EP2992070A2 - Procédé de préparation d'une huile de base lourde - Google Patents
Procédé de préparation d'une huile de base lourdeInfo
- Publication number
- EP2992070A2 EP2992070A2 EP14720073.7A EP14720073A EP2992070A2 EP 2992070 A2 EP2992070 A2 EP 2992070A2 EP 14720073 A EP14720073 A EP 14720073A EP 2992070 A2 EP2992070 A2 EP 2992070A2
- Authority
- EP
- European Patent Office
- Prior art keywords
- range
- catalyst
- process according
- hydrofinishing
- dewaxing
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn
Links
- 239000002199 base oil Substances 0.000 title claims abstract description 62
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 16
- 239000003054 catalyst Substances 0.000 claims abstract description 79
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 46
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims abstract description 34
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 25
- 239000005864 Sulphur Substances 0.000 claims abstract description 23
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 23
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 22
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 22
- 239000010457 zeolite Substances 0.000 claims abstract description 22
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 19
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims abstract description 17
- 239000007789 gas Substances 0.000 claims abstract description 17
- 229910000323 aluminium silicate Inorganic materials 0.000 claims abstract description 15
- 230000003197 catalytic effect Effects 0.000 claims abstract description 13
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 13
- 229910052751 metal Inorganic materials 0.000 claims abstract description 13
- 239000002184 metal Substances 0.000 claims abstract description 13
- 238000009835 boiling Methods 0.000 claims abstract description 11
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 9
- 239000011230 binding agent Substances 0.000 claims abstract description 9
- 239000001257 hydrogen Substances 0.000 claims abstract description 9
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 9
- 239000000463 material Substances 0.000 claims abstract description 4
- 238000000034 method Methods 0.000 claims description 36
- 239000010953 base metal Substances 0.000 claims description 4
- 239000000047 product Substances 0.000 description 39
- 230000001050 lubricating effect Effects 0.000 description 15
- 239000003921 oil Substances 0.000 description 14
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 14
- 150000001875 compounds Chemical class 0.000 description 12
- 239000002904 solvent Substances 0.000 description 12
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 11
- 239000004215 Carbon black (E152) Substances 0.000 description 9
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 9
- 229910000510 noble metal Inorganic materials 0.000 description 9
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 7
- 229910052697 platinum Inorganic materials 0.000 description 7
- 239000000203 mixture Substances 0.000 description 6
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 6
- 239000011148 porous material Substances 0.000 description 6
- 238000004821 distillation Methods 0.000 description 5
- 229910052763 palladium Inorganic materials 0.000 description 5
- 150000003839 salts Chemical class 0.000 description 5
- 229910003294 NiMo Inorganic materials 0.000 description 4
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- 239000012263 liquid product Substances 0.000 description 4
- 229910052759 nickel Inorganic materials 0.000 description 4
- 230000000737 periodic effect Effects 0.000 description 4
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 4
- 239000010941 cobalt Substances 0.000 description 3
- 229910017052 cobalt Inorganic materials 0.000 description 3
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 229940104869 fluorosilicate Drugs 0.000 description 3
- 238000005342 ion exchange Methods 0.000 description 3
- 239000000314 lubricant Substances 0.000 description 3
- 201000011540 mitochondrial DNA depletion syndrome 4a Diseases 0.000 description 3
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 3
- 239000000377 silicon dioxide Substances 0.000 description 3
- 239000001993 wax Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 2
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 description 2
- 239000011959 amorphous silica alumina Substances 0.000 description 2
- 239000001273 butane Substances 0.000 description 2
- 125000004432 carbon atom Chemical group C* 0.000 description 2
- 150000001768 cations Chemical class 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- YBMRDBCBODYGJE-UHFFFAOYSA-N germanium dioxide Chemical compound O=[Ge]=O YBMRDBCBODYGJE-UHFFFAOYSA-N 0.000 description 2
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 2
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 2
- 238000002844 melting Methods 0.000 description 2
- 230000008018 melting Effects 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 229910052750 molybdenum Inorganic materials 0.000 description 2
- 239000011733 molybdenum Substances 0.000 description 2
- DDTIGTPWGISMKL-UHFFFAOYSA-N molybdenum nickel Chemical compound [Ni].[Mo] DDTIGTPWGISMKL-UHFFFAOYSA-N 0.000 description 2
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 2
- 125000001477 organic nitrogen group Chemical group 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 1
- QZYDAIMOJUSSFT-UHFFFAOYSA-N [Co].[Ni].[Mo] Chemical compound [Co].[Ni].[Mo] QZYDAIMOJUSSFT-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 125000005210 alkyl ammonium group Chemical group 0.000 description 1
- 230000027455 binding Effects 0.000 description 1
- 238000009739 binding Methods 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- WHDPTDWLEKQKKX-UHFFFAOYSA-N cobalt molybdenum Chemical compound [Co].[Co].[Mo] WHDPTDWLEKQKKX-UHFFFAOYSA-N 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 1
- 229910001657 ferrierite group Inorganic materials 0.000 description 1
- 229940119177 germanium dioxide Drugs 0.000 description 1
- 239000001282 iso-butane Substances 0.000 description 1
- 150000001457 metallic cations Chemical class 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000010705 motor oil Substances 0.000 description 1
- MOWMLACGTDMJRV-UHFFFAOYSA-N nickel tungsten Chemical compound [Ni].[W] MOWMLACGTDMJRV-UHFFFAOYSA-N 0.000 description 1
- 150000002823 nitrates Chemical class 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 150000003467 sulfuric acid derivatives Chemical class 0.000 description 1
- 239000004408 titanium dioxide Substances 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- 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
-
- 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
- C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining 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
- C10G45/60—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 characterised by the catalyst used
- C10G45/64—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 characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
-
- 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
- C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
- C10G65/043—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a change in the structural skeleton
-
- 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
- C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
- C10G65/08—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a hydrogenation of the aromatic 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
- 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
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/10—Lubricating oil
Definitions
- the present invention relates to a process for preparing a heavy base oil.
- base oils such as motor oils to protect the internal combustion engines in motor vehicles.
- the lubricants are generally composed of a majority of base oil and a variety of additives to obtain the desired properties.
- Light lubricating base oils are mainly used in automotive applications and heavy lubricating base oils are used in heavy duty applications such as ship engines and industrial processes.
- Base oils for use in lubricants are on a large scale prepared by firstly hydrotreating a vacuum gas oil distillate and/or a deasphalted oil and by subsequently catalytically dewaxing and hydrofinishing of the
- a noble metal dewaxing catalyst is applied in the catalytic dewaxing step.
- Noble metal dewaxing catalysts are well known to be poisoned by organic nitrogen and organic sulphur compounds and therefore a severe hydrotreating step has to be applied in order to sufficiently reduce the levels of organic nitrogen and organic sulphur compounds in the 370 °C plus product of the hydrotreater .
- hydrotreater improves the quality of the 370 °C plus hydrotreated product which serves as feedstock for a base oil plant.
- a higher hydrotreating severity means that the yield of the 370 °C plus hydrotreated product becomes lower and the overall hydrotreated product lighter (boiling point shift due to severe
- a reduction of the yield of heavy lubricating base oils is undesirable in periods that there is a high demand for heavy base oils.
- Object of the present invention is therefore to provide an upgrading process for hydrocarbonaceous feedstocks in which a high yield of heavy lubricating base oils is obtained.
- This object is achieved when a hydrocarbonaceous feedstock is subjected to an upgrading process which comprises a particular sequence of processing steps.
- the present invention relates to a process for preparing a heavy base oil comprising the steps of:
- step (c) removing at least 50% of the N3 ⁇ 4 and 3 ⁇ 4S which is present in the hydrotreated product as obtained in step (b) ;
- step (c) hydrotreated product as obtained in step (c) with a dewaxing catalyst in the presence of a hydrogen- containing gas under catalytic dewaxing conditions to obtain a dewaxed product, which dewaxing catalyst
- alumina comprises a Group VIII metal hydrogenation component, dealuminated aluminosilicate zeolite crystallites and a low acidity refractory oxide binder material which is essentially free of alumina;
- step (e) hydrofinishing at least part of the dewaxed product as obtained in step (d) with a hydrofinishing catalyst in the presence of a hydrogen-containing gas under
- the heavy lubricating base oils obtained include Group II and Group II
- the hydrocarbonaceous feedstock as provided in step (a) preferably contains more than 65%, but at least 50% by weight of hydrocarbons boiling above 460°C.
- the hydrocarbonaceous feedstock as provided in step (a) has a 370 °C plus fraction that has a viscosity at 100 °C of above 12 cSt, preferably at least 14 cSt.
- the hydrocarbonaceous feedstock contains nitrogen in an amount in the range of from 800-2500 ppmw, preferably in the range of from 1000-1500 ppmw, and sulphur in an amount in the range of from 1.2 to 4.0 %wt, preferably in the range of from 1.5 - 3.0 %wt
- the ratio of the fraction of hydrocarbons boiling in the range of from 370-460 °C and the fraction of hydrocarbons boiling in the range of from 460 to 800°C is preferably less than 10.
- hydrocarbonaceous feedstock examples include straight-run gasoil, hydrocracked gasoil, thermal cracked gasoil, coker gasoil, vacuum gasoil, light or heavy cycle oil, deasphalted oil (DAO) or a combination of two or more thereof.
- the hydrocarbon feedstock may also be a solvent extracted waxy raffinate. At least part of the
- hydrocarbonaceous feedstock as provided in step (a) can suitably be a blend obtained by blending at least one distillate fraction, preferably a vacuum distillate fraction, and a deasphalted oil (DAO) .
- the DAO that can be used is suitably obtained by deasphalting a residual hydrocarbon oil, preferably a vacuum residue.
- a well known and suitable deasphalting method is solvent deasphalting, which involves the counter-current treatment of the residual hydrocarbon oil feed with an extracting solvent.
- This extracting solvent usually is a light hydrocarbon solvent containing paraffinic compounds having 3 to 8 carbon atoms, such as propane, butane, isobutane, pentane, isopentane, hexane and mixtures of two or more of these.
- Preferred paraffinic hydrocarbons are those having 3 to 5 carbon atoms with propane, butane, pentane and mixtures thereof being most
- the solvent deasphalting treatment is conveniently carried out in a rotating disc contactor or a plate column with the residual hydrocarbon oil feed entering in the top section and the extracting solvent entering in the bottom section.
- the lighter hydrocarbons present in the residual hydrocarbon oil dissolve in the extracting solvent and are withdrawn at the top of the apparatus. From this top-fraction, the DAO is obtained after recovery of the extracting solvent.
- asphaltenes which are insoluble in the extracting solvent, are withdrawn at the bottom of the apparatus.
- deasphalting is carried out at a total extracting solvent to residual hydrocarbon oil ratio of 1.5-8 wt/wt, a pressure of 1-50 bar and a temperature of 50-230 °C.
- the deasphalted oil may be obtained by deasphalting a residue fraction, preferably a vacuum residue fraction, containing hydrocarbons that have a boiling point of at least460 °C.
- step (b) the hydrocarbonanceous feedstock is hydrotreated with a suitable hydrotreating catalyst or hydrotreating catalyst package in the presence of a hydrogen-containing gas under hydrotreating conditions to obtain a hydrotreated product which contains nitrogen in an amount in the range of from 30-80 ppmw and sulphur in an amount in the range of from 200-450 ppmw.
- the hydrotreating catalyst or catalyst package to be used in the first reaction zone in step (a) can suitably be a desulphurisation catalyst or a combination of desulphurisation catalysts (including a possible
- the desulphurisation catalyst may be any hydrodesulphurisation catalyst known in the art or combination of hydrotreating catalysts that will deliver hydrotreated effluent with the prescribed levels of nitrogen and sulphur.
- these catalysts comprise a Group VIII metal of the Periodic Table and a compound of a Group VIB metal of the Periodic Table as
- hydrogenation components on a porous catalyst support usually alumina or amorphous silica-alumina.
- alumina usually alumina or amorphous silica-alumina.
- suitable combinations of hydrogenation compounds are cobalt-molybdenum, nickel-molybdenum, nickel-tungsten, and nickel-cobalt-molybdenum.
- hydrodesulphurisation catalyst comprising compounds of nickel and/or cobalt and molybdenum as hydrogenation compounds is preferred.
- the hydrotreated product as obtained in step (b) contains nitrogen in an amount in the range of from 30-80 ppmw and sulphur in an amount in the range of from 200-450 ppmw, which means that the hydrotreating in step (b) is not a severe hydrotreating process.
- use is made of hydrotreating catalysts or hydrotreating catalyst combinations that are not too active. Therefore, preferably use is made of an alumina-based hydrotreating catalyst.
- the catalyst is substantially free of a cracking component.
- a catalyst or combination of catalysts comprising nickel and/or cobalt and molybdenum supported on alumina without a zeolitic cracking compound is particularly preferred.
- step (b) also use can be made of stacked-bed configurations in which two or more hydrotreating
- the temperature in the hydrotreating step is suitably in the range of from 250-480 °C, preferably in the range of from 280-450 °C, and more preferably in the range of from 350-420 °C.
- Suitable hydrotreating pressures are in the range of from 30-250 bara.
- the hydrotreating pressure is in the range of from 110 to 180 bara, more preferably in the range of from 120 to 170 bara.
- the weight hourly space velocity is suitably in the range of from 0.2-10 hr -1 , preferably in the range of from 0.2-2.0 hr -1 , and more preferably in the range of from 0.2-1.0 hr "1 .
- step (a) will inter alia depend on the catalyst used, and the sulphur content and nitrogen content of the hydrocarbon feedstock.
- the ratio of the amount of nitrogen and the amount of sulphur (N/S) in the hydrotreated product as obtained in step (b) is suitably in the range of from 0.1-0.3, preferably in the range of from 0.12-0.28
- step (c) at least 50% of the N3 ⁇ 4 and 3 ⁇ 4S which is present in the hydrotreated product as obtained in step (b) is removed.
- at least part of the N3 ⁇ 4 and 3 ⁇ 4S which is present in the hydrotreated product as obtained in step (b) is removed by means of stripping, preferably steam stripping.
- the stripping is carried out at a temperature ranging from 100 to 350C, preferably from 130 to 240C and a pressure ranging from 1 to 50 bar, preferably from 1.5 to 10 bar.
- the stripping is carried out at a temperature ranging from 100 to 350C, preferably from 130 to 240C and a pressure ranging from 1 to 50 bar, preferably from 1.5 to 10 bar.
- step (c) preferably at least 95% of the N3 ⁇ 4 and 3 ⁇ 4S which is present in the hydrotreated product as obtained in step (b) is removed from the hydrotreated product in step (c) .
- step (c) also hydrocarbons boiling below
- step (b) the entire hydrotreated product as obtained in step (b) is subjected to step (c) .
- step (d) at least part of the hydrotreated product as obtained in step (c) is catalytically dewaxed with a dewaxing catalyst in the presence of a hydrogen- containing gas under catalytic dewaxing conditions to obtain a dewaxed product, which dewaxing catalyst comprises a Group VIII metal hydrogenation component, dealuminated aluminosilicate zeolite crystallites and a low acidity refractory oxide binder.
- step (c) the entire hydrotreated product as obtained in step (c) is subjected to step (d) .
- catalytic dewaxing is here meant a process for decreasing the pour point of lubricating base oil products by selectively converting the components of the oil feed which impart a high pour point to products which do not impart a high pour point.
- Products which impart a high pour point are compounds having a high melting point. These compounds are referred to as waxes. Wax compounds include for example high temperature melting normal paraffins, iso-paraffins and mono-ringed
- the pour point is preferably reduced by at least 40 °C and more preferably by at least 60 °C.
- the hydrocarbonacous feedstock in the process according to the present invention will thus contain waxy molecules which impart an undesirable high pour point. Small amounts of these compounds can strongly influence the pour point.
- the feedstock will suitably contain between less than 2% and up to 80% of these waxy compounds.
- the hydrotreated feedstock is contacted under catalytic dewaxing conditions with a catalyst composition comprising a Group VIII metal hydrogenation component, dealuminated aluminosilicate zeolite crystallites and a low acidity refractory oxide binder.
- the aluminosilicate zeolite crystallites preferably have pores with a diameter in the range of from 0.35 to 0.80 nm. This diameter refers to the maximum pore
- the pores in a molecular sieve are polygonal shaped channels having a minimum and a maximum pore diameter.
- the maximum pore diameter is the critical parameter, because it determines the size of the waxy molecules which can enter the pores.
- aluminosilicate zeolites which are suitable to be used in the present invention are
- the zeolitic component is ZSM-5, ZSM-11, ZSM-12, ZSM-22, ZSM-23, ZSM- 35, ZSM-38, ZSM-48, ZSM-57, SSZ-23, SSZ-24, SSZ-25, SSZ- 26, SSZ-32, SSZ-33 and MCM-22 and mixtures of two or more of these.
- the zeolitic component is ZSM-5,
- the zeolitic component in the dewaxing catalyst is present in an amount in the range of from 10- 50 wt%, based on the total weight of the dewaxing
- Preferred aluminosilicate zeolites are of the MFI- topology for example ZSM-5.
- the dewaxing catalyst also comprises a low acidity refractory oxide binder material which is essentially free of alumina. Examples are low acidity refractory oxides such as silica, zirconia, titanium dioxide, germanium dioxide, boria and mixtures of two or more of these.
- the most preferred binder is silica.
- the weight ratio of modified molecular sieve to binder is suitably within the range of from 05/95 to 95/05.
- alumina moiety refers to an
- a ⁇ C ⁇ -unit which is part of the framework of the alumino- silicate zeolite, i.e. which has been incorporated via covalent bindings with other oxide moieties, such as silica (S1O2), in the framework of the aluminosilicate zeolite.
- the mole percentage of alumina present in the aluminosilicate zeolite is defined as the percentage of moles AI2O3 relative to the total number of moles of oxides constituting the aluminosilicate zeolite (prior to dealumination) or modified molecular sieve (after
- the surface of the zeolite crystallites is selectively dealuminated .
- dealumination results in a reduction of the number of surface acid sites of the zeolite crystallites, whilst not affecting the internal structure of the zeolite crystallites .
- Dealumination can be attained by methods known in the art. Particularly useful methods are those, wherein the dealumination selectively occurs, or anyhow is claimed to occur selectively, at the surface of the crystallites of - li the molecular sieve. Examples of dealumination processes are described in the afore mentioned WO-A-9641849.
- dealumination is performed by a process in which the zeolite is contacted with an aqueous
- fluorosilicate salt is represented by the formula:
- ⁇ ⁇ ' is a metallic or non-metallic cation other than H+ having the valence x b' .
- This treatment will be also referred to as the AHS treatment.
- cations x b' are alkylammonium, NH4 + , Mg ++ , Li + , Na + , K + , Ba ++ , Cd ++ , Cu+, Ca ++ , Cs+, Fe ++ , Co ++ , Pb ++ , Mn ++ , Rb+, Ag + , Sr ++ , Tl + , and Zn ++ .
- ⁇ ⁇ ' is the ammonium cation.
- the zeolite material may be contacted with the fluorosilicate salt at a pH of suitably between 3 and 7.
- Such a dealumination process is for example described in US-A-5157191.
- the dealumination treatment is referred to as the AHS-treatment .
- the dewaxing catalyst to be used in accordance with the present invention is preferably prepared by first extruding the aluminosilicate zeolite with the binder and subsequently subjecting the extrudate to a dealumination treatment, preferably the AHS treatment as described above. It has been found that an increased mechanical strenght of the catalyst extrudate is obtained when prepared according to this sequence of steps.
- the Group VIII metal of the Periodic Table is
- the catalyst extrudate comprising the dealuminated aluminosilicate zeolite crystallites by known techniques, such as ion-exchange techniques.
- Typical ion-exchange techniques call for contacting the selected zeolite with a salt of the desired replacing cation.
- a salt of the desired replacing cation a wide variety of salts can be employed, particular preference is given to chloride, nitrates and sulphates.
- Representative ion-exchange techniques are disclosed in a wide variety of patents including
- step (d) use is made of dewaxing catalyst which comprises a Group VIII metal hydrogenation component.
- Group VIII metal components include those components based on both noble and non-noble metals.
- Particularly suitable Group VIII metal components are palladium, platinum, nickel and/or cobalt in sulphidic, oxidic and/or elemental form.
- the total amount Group VIII metal of the Periodic Table will suitably not exceed 10% by weight calculated as element and based on total weight of support, and preferably is in the range of from 0.1 to 5.0% by weight, more preferably from 0.2 to 3.0% by weight. If both platinum and palladium are present, the weight ratio of platinum to palladium may vary within wide limits, but suitably is in the range of from 0.05 to 10, more suitably 0.1 to 5. Catalysts comprising
- hydrogenation component is preferably platinum or
- the catalytic dewaxing conditions in step (d) of the process according to the invention are typical catalytic dewaxing conditions. Therefore, the temperature is suitably in the range of from 300-400 °C, preferably in the range of from 320-390 °C, and more preferably in the range of from 330-380 °C. Suitable dewaxing pressures are in the range of from 80-240 bara. Preferably, the
- dewaxing pressure is in the range of from 100-180 bara, more preferably in the range of from 120-170 bara.
- the weight hourly space velocity in step (d) is suitably in the range of from 0.4 to 7 hr -1 , preferably in the range of from 0.5 to 2.5 hr -1 , and more preferably in the range of from 0.65 to 2.25 hr -1 .
- Step (d) is carried out in the presence of hydrogen.
- Hydrogen is suitably supplied to the second reaction zone at a rate of 350 to 1500 Nl/kg feed.
- the dewaxed product as obtained in step (d) has a viscosity index (VI) which enables the production of high VI lubricating base oils.
- the dewaxed product as obtained in step (d) suitably contains sulphur in an amount of less than 350 ppmw, preferably less than 300 ppmw, and it contains nitrogen in an amount of less than 80 ppmw, preferably less than 60 ppmw.
- the dewaxed product has suitably a viscosity at 100 °C in the range of 10 to 17 cSt, preferably in the range of from 10 to 15 cSt.
- step (e) at least part of the dewaxed product as obtained in step (d) is hydrofinished with a
- hydrofinishing catalyst in the presence of a hydrogen- containing gas under hydrofinishing conditions to obtain a heavy base oil.
- step (d) the entire dewaxed product as obtained in step (d) is subjected to step (e) .
- Hydrofinishing is known in the art and examples of suitable hydrofinishing steps are disclosed in, for instance, US-A-5139647, WO-A-9201657 and WO-A-9201769.
- hydrofinishing comprises contacting a
- hydrocarbon feed in this case a feed comprising the dewaxed lubricating base oil, with a hydrogenation catalyst under relatively mild conditions in order to saturate at least part of the aromatics still present in the dewaxed base oil.
- Suitable catalysts are those normally applied for this purpose with noble metal-based catalysts, such as those comprising Pt and/or Pd supported on an amorphous silica-alumina carrier.
- a non- noble metal hydrofinishing catalyst a so-called base metal hydrofinishing catalyst such as nickel-molybdenum on an alumina support.
- Hydrofinishing conditions as per invention involve operating temperatures up to 390 °C and preferably in the range of from 300 to 380 °C, more preferably 330 to
- 200 bara preferably in the range of from 100 to 170 bara, and weight hourly space velocities in the range of from 0.3-2.5 hr -1 , preferably in the range of from 0.5 - 1.5 hr "1 .
- the yield of the heavy base oil in step (e) is high when compared to known processes for preparing base oils wherein use is made of hydrocracking and catalytically dewaxing steps.
- This high yield of heavy base oils can be expressed as the ratio of heavy base oil over light base oil as obtained in step (e) .
- the high yield of heavy base oil can for instance be expressed as the ratio of 500N base oil over 150N base oil as obtained in step (e) .
- the 500 N base oil is a heavy Group II base oil having typically a viscosity at 100 °C in the range of from 10.0-12.9 cSt, whereas the 150N base oil is a light Group
- the ratio of 500N base oil over 150N base oil as obtained in step (e) is at least 1.0, preferably at least 1.5, more preferably at least 2.5, and most preferably at least 3.0.
- step (f) the heavy base oil is recovered.
- the heavy base oil as obtained in step (e) can for instance be separated from the other components of the effluent from the hydrofinishing process, including light base oils, by means of conventional methods, such as by distillation under atmospheric or reduced pressure. Of these, distillation under reduced pressure, including vacuum flashing and vacuum distillation, is most suitably applied.
- the cut point (s) of the distillate fraction (s) is/are selected such that each product distillate
- the heavy base oil as recovered in step (f) suitably contains sulphur in an amount of less than 300 ppmw, preferably less than 200 ppmw, and it contains nitrogen in an amount of less than 80 ppmw, preferably less than 50 ppmw.
- the heavy base oil has suitably a viscosity at
- a Basrah Light waxy distillate feedstock is provided in a step (a) .
- Table 1 Main characteristics of the feedstock
- a step (b) the feedstock is hydrotreated.
- the feedstock as described in Table 1 is hydrotreated over a conventional NiMo on alumina hydrotreating catalyst (for this example C-424 from Criterion catalyst portfolio) aiming at producing a hydrotreated effluent (370 °C+ fraction) containing ca. 50 ppm nitrogen and ca. 300 ppm sulphur.
- a conventional NiMo on alumina hydrotreating catalyst for this example C-424 from Criterion catalyst portfolio
- iMo/Al20 3 -type-II hydrotreating catalyst like for example DN-3100 from Criterion catalyst portfolio.
- the operating conditions and main outcome of the hydroprocessing step are indicated in Table 3.
- step (c) products obtained in step (c) are subjected to a dewaxing step in accordance with the present invention and a conventional dewaxing step.
- Example 1 The 370 °C+ fraction of Example 1 is catalytically dewaxed on Shell commercial dewaxing catalyst SLD-800, a base metal (Ni) catalyst specifically developed for the dewaxing of severely contaminated feedstocks.
- Example 2 The 370 °C+ fraction of Example 2 is catalytically dewaxed on Shell commercial dewaxing catalyst SLD-821, a noble metal (Pt) catalyst specifically developed for the dewaxing of deeply hydrotreated feedstocks for base oil
- step (e) the dewaxed product as obtained in step (d) according to the present invention is
- Example 3 The 370 °C+ fraction of Example 3, stripped from any gases, is submitted to a hydrofinishing step using either a base metal hydrofinishing catalyst (high active
- Example 5a or a noble metal hydrofinishing catalyst (like Criterion LN-5) ;
- Example 5b known for its high hydrogenation power and resistance to sulphur and nitrogen poisoning.
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Abstract
L'invention concerne un procédé de préparation d'une huile de base lourde comprenant les étapes suivantes : (a) la préparation d'une matière première hydrocarbonée qui contient au moins 50 % en poids d'hydrocarbures ayant un point d'ébullition supérieur à 460 °C, de l'azote en une quantité dans la plage allant de 800 à 2 500 ppm en poids, et du soufre en une quantité dans la plage allant de 1,5 à 4,0 ppm en poids ; (b) l'hydrotraitement de la matière première hydrocarbonée avec un catalyseur d'hydrotraitement en présence d'un gaz contenant de l'hydrogène dans des conditions d'hydrotraitement pour obtenir un produit hydrotraité qui contient de l'azote en une quantité dans la plage allant de 30 à 80 ppm en poids et du soufre en une quantité dans la plage allant de 200 à 450 ppm en poids ; (c) l'élimination d'au moins 50 % du N¾ et du ¾S présents dans le produit hydrotraité tel qu'obtenu à l'étape (b) ; (d) le déparaffinage catalytique d'au moins une partie du produit hydrotraité tel qu'obtenu à l'étape (c) avec un catalyseur de déparaffinage en présence d'un gaz contenant de l'hydrogène dans des conditions de déparaffinage catalytique pour obtenir un produit déparaffiné, ledit catalyseur de déparaffinage comprenant un composant d'hydrogénation métallique du groupe VIII, des cristallites de zéolithe aluminosilicate désaluminée et un matériau liant oxydique réfractaire de faible acidité qui est essentiellement exempt d'alumine ; (e) l'hydrofinition d'au moins une partie du produit déparaffiné tel qu'obtenu à l'étape (d) avec un catalyseur d'hydrofinition en présence d'un gaz contenant de l'hydrogène dans des conditions d'hydrofinition pour obtenir une huile de base lourde ; et (f) la récupération de l'huile de base lourde.
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EP14720073.7A EP2992070A2 (fr) | 2013-05-02 | 2014-04-22 | Procédé de préparation d'une huile de base lourde |
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EP13166276 | 2013-05-02 | ||
PCT/EP2014/058144 WO2014177424A2 (fr) | 2013-05-02 | 2014-04-22 | Procédé de préparation d'une huile de base lourde |
EP14720073.7A EP2992070A2 (fr) | 2013-05-02 | 2014-04-22 | Procédé de préparation d'une huile de base lourde |
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EP14720073.7A Withdrawn EP2992070A2 (fr) | 2013-05-02 | 2014-04-22 | Procédé de préparation d'une huile de base lourde |
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EP (1) | EP2992070A2 (fr) |
KR (1) | KR20160003203A (fr) |
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Family Cites Families (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
MY125670A (en) * | 1995-06-13 | 2006-08-30 | Shell Int Research | Catalytic dewaxing process and catalyst composition |
AU724570B2 (en) * | 1996-07-15 | 2000-09-28 | Chevron U.S.A. Inc. | Base stock lube oil manufacturing process |
TWI277649B (en) * | 2001-06-07 | 2007-04-01 | Shell Int Research | Process to prepare a base oil from slack-wax |
US7282137B2 (en) * | 2002-10-08 | 2007-10-16 | Exxonmobil Research And Engineering Company | Process for preparing basestocks having high VI |
CN1317368C (zh) * | 2004-03-31 | 2007-05-23 | 中国石油化工股份有限公司 | 一种润滑油基础油的制备方法 |
EP1997868A1 (fr) * | 2007-05-30 | 2008-12-03 | Shell Internationale Researchmaatschappij B.V. | Procédé pour la production d'huile à base naphténique |
US8182672B2 (en) * | 2007-12-28 | 2012-05-22 | Exxonmobil Research And Engineering Company | Process for preparing lube basestocks having superior low temperature properties at high VI |
-
2014
- 2014-04-22 RU RU2015151620A patent/RU2671862C2/ru active
- 2014-04-22 EP EP14720073.7A patent/EP2992070A2/fr not_active Withdrawn
- 2014-04-22 KR KR1020157034081A patent/KR20160003203A/ko not_active Application Discontinuation
- 2014-04-22 WO PCT/EP2014/058144 patent/WO2014177424A2/fr active Application Filing
- 2014-04-22 CN CN201480024800.5A patent/CN105209580B/zh active Active
Non-Patent Citations (1)
Title |
---|
See references of WO2014177424A3 * |
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Also Published As
Publication number | Publication date |
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CN105209580A (zh) | 2015-12-30 |
KR20160003203A (ko) | 2016-01-08 |
WO2014177424A3 (fr) | 2015-01-08 |
RU2671862C2 (ru) | 2018-11-07 |
RU2015151620A (ru) | 2017-06-07 |
RU2015151620A3 (fr) | 2018-03-19 |
WO2014177424A2 (fr) | 2014-11-06 |
CN105209580B (zh) | 2018-06-08 |
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