas is used as a carbon source.
  • Biomass can also be used as the carbon source in the F-T process and it is then generally called biomass-to-liquid (BTL) technology.
  • Slack wax produced by solvent dewaxing contains varied amounts of impurities which makes the slack wax a low value product.
  • a catalytic dewaxing (cat-dewaxing) unit is a device where hydrocarbon feedstock is catalytically dewaxed, i.e. selectively cracked and isomerized.
  • a cat-dewaxing unit is generally called as VHVI (Very High Viscosity Index) unit, since base oils with very high viscosity index are obtained in said unit.
  • VHVI Very High Viscosity Index
  • linear paraffins are isomerized to form branched paraffins (iso-paraffins). Also, cracking of hydrocarbons takes place to some extent.
  • US 2004/0256287 A1 discloses a process of hydrocracking a waxy hydrocarbon feedstock, such as Fischer-Tropsch waxy hydrocarbons, in the presence of a hydrocracking catalyst.
  • the hydrocracking effluent is hydroisomerized in the presence of a hydroisomerization catalyst.
  • the hydroisomerization effluent is fractioned to provide a heavy fraction and a middle distillate fuel, and the heavy fraction is dewaxed to provide a lubricant base oil having a viscosity index greater than 130.
  • US 2009/0065393 A1 discloses a method for obtaining a petroleum distillate in which a paraffin-based wax such Fischer-Tropsch wax and/or slack wax, is subjected to a cracking process in the presence of a catalyst, followed by hydrogenating the olefinic intermediate obtained in the presence of a catalyst, and recovering the distillate.
  • a paraffin-based wax such Fischer-Tropsch wax and/or slack wax
  • US2007/175794 and US6315891 disclose methods of producing base oils by hydrocraking a feedstock comprising a mixture of VGO and Fischer-Tropsch wax.
  • US8404912 discloses a process of producing base oils by hydrocracking a mixture of VGO and a heavy wax derived from pyrolysis of plastic.
  • middle distillates and very high viscosity index lubricant base oils in high yields from available feasible feeds and yet upgrading the product quality.
  • the middle distillates and base oils desirably have high cetane number and high viscosity index, respectively.
  • the present invention provides a method according to claim 1.
  • Vacuum gas oil is a petroleum based heavy hydrocarbon distillate which is widely used as a feedstock in fluid catalytic crackers to produce a wide range of valuable products for various applications, such as gasoline, diesel fuel and base oil.
  • VGO contains a large quantity of cyclic and aromatic compounds as well as sulphur and nitrogen which impede its conversion to high quality valuable end products.
  • VGO quality influences on the quality of the end products.
  • High quality Group III base oils with high viscosity index can be produced from suitable VGO in good yields. However, further increase of the viscosity index inevitably results in undesired lower yields.
  • a beneficial advantage of the method of the invention is that strict quality requirements of VGO as an adequate feedstock can be bargained when wax is introduced to the feedstock.
  • the adequate quality of the feedstock is adjusted by means of the VGO and wax. This means in practice that lower quality VGO with higher quality wax including a minor amount of impurities, and vice versa, can be used in the method of the invention and still high quality products are produced. This feature allows to employ VGO and waxes in a larger quality range and provides an economic advantage.
  • the method is efficient, simple and economic.
  • the present invention provides a method according to claim 1.
  • slack wax means a crude wax produced by chilling and solvent filter-pressing wax distillate
  • vacuum gas oil (VGO) means a hydrocarbon product obtained from crude oil vacuum distillation
  • Group III Base oil means paraffinic base stock which contains sulphur ⁇ 0.03 wt.%, saturates ⁇ 90 wt.% and has a viscosity index of ⁇ 120.
  • the feedstock suitable for use in the method of the invention typically comprises at most about 0.18 wt.% nitrogen, at most about 2 wt.% sulphur, and about 45 wt.% aromatic compounds.
  • the wax used is slack wax.
  • the slack wax is provided as unpurified slack wax obtained from solvent dewaxing of a waxy petroleum feed.
  • Wax is combined with VGO to provide a feedstock comprising the VGO a major component and the wax as a minor component.
  • the feedstock comprises at most about 30 wt.% wax, the balance being the VGO.
  • the feedstock comprises at most about 25 wt.% wax.
  • the feedstock comprises at most about 20 wt.% wax.
  • the feedstock comprises 1-25 wt.% wax.
  • the feedstock comprises 10-20 wt.% wax.
  • the balance is the VGO.
  • the feedstock comprising wax is subjected to a hydrocracking step.
  • a hydrocracking step heteroatoms such as N and S are removed, larger long-chain hydrocarbons are cleaved into smaller short-chain hydrocarbons and/or some cyclic hydrocarbons are ring-opened to form linear and/or branched hydrocarbons.
  • dearomatization of the aromatic compounds and isomerization of the hydrocracked molecules may also occur to some extent in the process.
  • the cleavage of the hydrocarbons of the wax in the hydrocracking step is not as extensive as that of VGO.
  • the hydrocracking is typically performed in the presence of a hydrocracking catalyst.
  • Hydrocracking catalysts suitable for use in this step are well known to a skilled person in the art.
  • the hydrocracking catalyst may be arranged in one or more layers in a fixed bed.
  • the catalyst may also be arranged in graded catalyst bed.
  • Alternatives for suitable arrangement of the catalyst are well known to a skilled person in the art.
  • the feedstock is first subjected to a hydrotreatment step before the hydrocracking step.
  • the hydrotreatment step is carried out under conditions where any heteroatoms, such as oxygen, sulphur and/or nitrogen present in the feedstock are removed. Also aromatic compounds are typically saturated in this step. No substantial cracking of the hydrocarbons in the feedstock takes place in this step.
  • the hydrotreatment step before hydrocracking ensures good hydrocracking performance and improves the yield of the products produced in the subsequent hydrocracking.
  • the hydrotreatment is typically performed in the presence of a catalyst. Catalysts suitable for use in this step are well known to a skilled person in the art.
  • the catalyst may be arranged in one or more layers in a fixed bed.
  • the catalyst may also be arranged in graded catalyst bed. Alternatives for suitable arrangement of the catalyst are well known to a skilled person in the art.
  • the hydrotreatment and hydrocracking steps can be conducted in a single reactor or separate reactors. When the two steps are conducted in separate reactors, the hydrotreatment reactor is arranged upstream of the hydrocracking reactor.
  • the feed rate of hydrogen per feedstock in the hydrocracking step, optionally including a hydrotreatment step, is about more than 1000 Nm 3 /m 3 .
  • the hydrocracking is typically carried out at a pressure in the range from about 120 to about 170 bar. In an embodiment, the pressure is about 150 bar.
  • the temperature is in the range of about 350°C to about 450°C.
  • VGO and the wax forming a feedstock can be fed to the hydrocracking reactor as separate streams or combined into a single stream which is fed to the reactor.
  • the first effluent obtained from the hydrocracking step is fractionated by distillation whereby at least a bottom fraction and a middle distillate fraction are obtained. Adequate fuel oil quality for the middle distillate fraction is achieved and it is suitable for use as a component in diesel fuel.
  • the bottom fraction is mainly composed of linear paraffins and naphtenes. Fractionation of the first effluent also produces a quantity of light gaseous hydrocarbons.
  • the bottom fraction is subjected to a dewaxing step.
  • waxy n-paraffins are isomerized to provide branched iso-paraffins. Isomerization of hydrocarbons is desired and generally improves the cold flow properties of a base oil.
  • the dewaxing is typically performed in the presence of a dewaxing catalyst. Dewaxing catalysts suitable for use in this step are well known to a skilled person in the art.
  • the dewaxing step provides a second effluent which is fractionated in a distiller to high quality middle distillate and base oil. Also lighter gaseous hydrocarbons are obtained. Group III Base oil having desirably a high viscosity index of >130 and middle distillate with high cetane number and improved cold flow properties are achieved.
  • the middle distillate obtained from the dewaxing step can be used as diesel fuel as such or as a blending component.
  • the present invention can be a batch process or a continuous process.
  • the arrangement for producing oil-based components comprises a hydrocracking reactor A for cracking a waxy feed to provide a first effluent 4, a first distiller B, a dewaxing unit C and a second distiller D.
  • the hydrocracking reactor A comprises at least one inlet for supplying a feedstock into the hydrocracking reactor A and an outlet for discharging the first effluent 4 from the hydrocracking reactor A.
  • the hydrocracking reactor A comprises at least two inlets, one for wax 2 and one for combined hydrogen 1 and VGO 3.
  • the hydrocracking reactor A comprises a catalytic hydrotreatment zone HT and a catalytic hydrocracking zone HC, the hydrotreatment zone lying upstream of the hydrocracking zone.
  • the catalysts in each of the two zones can be arranged in one or more beds. Further, the beds can be graded in respect to the amount of the catalyst employed. A suitable arrangement and grading of the catalyst are well known to a skilled person in the art.
  • the hydrotreatment zone and the hydrocracking zone can be arranged in individual reactors, the hydrotreatment reactor lying upstream of the hydrocracking reactor (not shown in Fig. 1 ).
  • the first distiller B is in a flow connection with the hydrocracking reactor A for fractioning the first effluent 4 to provide at least a bottom fraction HCB and a middle distillate fraction MD.
  • the first distiller B comprises an inlet for supplying the first effluent 4 into the first distiller B and at least one outlet for discharging the bottom fraction HCB and a middle distillate fraction MD.
  • the flow connection between the hydrocracking reactor A and the first distiller B is arranged through a pipe connection between the outlet of the hydrocracking reactor A and the inlet of the first distiller B.
  • the first distiller B is arranged downstream of the hydrocracking reactor A.
  • the dewaxing unit C is in a flow connection with the first distiller B for dewaxing the bottom fraction HCB to provide a second effluent 6.
  • unit C is a solvent dewaxing reactor.
  • the dewaxing unit C comprises an inlet for supplying the bottom fraction HCB into the dewaxing unit C and an outlet for discharging the second effluent 6.
  • the flow connection between the first distiller B and the dewaxing unit C is arranged through a pipe connection between the outlet of the first distiller B discharging the bottom fraction HCB and the inlet of the dewaxing unit C.
  • the dewaxing unit C is arranged downstream of the first distiller B.
  • the second distiller D is in a flow connection with the dewaxing unit C for fractioning the second effluent 6 to provide at least a middle distillate fraction MD and base oil.
  • the second distiller D comprises an inlet for supplying second effluent 6 into the second distiller D and at least one outlet, but preferably two outlets, for discharging the middle distillate MD and base oil.
  • the flow connection between the dewaxing unit C and the second distiller D is arranged through a pipe connection between the outlet of dewaxing unit C and the inlet of the second distiller D.
  • the second distiller D is arranged downstream of the dewaxing unit C and comprises at least one outlet for discharging the middle distillate MD and base oil.
  • the disclosure provides an arrangement for producing oil-based components, the apparatus comprising:
  • Feedstock comprising 20 wt.% slack wax and a balance of VGO was introduced to a hydrocracking reactor comprising a hydrotreatment zone and a hydrocracking zone.
  • the content of sulphur and nitrogen of the feedstock was 1.3 wt.% and 0.079 wt.%, respectively.
  • the viscosity index of the feedstock was 106.
  • the feedstock was introduced to the hydrocracking reactor at a temperature of about 400°C and at a pressure of about 132 bar.
  • the feed of hydrogen per feedstock was 1.1 L/L.
  • the effluent from the hydrocracking reactor was fed to a distiller.
  • a bottom fraction (HCB) and a middle distillate fraction were obtained.
  • the yield of the bottom fraction with 20 wt.% slack wax addition to VGO was increased from 31% to 35% as compared to a VGO feed without slack wax.
  • the cetane number of a middle distillate fraction was increased from 60 (100% VGO) to 64 (80% VGO/20% slack wax).
  • the bottom fraction was solvent dewaxed (SDW) to provide base oil and additional middle distillate.
  • SDW solvent dewaxed
  • Catalytic dewaxing processes are especially developed to improve the cold properties of the base oil products without sacrificing the viscosity index. Therefore, SDW can be used as an indicator of the viscosity index also of the catalytically dewaxed product. SDW is also a generally accepted and used method in the field and correlates well with catalytic dewaxing.
  • Figure 2 shows that the viscosity index of base oil was remarkable higher with 20 wt.% slack wax addition than that of pure VGO feed.
  • Base oil obtained from the solvent dewaxing, having a viscosity index of at least 130 was achieved even with 4 cSt product.
  • Figure 2 further shows that the viscosity index of the base oil is increased by more than about 10 units compared to that of base oil which is prepared from VGO without wax.

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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)
  • Crystallography & Structural Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Claims (5)

  1. Procédé pour produire des composants à base d'huile, comprenant les étapes suivantes :
    - obtention de VGO (gazole sous vide) et de gatsch ;
    - combinaison du VGO en tant que composant majeur et du gatsch en tant que composant mineur pour former une charge ;
    - soumission de la charge à une étape d'hydrocraquage pour former un premier effluent ;
    - fractionnement du premier effluent pour former au moins une fraction de fond et une fraction de distillat moyen ;
    - récupération de la fraction de fond et de la fraction de distillat moyen, dans lequel la charge comprend au plus 30 % en poids de gatsch et le gatsch est fourni sous la forme de gatsch non purifié obtenu à partir d'un déparaffinage au solvant d'une charge de pétrole paraffineux.
  2. Procédé selon la revendication 1, dans lequel
    - la fraction de fond est soumise à une opération de déparaffinage pour former un deuxième effluent ;
    - le deuxième effluent est fractionné pour former au moins un distillat moyen et une huile de base ;
    - le distillat moyen et l'huile de base sont récupérés.
  3. Procédé selon l'une quelconque des revendications précédentes, dans lequel la charge comprend au plus 25 % en poids de gatsch, plus spécifiquement au plus 20 % en poids, encore plus spécifiquement 1 à 25 % en poids, plus spécifiquement encore 10 à 20 % en poids, le reste étant le VGO.
  4. Procédé selon l'une quelconque des revendications précédentes, dans lequel la charge comprend au plus 0,18 % en poids d'azote, au plus 2 % en poids de soufre, et environ 45 % en poids de composés aromatiques.
  5. Procédé selon l'une quelconque des revendications précédentes, dans lequel la charge est soumise à une étape d'hydrotraitement avant l'étape d'hydrocraquage.
EP15163663.6A 2015-04-15 2015-04-15 Procédé de production de composants à base d'huile Active EP3081623B1 (fr)

Priority Applications (9)

Application Number Priority Date Filing Date Title
DK15163663.6T DK3081623T3 (da) 2015-04-15 2015-04-15 En fremgangsmåde til fremstilling af oliebaserede komponenter
ES15163663T ES2740837T3 (es) 2015-04-15 2015-04-15 Un procedimiento para producir componentes a base de aceite
EP15163663.6A EP3081623B1 (fr) 2015-04-15 2015-04-15 Procédé de production de composants à base d'huile
PL15163663T PL3081623T3 (pl) 2015-04-15 2015-04-15 Sposób wytwarzania składników na bazie oleju
CA2981556A CA2981556C (fr) 2015-04-15 2016-04-15 Procede de production de constituants a base d'huile
US15/566,396 US20180112140A1 (en) 2015-04-15 2016-04-15 Method for producing oil-based components
PCT/EP2016/058365 WO2016166293A1 (fr) 2015-04-15 2016-04-15 Procédé de production de constituants à base d'huile
BR112017021764-3A BR112017021764B1 (pt) 2015-04-15 2016-04-15 método para produção de componentes baseados em óleo
CN201680021515.7A CN107532093B (zh) 2015-04-15 2016-04-15 用于生产油基组分的方法

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP15163663.6A EP3081623B1 (fr) 2015-04-15 2015-04-15 Procédé de production de composants à base d'huile

Publications (2)

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EP3081623A1 EP3081623A1 (fr) 2016-10-19
EP3081623B1 true EP3081623B1 (fr) 2019-06-12

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EP (1) EP3081623B1 (fr)
CN (1) CN107532093B (fr)
BR (1) BR112017021764B1 (fr)
CA (1) CA2981556C (fr)
DK (1) DK3081623T3 (fr)
ES (1) ES2740837T3 (fr)
PL (1) PL3081623T3 (fr)
WO (1) WO2016166293A1 (fr)

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RU2694054C1 (ru) * 2018-08-22 2019-07-09 Общество с ограниченной ответственностью "ЛУКОЙЛ-Волгограднефтепереработка" (ООО "ЛУКОЙЛ-Волгограднефтепереработка") Способ получения компонентов базовых масел
FI130086B (en) 2021-07-19 2023-01-31 Neste Oyj Procedure for treating plastic waste

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ZA989528B (en) * 1997-12-03 2000-04-19 Schuemann Sasol S A Pty Ltd "Production of lubricant base oils".
US20040245147A1 (en) * 2003-06-06 2004-12-09 Boucher Ashe Heather A. Process to manufacture high viscosity hydrocracked base oils
US20040256287A1 (en) 2003-06-19 2004-12-23 Miller Stephen J. Fuels and lubricants using layered bed catalysts in hydrotreating waxy feeds, including fischer-tropsch wax, plus solvent dewaxing
CN1926220A (zh) * 2004-03-02 2007-03-07 国际壳牌研究有限公司 连续制备两种或多种基础油级分和中间馏分的方法
US20070278134A1 (en) * 2006-06-01 2007-12-06 Chevron U.S.A. Inc. Process for producing light neutral base oil having a high viscosity index
US20090065393A1 (en) 2007-09-07 2009-03-12 Uop, Llc Fluid catalytic cracking and hydrotreating processes for fabricating diesel fuel from waxes
US8404912B1 (en) * 2012-05-09 2013-03-26 Chevron U.S.A. Inc. Process for making high VI lubricating oils
US20140042056A1 (en) * 2012-08-10 2014-02-13 Exxonmobil Research And Engineering Company Co-production of heavy and light base oils
WO2014125683A1 (fr) * 2013-02-13 2014-08-21 Ｊｘ日鉱日石エネルギー株式会社 Procédé pour la production d'huile de base pour des huiles de graissage

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* Cited by examiner, † Cited by third party
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Publication number Publication date
BR112017021764B1 (pt) 2021-05-04
ES2740837T3 (es) 2020-02-06
US20180112140A1 (en) 2018-04-26
WO2016166293A1 (fr) 2016-10-20
CA2981556A1 (fr) 2016-10-20
PL3081623T3 (pl) 2019-12-31
CN107532093B (zh) 2020-08-25
CN107532093A (zh) 2018-01-02
CA2981556C (fr) 2020-09-29
EP3081623A1 (fr) 2016-10-19
BR112017021764A2 (pt) 2018-07-10
DK3081623T3 (da) 2019-08-12

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