EP0441195B1 - Process for the preparation of base oils and middle distillates stabilized against oxydation and low temperatures - Google Patents
Process for the preparation of base oils and middle distillates stabilized against oxydation and low temperatures Download PDFInfo
- Publication number
- EP0441195B1 EP0441195B1 EP91100942A EP91100942A EP0441195B1 EP 0441195 B1 EP0441195 B1 EP 0441195B1 EP 91100942 A EP91100942 A EP 91100942A EP 91100942 A EP91100942 A EP 91100942A EP 0441195 B1 EP0441195 B1 EP 0441195B1
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- catalyst
- zeolite
- boiling
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- 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.)
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Links
- 238000000034 method Methods 0.000 title claims description 22
- 239000002199 base oil Substances 0.000 title claims description 20
- 238000007254 oxidation reaction Methods 0.000 title claims description 7
- 238000002360 preparation method Methods 0.000 title claims description 6
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 30
- 239000003054 catalyst Substances 0.000 claims description 30
- 239000010457 zeolite Substances 0.000 claims description 24
- 238000009835 boiling Methods 0.000 claims description 22
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 22
- 229910021536 Zeolite Inorganic materials 0.000 claims description 18
- 238000004517 catalytic hydrocracking Methods 0.000 claims description 14
- 239000000377 silicon dioxide Substances 0.000 claims description 14
- 235000012239 silicon dioxide Nutrition 0.000 claims description 14
- 229910052681 coesite Inorganic materials 0.000 claims description 11
- 229910052906 cristobalite Inorganic materials 0.000 claims description 11
- 239000007789 gas Substances 0.000 claims description 11
- 239000003921 oil Substances 0.000 claims description 11
- 229910052682 stishovite Inorganic materials 0.000 claims description 11
- 229910052905 tridymite Inorganic materials 0.000 claims description 11
- 239000007788 liquid Substances 0.000 claims description 9
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 8
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 8
- 229910052739 hydrogen Inorganic materials 0.000 claims description 8
- 239000001257 hydrogen Substances 0.000 claims description 8
- 238000005984 hydrogenation reaction Methods 0.000 claims description 8
- 229910052751 metal Inorganic materials 0.000 claims description 6
- 239000002184 metal Substances 0.000 claims description 6
- 230000003647 oxidation Effects 0.000 claims description 6
- 239000012071 phase Substances 0.000 claims description 6
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 5
- 150000002739 metals Chemical class 0.000 claims description 5
- 230000000737 periodic effect Effects 0.000 claims description 5
- 229910052593 corundum Inorganic materials 0.000 claims description 4
- 238000004821 distillation Methods 0.000 claims description 4
- 229910052698 phosphorus Inorganic materials 0.000 claims description 4
- 239000011574 phosphorus Substances 0.000 claims description 4
- 229910001845 yogo sapphire Inorganic materials 0.000 claims description 4
- 229910052799 carbon Inorganic materials 0.000 claims description 3
- 239000012876 carrier material Substances 0.000 claims description 3
- 239000000017 hydrogel Substances 0.000 claims description 3
- 239000002480 mineral oil Substances 0.000 claims description 3
- 235000010446 mineral oil Nutrition 0.000 claims description 3
- 238000002329 infrared spectrum Methods 0.000 claims description 2
- 239000007791 liquid phase Substances 0.000 claims description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims 1
- 239000000314 lubricant Substances 0.000 claims 1
- 239000011734 sodium Substances 0.000 claims 1
- 229910052708 sodium Inorganic materials 0.000 claims 1
- 239000000203 mixture Substances 0.000 description 10
- 238000006243 chemical reaction Methods 0.000 description 9
- 238000004519 manufacturing process Methods 0.000 description 8
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 7
- 239000010687 lubricating oil Substances 0.000 description 6
- JKQOBWVOAYFWKG-UHFFFAOYSA-N molybdenum trioxide Chemical compound O=[Mo](=O)=O JKQOBWVOAYFWKG-UHFFFAOYSA-N 0.000 description 6
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 229910000323 aluminium silicate Inorganic materials 0.000 description 4
- 230000003197 catalytic effect Effects 0.000 description 4
- WQOXQRCZOLPYPM-UHFFFAOYSA-N dimethyl disulfide Chemical compound CSSC WQOXQRCZOLPYPM-UHFFFAOYSA-N 0.000 description 4
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 230000006641 stabilisation Effects 0.000 description 4
- 238000011105 stabilization Methods 0.000 description 4
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 239000003513 alkali Substances 0.000 description 3
- QGAVSDVURUSLQK-UHFFFAOYSA-N ammonium heptamolybdate Chemical compound N.N.N.N.N.N.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.[Mo].[Mo].[Mo].[Mo].[Mo].[Mo].[Mo] QGAVSDVURUSLQK-UHFFFAOYSA-N 0.000 description 3
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 239000010705 motor oil Substances 0.000 description 3
- PXHVJJICTQNCMI-UHFFFAOYSA-N nickel Substances [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 3
- KBJMLQFLOWQJNF-UHFFFAOYSA-N nickel(ii) nitrate Chemical compound [Ni+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O KBJMLQFLOWQJNF-UHFFFAOYSA-N 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- ZOXJGFHDIHLPTG-UHFFFAOYSA-N Boron Chemical compound [B] ZOXJGFHDIHLPTG-UHFFFAOYSA-N 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- 229910052784 alkaline earth metal Inorganic materials 0.000 description 2
- 125000003118 aryl group Chemical group 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- KGBXLFKZBHKPEV-UHFFFAOYSA-N boric acid Chemical compound OB(O)O KGBXLFKZBHKPEV-UHFFFAOYSA-N 0.000 description 2
- 229910052796 boron Inorganic materials 0.000 description 2
- 238000001354 calcination Methods 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 239000002283 diesel fuel Substances 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 235000019253 formic acid Nutrition 0.000 description 2
- NAQMVNRVTILPCV-UHFFFAOYSA-N hexane-1,6-diamine Chemical compound NCCCCCCN NAQMVNRVTILPCV-UHFFFAOYSA-N 0.000 description 2
- 230000000887 hydrating effect Effects 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 238000005470 impregnation Methods 0.000 description 2
- 229910052750 molybdenum Inorganic materials 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 229910052814 silicon oxide Inorganic materials 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- XFNJVJPLKCPIBV-UHFFFAOYSA-N trimethylenediamine Chemical compound NCCCN XFNJVJPLKCPIBV-UHFFFAOYSA-N 0.000 description 2
- 229910052721 tungsten Inorganic materials 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- VILCJCGEZXAXTO-UHFFFAOYSA-N 2,2,2-tetramine Chemical compound NCCNCCNCCN VILCJCGEZXAXTO-UHFFFAOYSA-N 0.000 description 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000010306 acid treatment Methods 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 230000001476 alcoholic effect Effects 0.000 description 1
- 150000001342 alkaline earth metals Chemical class 0.000 description 1
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 150000001639 boron compounds Chemical class 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000003776 cleavage reaction Methods 0.000 description 1
- UFMZWBIQTDUYBN-UHFFFAOYSA-N cobalt dinitrate Chemical compound [Co+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O UFMZWBIQTDUYBN-UHFFFAOYSA-N 0.000 description 1
- 229910001981 cobalt nitrate Inorganic materials 0.000 description 1
- 229910000428 cobalt oxide Inorganic materials 0.000 description 1
- IVMYJDGYRUAWML-UHFFFAOYSA-N cobalt(ii) oxide Chemical compound [Co]=O IVMYJDGYRUAWML-UHFFFAOYSA-N 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- SBZXBUIDTXKZTM-UHFFFAOYSA-N diglyme Chemical compound COCCOCCOC SBZXBUIDTXKZTM-UHFFFAOYSA-N 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 230000009969 flowable effect Effects 0.000 description 1
- 229940097789 heavy mineral oil Drugs 0.000 description 1
- XXMIOPMDWAUFGU-UHFFFAOYSA-N hexane-1,6-diol Chemical compound OCCCCCCO XXMIOPMDWAUFGU-UHFFFAOYSA-N 0.000 description 1
- 238000001027 hydrothermal synthesis Methods 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 238000005461 lubrication Methods 0.000 description 1
- 239000011733 molybdenum Substances 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 229910000480 nickel oxide Inorganic materials 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 229910017464 nitrogen compound Inorganic materials 0.000 description 1
- 150000002830 nitrogen compounds Chemical class 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
- 150000002898 organic sulfur compounds Chemical class 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 229920000768 polyamine Polymers 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 238000003385 ring cleavage reaction Methods 0.000 description 1
- 230000007017 scission Effects 0.000 description 1
- 150000003377 silicon compounds Chemical class 0.000 description 1
- 239000003381 stabilizer Substances 0.000 description 1
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 description 1
- 239000010937 tungsten Substances 0.000 description 1
- 238000005406 washing 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
- 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
Definitions
- the invention relates to the production of middle distillates in the boiling range from 180 to 360 ° C on the one hand and an oxidation-stable residue suitable as a base oil for lubricating oils on the other hand by treating mineral oil fractions with a boiling range above 350 ° C in a first stage by hydrocracking and in a second stage Hydrogenation with a catalyst based on a borosilicate zeolite.
- Base oils with very high viscosity indices can be obtained by hydrocracking vacuum gas oils.
- components with low VI are either split into low-boiling components or converted into compounds with high VI by hydrogenation, ring cleavage and isomerization.
- the subsequent dewaxing serves to improve the fluidity at low temperatures.
- Long-chain, unbranched and little branched hydrocarbons are separated. This separation can take place physically by precipitating the paraffin crystals at low temperatures using a mixture of solvents or by hydrogenating cleavage of these compounds on shape-selective catalysts.
- To assess fluidity e.g. the determination of the pour point according to DIN 51 597 is used.
- the oxidation stability can be adjusted by hydrogenating the base oil or by adding stabilizers.
- the test can be carried out according to DIN 51 352, for example, by increasing the Conradson coke residue after aging by passing air through it.
- US Pat. No. 4,347,121 describes a process in which base oils for the production of lubricating oil are obtained in succession by hydrocracking, hydrofinishing and catalytic dewaxing with viscosity indices of approximately 100 which are stable to oxidation and sufficiently flowable at low temperatures.
- DE-PS 2 613 877 relates to a process for the production of lubricating oil in which lubricating oils with a low pour point and a VI of 95 are obtained via two hydrocracking stages and a catalytic dewaxing stage.
- the viscosity index of the base oil obtained in all these processes is not sufficient to produce high-quality lubricating oils from these base oils.
- This object was achieved with a two-stage process for the production of oxidation-stable base oils with a VI (viscosity index) 110 to 135 (VHVI oils) and very good fluidity at low temperature by using heavy mineral oil fractions with a boiling range above 350 ° C on one Hydrocracking catalyst converted under hydrocracking conditions to 20 to 80 wt .-% in portions that boil below 360 ° C, the reactor discharge, if necessary, in a high pressure separator into liquid and gas phase, the entire reactor discharge or only the liquid phase, directly, or after distilling off the bottom 360 ° C boiling in a second stage treated with hydrogen in the presence of a catalyst at 200 to 450 ° C and 20 to 150 bar, which is a crystalline borosilicate zeolite of the pentasil type, aluminum oxide and / or amorphous aluminosilicate as a carrier material and one or more metals from the Group VIb and / or Group VIII of the Periodic Table and Pho sphor contains, and after
- the first stage is generally carried out at pressures of 40 to 150 bar, temperatures of 300 to 450 ° C. and specific catalyst loads of 0.1 to 4 kg / lxh with hydrogen in the presence of a catalyst, the support of which is preferably made of aluminum oxide, a amorphous aluminosilicate and / or a dealuminated Y zeolite, and which contains as hydrogenation components one or more metals from group VI b and / or VIII of the periodic table and phosphorus.
- the entire liquid outflow from the first stage is fed directly to the second stage without intermediate relaxation or after the parts boiling below 360 ° C. have been distilled off, with printing of e.g. 20 to 150 bar, temperatures of e.g.
- the VI from 110 to 135 in base oil with a boiling point> 360 ° C is set in the first stage using different degrees of conversion.
- the degree of conversion is the quotient of the portion boiling below 360 ° C and the total hydrocarbon portion.
- the reaction conditions pressure, temperature and specific catalyst load
- the reaction conditions are selected so that the resulting base oil with a start of boiling above 360 ° C is stable to oxidation and has a pour point below -12 ° C.
- a further surprising advantage of the method according to the invention is the finding that the base oils according to the method respond better to pour point improvers than base oils which have been dewaxed with solvents.
- middle distillates obtained in this process have excellent cooling properties.
- the pour point is always below -30 ° C.
- Such middle distillates are valuable mixed components for the production of low-temperature diesel fuels.
- the preparation of catalysts for the hydrocracking stage of the process according to the invention can be carried out by mixing an aluminum oxide component with a silicon oxide component or an aluminosilicate, optionally with the addition of a dealuminated zeolite of the Y type with an SiO2 / Al2O3 molar ratio in the range from 7 to 150 and a peptizing agent, such as for example formic acid.
- a SiO2 component a hydrogel with a SiO2 content of 10 to 20% by weight is particularly suitable Bands in the IR spectrum at wavenumbers of 1,630 and 960 cm ,1, a Na content of less than 0.01% by weight and a BET surface area of more than 400 m2 / g.
- the dealumination of the Y zeolite can be carried out by acid treatment, for example according to DE-PS 2 435 716.
- 20 to 95% by weight of aluminum oxide, preferably 30 to 60% by weight and 5 to 50% by weight of silicon dioxide, preferably 20 to 40% by weight, can be used in amorphous carrier fractions.
- the weight fraction of dealuminated Y zeolite in the carrier can be varied in the range from 0 to 30.
- the paste is extruded through a die with a diameter between 1 and 3 mm and then dried and calcined at elevated temperatures.
- the carrier composition of the catalyst used in the second stage, the dewaxing and stabilization stage, of the process according to the invention can expediently vary in the range from 10 to 90% by weight of boron zeolite of the pentasil type, 10 to 90% by weight of aluminum oxide and 20 to 40% by weight. -% silicon oxide.
- the borosilicate zeolites of the pentasil type are characterized by a high SiO2 / B2O3 ratio and by pore sizes between those of type A zeolites and those of type X or Y.
- borosilicate zeolites can also be prepared if the reaction is carried out in ethereal solution, e.g. Diethylene glycol dimethyl ether or in alcoholic solution, e.g. 1,6-hexanediol.
- ethereal solution e.g. Diethylene glycol dimethyl ether
- alcoholic solution e.g. 1,6-hexanediol.
- the synthesis of borosilicate zeolites in aqueous polyamine solution without the addition of alkali is essential and particularly advantageous. After their isolation, drying at 100 ° C. to 160 ° C., preferably 110 ° C. and calcination at 450 to 550 ° C., preferably 500 ° C., the zeolites thus produced can be shaped together with the other carrier materials.
- the hydrogenation components for the catalysts in both stages of the process according to the invention can be incorporated into the moist carrier mixture and / or applied to the catalyst carrier by impregnation.
- the catalyst particles are brought into contact, for example, one or more times with a solution which contains the desired hydrogenation components.
- the amount of solution corresponds to the previously determined water absorption of the catalyst particles.
- hydrogenation metal components preferably Co, Ni, Mo, and W, for example in the form of ammonium heptamolybdate, nickel nitrate, ammonium metatungstate, cobalt nitrate.
- the finished catalyst is obtained after renewed drying and calcination and can contain 2 to 10 wt .-% nickel or cobalt oxide and 10 to 25 wt .-% molybdenum or tungsten, calculated as MoO3 and WO3.
- Phosphorus components can also be added to the catalysts, both when the carrier components are mixed and as part of the impregnation solution. Amounts in the range of 1 to 12% by weight of P2O5 based on the finished catalyst are usually added.
- the catalysts Before using the catalysts, they are sulfurized from the oxidic to the more active sulfidic form, e.g. by passing a mixture of hydrogen and H2S converted.
- Suitable feedstocks for the process are heavy gas oils, vacuum gas oils, deasphalted residue oils and mixtures thereof in the boiling range above 350 ° C. A prior breakdown of the organic sulfur and nitrogen compounds is not necessary, but is advantageous in certain cases.
- the procedure is appropriately such that the feed is added to the hydrocracking reactor together with hydrogen and brought to the reaction temperature.
- the conversion rate for a boiling temperature ⁇ 360 ° C is set between 20 and 80%.
- the effluent from the hydrocracking reactor is separated into a liquid and gas phase in a high pressure separator.
- Ammonia and hydrogen sulfide, which are contained in the gas phase, are optionally separated in a downstream wash, and the hydrogen is returned to the reaction zone.
- the liquid portion is fed to the second reactor at the same pressure level, where dewaxing and hydrating stabilization take place.
- the addition of a sulfur component for example dimethyl disulfide (DMDS), is necessary before entering the second reactor in order to prevent desulfurization of the catalyst.
- DMDS dimethyl disulfide
- the effluent from the second reactor is separated in a further high-pressure separator in a downstream distillation into liquid gas, naphtha, middle distillate and a residue with a boiling point> 360 ° C. Due to its viscosity index between 110 and 135, its oxidation stability and its pour point below -12 ° C, this residue is ideal as a base oil for the production of high-quality lubricating oils.
- the base oils obtained by the process according to the invention respond much better to pour point improvers than, for example, base oils dewaxed with solvents. It won't just be requires smaller amounts of pour point improver to set a given pour point, but also reaches lower-lying pour points than was possible using conventional methods.
- the middle distillates in the boiling range 180 to 360 ° C are only separated after the dewaxing stage, this results in excellent cold properties for these middle distillates.
- the distillates With a pour point of ⁇ -30 ° C, the distillates also meet extreme requirements, e.g. for diesel fuel in winter operation.
- a moist carrier mixture is prepared by mixing 227 g of hydrogel (SiO2 content 15%) with 102 g of aluminum oxide and 10 g of formic acid, adding 18 g of phosphoric acid, 16.2 g of nickel nitrate and 309 g of ammonium heptamolybdate dissolved in 150 ml of water.
- the carrier mixture is extruded through a 1.5 mm die, then dried at 150 ° C. and calcined at 500 ° C. for 5 hours.
- the moldings are impregnated with a solution consisting of nickel nitrate and ammonium heptamolybdate and dried and calcined again.
- the finished catalyst has the following composition (wt .-%): Al2O3 51, SiO2 17, MoO3 18, NiO 5, [PO4] 3 ⁇ 9.
- a borosilicate zeolite of the pentasil type is in a hydrothermal synthesis from 640 g of highly disperse SiO2, 122 g of H3BO3, 8000 g of an aqueous 1,6-hexanediamine solution (mixture 50:50 wt .-%) at 170 ° C under autogenous pressure in a stirred autoclave without added alkali. After filtering off and washing out, the crystalline reaction product is dried at 100 ° C./24 h and calcined at 500 ° C./24 h.
- This borosilicate zeolite is composed of 94.2 wt .-% SiO2 and 2.3 wt .-% B2O3 (loss on ignition: 3.5 wt .-%).
- the catalyst was prepared as described in Example 1 with the addition of the borosilicate zeolite.
- the gaseous constituents were separated off in a high-pressure separator and the entire liquid portions were fed to the dewaxing stage.
Description
Die Erfindung betrifft die Herstellung von Mitteldestillaten im Siedebereich von 180 bis 360°C einerseits und einem als Grundöl für Schmieröle geeigneten oxydationsstabilen Rückstands andererseits durch Behandlung von Mineralölfraktionen mit einem Siedebereich oberhalb von 350°C in einer ersten Stufe durch Hydrocracking und in einer zweiten Stufe durch Hydrierung mit einem Katalysator auf der Grundlage eines Borsilikatzeoliths.The invention relates to the production of middle distillates in the boiling range from 180 to 360 ° C on the one hand and an oxidation-stable residue suitable as a base oil for lubricating oils on the other hand by treating mineral oil fractions with a boiling range above 350 ° C in a first stage by hydrocracking and in a second stage Hydrogenation with a catalyst based on a borosilicate zeolite.
Durch die stetige Weiterentwicklung von Motorenölen werden auch immer höhere Anforderungen an die Grundöle, die die Basis für diese Motorenöle bilden, gestellt. Die Herstellung von kraftstoffsparenden Leichtlaufmotorenölen bedingt die Bereitstellung von niedrigviskosen Grundölen, die bei tiefen Temperaturen dünnflüssig sind und somit den Kaltstartverschleiß vermindern, und die bei hohen Temperaturen genügend viskos bleiben, um eine ausreichende Schmierung zu gewährleisten. Eine geringe Abhängigkeit der Viskosität von der Temperatur und damit ein hoher Viskositätsindex (VI) ist daher erforderlich. Weitere wichtige Qualitätsanforderungen an Grundöle stellen die Oxidationsstabilität und eine ausreichende Fluidität bei tiefen Temperaturen dar.Due to the constant further development of engine oils, ever increasing demands are made on the base oils that form the basis for these engine oils. The production of fuel-saving low-viscosity engine oils requires the provision of low-viscosity base oils that are thin at low temperatures and thus reduce cold start wear, and that remain sufficiently viscous at high temperatures to ensure adequate lubrication. A slight dependence of the viscosity on the temperature and therefore a high viscosity index (VI) is necessary. Oxidation stability and sufficient fluidity at low temperatures are further important quality requirements for base oils.
Grundöle mit sehr hohen Viskositätsindices (VHVI [very high viscosity index]-Öle) können durch Hydrocracken von Vakuumgasölen erhalten werden. Hierbei werden Komponenten mit niedrigem VI entweder in leicht siedende Komponenten gespalten oder durch Hydrierung, Ringspaltung sowie Isomerisierung in Verbindungen mit hohem VI umgewandelt.Base oils with very high viscosity indices (VHVI [very high viscosity index] oils) can be obtained by hydrocracking vacuum gas oils. Here, components with low VI are either split into low-boiling components or converted into compounds with high VI by hydrogenation, ring cleavage and isomerization.
Die anschließende Entparaffinierung dient dazu, die Fluidität bei tiefen Temperaturen zu verbessern. Hierbei werden langkettige, unverzweigte und wenig verzweigte Kohlenwasserstoffe abgetrennt. Diese Abtrennung kann zum einen auf physikalischem Wege durch Ausscheiden der Paraffinkristalle bei tiefen Temperaturen unter Verwendung eines Gemisches von Lösungsmitteln oder durch hydrierende Spaltung dieser Verbindungen an formselektiven Katalysatoren erfolgen. Zur Beurteilung der Fluidität wird z.B. die Bestimmung des Pourpoints nach DIN 51 597 angewendet.The subsequent dewaxing serves to improve the fluidity at low temperatures. Long-chain, unbranched and little branched hydrocarbons are separated. This separation can take place physically by precipitating the paraffin crystals at low temperatures using a mixture of solvents or by hydrogenating cleavage of these compounds on shape-selective catalysts. To assess fluidity, e.g. the determination of the pour point according to DIN 51 597 is used.
Die Oxidationsstabilität kann durch eine hydrierende Nachbehandlung des Grundöls oder durch Zugabe von Stabilisatoren eingestellt werden. Die Prüfung kann z.B. nach DIN 51 352 durch die Zunahme des Koksrückstandes nach Conradson nach Alterung mit Durchleiten von Luft erfolgen.The oxidation stability can be adjusted by hydrogenating the base oil or by adding stabilizers. The test can be carried out according to DIN 51 352, for example, by increasing the Conradson coke residue after aging by passing air through it.
In der US-PS 4 347 121 wird ein Verfahren beschrieben, bei dem nacheinander durch Hydrocracken, Hydrofinishing und katalytischem Entparaffinieren Grundöle zur Schmierölherstellung gewonnen werden mit Viskositätsindices von etwa 100, die oxidationsstabil und ausreichend fließfähig bei tiefen Temperaturen sind.US Pat. No. 4,347,121 describes a process in which base oils for the production of lubricating oil are obtained in succession by hydrocracking, hydrofinishing and catalytic dewaxing with viscosity indices of approximately 100 which are stable to oxidation and sufficiently flowable at low temperatures.
Gegenstand der US-PS 4 561 967 ist ein einstufiges, katalytisches Verfahren zur Herstellung von leichten Neutralölen mit guter UV-Stabilität, unter Einsatz von Hydrocrack-Produkten.The subject of US Pat. No. 4,561,967 is a single-stage, catalytic process for the production of light neutral oils with good UV stability, using hydrocracking products.
Die DE-PS 2 613 877 betrifft ein Verfahren zur Herstellung von Schmieröl, bei dem über zwei Hydrocrackstufen und eine katalytische Entparaffinierungsstufe Schmieröle mit niedrigem Pourpoint und einem VI von 95 erhalten werden.DE-PS 2 613 877 relates to a process for the production of lubricating oil in which lubricating oils with a low pour point and a VI of 95 are obtained via two hydrocracking stages and a catalytic dewaxing stage.
Der Viskositätsindex des erhaltenen Grundöls bei all diesen Verfahren ist als nicht ausreichend anzusehen, um aus diesen Grundölen hochwertige Schmieröle herzustellen.The viscosity index of the base oil obtained in all these processes is not sufficient to produce high-quality lubricating oils from these base oils.
Es bestand daher die Aufgabe, ein Verfahren vorzuschlagen, mit dem es gelingt, oxydationsstabile VHVI-Öle herzustellen.It was therefore the task to propose a process with which it is possible to produce oxidation-stable VHVI oils.
Diese Aufgabe wurde gelöst mit einem zweistufigen Verfahren zur Herstellung von oxidationsstabilen Grundölen mit einem VI (Viskositätsindex) 110 bis 135 (VHVI-Öle) und sehr guter Fluidität bei tiefer Temperatur, indem man schwere Mineralölfraktionen mit einem Siedebereich oberhalb vo n 350°C an einem Hydrocrackkatalysator unter Hydrocrackbedingungen zu 20 bis 80 Gew.-% in Anteile konvertiert, die unterhalb 360°C sieden, den Reaktoraustrag gegebenenfalls in einem Hochdruckabscheider in Flüssig- und Gasphase auftrennt, den gesamten Reaktoraustrag oder nur die Flüssigphase, direkt, oder nach Abdestillation der unterhalb 360°C siedenden Anteile in einer zweiten Stufe mit Wasserstoff in Gegenwart eines Katalysators bei 200 bis 450°C und 20 bis 150 bar behandelt, der einen kristallinen Borosilikatzeolith vom Pentasiltyp, Aluminiumoxid und/oder amorphes Alumosilikat als Trägermaterial und ein oder mehrere Metalle aus der Gruppe VIb und/oder Gruppe VIII des Periodensystems und Phosphor enthält, und nach Destillation der Hydrierprodukte ein Mitteldestillat im Siedebereich von 180 bis 360°C mit einem Pourpoint unter -30°C und einen oxidationsstabilen Rückstand mit einem Siedepunkt >360°C, einem Viskositätsindex zwischen 110 und 135 und einem Pourpoint von unter -12°C gewinnt.This object was achieved with a two-stage process for the production of oxidation-stable base oils with a VI (viscosity index) 110 to 135 (VHVI oils) and very good fluidity at low temperature by using heavy mineral oil fractions with a boiling range above 350 ° C on one Hydrocracking catalyst converted under hydrocracking conditions to 20 to 80 wt .-% in portions that boil below 360 ° C, the reactor discharge, if necessary, in a high pressure separator into liquid and gas phase, the entire reactor discharge or only the liquid phase, directly, or after distilling off the bottom 360 ° C boiling in a second stage treated with hydrogen in the presence of a catalyst at 200 to 450 ° C and 20 to 150 bar, which is a crystalline borosilicate zeolite of the pentasil type, aluminum oxide and / or amorphous aluminosilicate as a carrier material and one or more metals from the Group VIb and / or Group VIII of the Periodic Table and Pho sphor contains, and after distillation of the hydrogenation products a middle distillate in the boiling range of 180 to 360 ° C with a pour point below -30 ° C and an oxidation-stable residue with a boiling point> 360 ° C, a viscosity index between 110 and 135 and a pour point of below - Wins 12 ° C.
Die erste Stufe führt man in der Regel bei Drucken von 40 bis 150 bar, Temperaturen von 300 bis 450°C und spezifischen Katalysatorbelastungen von 0,1 bis 4 kg/l x h mit Wasserstoff in Gegenwart eines Katalysators durch, dessen Träger vorzugsweise aus Aluminiumoxid, einem amorphen Alumosilikat und/oder einem dealuminierten Y-Zeolithen zusammengesetzt ist, und der als Hydrierkomponenten ein oder mehrere Metalle aus der Gruppe VI b und/oder VIII des Periodensystems und Phosphor enthält. Der gesamte flüssige Ablauf aus der ersten Stufe wird direkt, ohne Zwischenentspannung, der zweiten Stufe zugeführt oder nach Abdestillieren der unterhalb 360°C siedenden Anteile, bei Drucken von z.B. 20 bis 150 bar, Temperaturen von z.B. 200 bis 450°C und spezifischen Katalysatorbelastungen von 0,1 bis 4 kg/l x h mit Wasserstoff in Gegenwart eines Katalysators behandelt, der einen Borosilikatzeolith vom Pentasiltyp neben Aluminiumoxid und/oder Alumosilikat bzw. Siliciumdioxid enthält. Zur hydrierenden Stabilisierung der Öle sind auf dem Katalysator ein oder mehrere Metalle aus der Gruppe VI b und/oder Gruppe VIII des Periodensystems aufgebracht.The first stage is generally carried out at pressures of 40 to 150 bar, temperatures of 300 to 450 ° C. and specific catalyst loads of 0.1 to 4 kg / lxh with hydrogen in the presence of a catalyst, the support of which is preferably made of aluminum oxide, a amorphous aluminosilicate and / or a dealuminated Y zeolite, and which contains as hydrogenation components one or more metals from group VI b and / or VIII of the periodic table and phosphorus. The entire liquid outflow from the first stage is fed directly to the second stage without intermediate relaxation or after the parts boiling below 360 ° C. have been distilled off, with printing of e.g. 20 to 150 bar, temperatures of e.g. 200 to 450 ° C and specific catalyst loads of 0.1 to 4 kg / l x h treated with hydrogen in the presence of a catalyst which contains a borosilicate zeolite of the pentasil type in addition to aluminum oxide and / or aluminosilicate or silicon dioxide. One or more metals from group VI b and / or group VIII of the periodic table are applied to the catalyst for the hydrogenative stabilization of the oils.
Der VI von 110 bis 135 im Grundöl mit einem Siedepunkt >360°C wird mittels unterschiedlicher Konversionsgrade in der ersten Stufe eingestellt. Der Konversionsgrad ist der Quotient aus dem unterhalb 360°C siedenden Anteil und dem gesamten Kohlenwasserstoffanteil. In der 2. Stufe werden die Reaktionsbedingungen (Druck, Temperatur und spezifische Katalysatorbelastung) so gewählt, daß das resultierende Grundöl mit einem Siedebeginn oberhalb von 360°C, oxidationsstabil ist und einen Pourpoint von unter -12°C aufweist.The VI from 110 to 135 in base oil with a boiling point> 360 ° C is set in the first stage using different degrees of conversion. The degree of conversion is the quotient of the portion boiling below 360 ° C and the total hydrocarbon portion. In the second stage, the reaction conditions (pressure, temperature and specific catalyst load) are selected so that the resulting base oil with a start of boiling above 360 ° C is stable to oxidation and has a pour point below -12 ° C.
Ein weiterer überraschender Vorteil des erfindungsgemäßen Verfahrens ist der Befund, daß die verfahrensgemäßen Grundöle besser als Grundöle, die mit Lösungsmitteln entparaffiniert wurden, auf Pourpointverbesserer ansprechen.A further surprising advantage of the method according to the invention is the finding that the base oils according to the method respond better to pour point improvers than base oils which have been dewaxed with solvents.
Daneben besitzen die bei diesem Verfahren anfallenden Mitteldestillate mit einem im Siedebereich von 180 bis 360°C, hervorragende Kälteeigenschaften. Der Pourpoint liegt stets unterhalb von -30°C. Solche Mitteldestillate sind wertvolle Mischkomponenten zur Herstellung von kältestabilen Dieselkraftstoffen.In addition, the middle distillates obtained in this process, with a boiling range of 180 to 360 ° C, have excellent cooling properties. The pour point is always below -30 ° C. Such middle distillates are valuable mixed components for the production of low-temperature diesel fuels.
Die Herstellung von Katalysatoren für die Hydrocrackstufe des erfindungsgemäßen Verfahrens kann durch Mischen einer Aluminiumoxidkomponente mit einer Siliciumoxidkomponente oder einem Alumosilikat, gegebenenfalls unter Zusatz eines dealuminierten Zeolithen vom Y-Typ mit einem SiO₂/Al₂O₃-Molverhältnis im Bereich von 7 bis 150 und einem Peptisierungsmittel, wie z.B. Ameisensäure, erfolgen. Als SiO₂-Komponente eignet sich besonders ein Hydrogel mit einem SiO₂-Gehalt von 10 bis 20 Gew.-%, charakteristischen Banden im IR-Spektrum bei Wellenzahlen von 1 630 und 960 cm⁻¹, einem Na-Gehalt von unter 0.01 Gew.-% und einer BET-Oberfläche von oberhalb 400 m²/g. Die Dealuminierung des Y-Zeolithen kann durch Säurebehandlung z.B. nach der DE-PS 2 435 716 erfolgen. An amorphen Trägeranteilen können 20 bis 95 Gew.-% Aluminiumoxid, bevorzugt 30 bis 60 Gew.-% sowie 5 bis 50 Gew.-% Siliciumdioxid, bevorzugt 20 bis 40 Gew.-% eingesetzt werden. Der Gewichtsanteil an dealuminiertem Y-Zeolith im Träger kann im Bereich 0 bis 30 variiert werden. Nach intensivem Mischen wird die Paste durch eine Matrize mit einem Durchmesser zwischen 1 und 3 mm extrudiert und anschließend getrocknet und bei erhöhten Temperaturen calciniert.The preparation of catalysts for the hydrocracking stage of the process according to the invention can be carried out by mixing an aluminum oxide component with a silicon oxide component or an aluminosilicate, optionally with the addition of a dealuminated zeolite of the Y type with an SiO₂ / Al₂O₃ molar ratio in the range from 7 to 150 and a peptizing agent, such as for example formic acid. As a SiO₂ component, a hydrogel with a SiO₂ content of 10 to 20% by weight is particularly suitable Bands in the IR spectrum at wavenumbers of 1,630 and 960 cm ,¹, a Na content of less than 0.01% by weight and a BET surface area of more than 400 m² / g. The dealumination of the Y zeolite can be carried out by acid treatment, for example according to DE-PS 2 435 716. 20 to 95% by weight of aluminum oxide, preferably 30 to 60% by weight and 5 to 50% by weight of silicon dioxide, preferably 20 to 40% by weight, can be used in amorphous carrier fractions. The weight fraction of dealuminated Y zeolite in the carrier can be varied in the range from 0 to 30. After intensive mixing, the paste is extruded through a die with a diameter between 1 and 3 mm and then dried and calcined at elevated temperatures.
Die Trägerzusammensetzung des in der 2. Stufe, der Entparaffinierungs- und Stabilisierungsstufe, des erfindungsgemäßen Verfahrens eingesetzten Katalysators kann zweckmäßig variieren im Bereich 10 bis 90 Gew.-% Borzeolith vom Pentasiltyp, 10 bis 90 Gew.-% Aluminiumoxid und 20 bis 40 Gew.-% Siliciumoxid.The carrier composition of the catalyst used in the second stage, the dewaxing and stabilization stage, of the process according to the invention can expediently vary in the range from 10 to 90% by weight of boron zeolite of the pentasil type, 10 to 90% by weight of aluminum oxide and 20 to 40% by weight. -% silicon oxide.
Die verwendeten Borosilikatzeolithe vom Pentasiltyp sind durch ein hohes SiO₂/B₂O₃-Verhältnis gekennzeichnet sowie durch Porengrößen, die zwischen denen der Zeolithe vom Typ A und denen vom Typ X oder Y liegen. Sie werden z.B. bei 90 bis 200°C unter autogenem Druck synthetisiert, indem man eine Borverbindung z.B. H₃BO₃ mit einer Siliciumverbindung, vorzugsweise hochdispersem Siliciumdioxid in wäßriger Aminlösung, insbesondere in 1,6-Hexandiamin- oder 1,3-Propandiamin- oder Triethylentetramin-Lösung mit und insbesondere ohne Alkali- oder Erdalkalizusatz zur Reaktion bringt. Hierzu gehören auch die isotaktischen Zeolithe nach EP-A-34 727 und EP-A-46 504. Solche Borosilikatzeolithe können ebenfalls hergestellt werden, wenn man die Reaktion statt in wäßriger Aminlösung in etherischer Lösung, z.B. Diethylenglykoldimethylether oder in alkoholischer Lösung, z.B. 1,6-Hexandiol durchführt. Wesentlich und besonders vorteilhaft ist die Synthese der Borosilikatzeolithe in wäßriger Polyamin-Lösung ohne Zusatz von Alkali. Die so hergestellten Zeolithe können nach ihrer Isolierung, Trocknung bei 100°C bis 160°C, vorzugsweise 110°C und Calcinierung bei 450 bis 550°C, vorzugsweise 500°C, zusammen mit den anderen Trägermaterialien verformt werden.The borosilicate zeolites of the pentasil type are characterized by a high SiO₂ / B₂O₃ ratio and by pore sizes between those of type A zeolites and those of type X or Y. You will e.g. synthesized at 90 to 200 ° C under autogenous pressure by using a boron compound e.g. H₃BO₃ with a silicon compound, preferably highly disperse silicon dioxide in aqueous amine solution, in particular in 1,6-hexanediamine or 1,3-propanediamine or triethylenetetramine solution with and in particular without addition of alkali or alkaline earth metal to the reaction. These also include the isotactic zeolites according to EP-A-34 727 and EP-A-46 504. Such borosilicate zeolites can also be prepared if the reaction is carried out in ethereal solution, e.g. Diethylene glycol dimethyl ether or in alcoholic solution, e.g. 1,6-hexanediol. The synthesis of borosilicate zeolites in aqueous polyamine solution without the addition of alkali is essential and particularly advantageous. After their isolation, drying at 100 ° C. to 160 ° C., preferably 110 ° C. and calcination at 450 to 550 ° C., preferably 500 ° C., the zeolites thus produced can be shaped together with the other carrier materials.
Die Hydrierkomponenten für die Katalysatoren in beiden Stufen des erfindungsgemäßen Verfahrens können in das feuchte Trägergemisch eingearbeitet und/oder durch Auftränken auf den Katalysatorträger aufgebracht werden. Die Katalysatorteilchen werden hierzu z.B. mit einer Lösung, die die gewünschten Hydrierkomponenten enthält, ein- oder mehrmals in Berührung gebracht. Die Lösungsmenge entspricht der zuvor bestimmten Wasseraufnahme der Katalysatorteilchen. An Hydriermetallkomponenten werden bevorzugt Co, Ni, Mo, und W, z.B. in Form von Ammoniumheptamolybdat, Nickelnitrat, Ammoniummetawolframat, Cobaltnitrat eingesetzt. Der fertige Katalysator wird nach erneuter Trocknung und Calcinierung erhalten und kann 2 bis 10 Gew.-% Nickel- bzw. Cobaltoxid und 10 bis 25 Gew.-% Molybdän bzw. Wolfram, berechnet als MoO₃ und WO₃ enthalten. Den Katalysatoren können auch Phosphorkomponenten und zwar sowohl beim Mischen der Trägerkomponenten als auch als Bestandteil der Tränklösung beigemengt werden. Gewöhnlich werden hierbei Mengen im Bereich 1 bis 12 Gew.-% P₂O₅ bezogen auf den fertigen Katalysator zugesetzt.The hydrogenation components for the catalysts in both stages of the process according to the invention can be incorporated into the moist carrier mixture and / or applied to the catalyst carrier by impregnation. For this purpose, the catalyst particles are brought into contact, for example, one or more times with a solution which contains the desired hydrogenation components. The amount of solution corresponds to the previously determined water absorption of the catalyst particles. On hydrogenation metal components preferably Co, Ni, Mo, and W, for example in the form of ammonium heptamolybdate, nickel nitrate, ammonium metatungstate, cobalt nitrate. The finished catalyst is obtained after renewed drying and calcination and can contain 2 to 10 wt .-% nickel or cobalt oxide and 10 to 25 wt .-% molybdenum or tungsten, calculated as MoO₃ and WO₃. Phosphorus components can also be added to the catalysts, both when the carrier components are mixed and as part of the impregnation solution. Amounts in the range of 1 to 12% by weight of P₂O₅ based on the finished catalyst are usually added.
Vor der Verwendung der Katalysatoren werden diese durch Schwefelung von der oxidischen in die aktivere sulfidische Form, z.B. durch Überleiten eines Gemisches aus Wasserstoff und H₂S, umgewandelt.Before using the catalysts, they are sulfurized from the oxidic to the more active sulfidic form, e.g. by passing a mixture of hydrogen and H₂S converted.
Geeignete Einsatzstoffe für das Verfahren sind schwere Gasöle, Vakuumgasöle, entasphaltierte Rückstandöle und Mischungen davon im Siedebereich oberhalb 350°C. Ein vorheriger Abbau der organischen Schwefel- und Stickstoffverbindungen ist nicht erforderlich, jedoch in bestimmten Fällen von Vorteil.Suitable feedstocks for the process are heavy gas oils, vacuum gas oils, deasphalted residue oils and mixtures thereof in the boiling range above 350 ° C. A prior breakdown of the organic sulfur and nitrogen compounds is not necessary, but is advantageous in certain cases.
Im einzelnen geht man zweckmäßig so vor, daß der Einsatzstoff zusammen mit Wasserstoff auf den Hydrocrackreaktor gegeben und auf Reaktionstemperatur gebracht wird. Die Konversionsrate für eine Siedetemperatur <360°C wird zwischen 20 und 80 % eingestellt. Das Effluent aus dem Hydrocrackreaktor wird in einem Hochdruckabscheider in Flüssig- und Gasphase aufgetrennt. Ammoniak und Schwefelwasserstoff, die in der Gasphase enthalten sind, werden gegebenenfalls in einer nachgeschalteten Wäsche abgetrennt, und der Wasserstoff in die Reaktionszone zurückgeführt. Der Flüssiganteil wird auf gleichem Druckniveau dem zweiten Reaktor zugeführt, wo die Entparaffinierung sowie die hydrierende Stabilisierung erfolgt. Liegt der Schwefelgehalt im Flüssiganteil unterhalb von 100 mg/kg, so ist vor dem Eintritt in den zweiten Reaktor die Zugabe einer Schwefelkomponenten, z.B. Dimethyldisulfid (DMDS), erforderlich, um eine Entschwefelung des Katalysators zu verhindern. Das Effluent aus dem zweiten Reaktor wird nach der Abtrennung der Gasphase in einem weiteren Hochdruckabscheider in einer nachgeschalteten Destillation aufgetrennt in Flüssiggas, Naphtha, Mitteldestillat und einen Rückstand mit einem Siedepunkt >360°C. Dieser Rückstand eignet sich aufgrund seines Viskositätsindexes zwischen 110 bis 135, seiner Oxidationsstabilität und seines Pourpoints unterhalb -12°C, hervorragend als Grundöl zur Herstellung von hochwertigen Schmierölen. Weiter wurde festgestellt, daß die nach dem erfindungsgemäßen Verfahren erhaltenen Grundöle sehr viel besser als z.B. mit Lösungsmitteln entparaffinierte Grundöle auf Pourpointsverbesserer ansprechen. Es werden nicht nur geringere Mengen an Pourpointsverbesserer benötigt, um einen vorgegebenen Pourpoint einzustellen, sondern auch tiefer liegende Pourpoints erreicht, als sie nach herkömmlichen Verfahren möglich waren.In detail, the procedure is appropriately such that the feed is added to the hydrocracking reactor together with hydrogen and brought to the reaction temperature. The conversion rate for a boiling temperature <360 ° C is set between 20 and 80%. The effluent from the hydrocracking reactor is separated into a liquid and gas phase in a high pressure separator. Ammonia and hydrogen sulfide, which are contained in the gas phase, are optionally separated in a downstream wash, and the hydrogen is returned to the reaction zone. The liquid portion is fed to the second reactor at the same pressure level, where dewaxing and hydrating stabilization take place. If the sulfur content in the liquid fraction is below 100 mg / kg, the addition of a sulfur component, for example dimethyl disulfide (DMDS), is necessary before entering the second reactor in order to prevent desulfurization of the catalyst. After the separation of the gas phase, the effluent from the second reactor is separated in a further high-pressure separator in a downstream distillation into liquid gas, naphtha, middle distillate and a residue with a boiling point> 360 ° C. Due to its viscosity index between 110 and 135, its oxidation stability and its pour point below -12 ° C, this residue is ideal as a base oil for the production of high-quality lubricating oils. It was also found that the base oils obtained by the process according to the invention respond much better to pour point improvers than, for example, base oils dewaxed with solvents. It won't just be requires smaller amounts of pour point improver to set a given pour point, but also reaches lower-lying pour points than was possible using conventional methods.
Da nach dem vorliegenden Verfahren die Mitteldestillate im Siedebereich 180 bis 360°C, erst nach der Entparaffinierungsstufe abgetrennt werden, resultieren hieraus hervorragende Kälteeigenschaften für diese Mitteldestillate. Mit einem Pourpoint von < -30°C erfüllen die Destillate auch extreme Anfoderungen, z.B. für Dieselkraftstoff im Winterbetrieb.Since the middle distillates in the boiling range 180 to 360 ° C are only separated after the dewaxing stage, this results in excellent cold properties for these middle distillates. With a pour point of <-30 ° C, the distillates also meet extreme requirements, e.g. for diesel fuel in winter operation.
Die Verfahrensbedingungen für beide katalytische Stufen können in der Regel innerhalb folgender Bereiche variiert werden:
Herstellung des Katalysators für die Hydrocrackstufe:Preparation of the catalyst for the hydrocracking stage:
Ein feuchtes Trägergemisch wird durch Mischen von 227 g Hydrogel (SiO₂-Gehalt 15 %) mit 102 g Aluminiumoxid und 10 g Ameisensäure unten Zusatz von 18 g Phosphorsäure, 16,2 g Nickelnitrat und 309 g Ammoniumheptamolybdat gelöst in 150 ml Wasser, hergestellt. Das Trägergemisch wird durch eine 1,5 mm Matrize extrudiert, anschließend bei 150°C getrocknet und 5 Stunden bei 500°C calciniert. Die Formkörper werden mit einer Lösung, bestehend aus Nickelnitrat und Ammoniumheptamolybdat imprägniert und erneut getrocknet und calciniert. Der fertige Katalysator weist folgende Zusammensetzung auf (Gew.-%): Al₂O₃ 51, SiO₂ 17, MoO₃ 18, NiO 5, [PO₄]³⁻9.A moist carrier mixture is prepared by mixing 227 g of hydrogel (SiO₂ content 15%) with 102 g of aluminum oxide and 10 g of formic acid, adding 18 g of phosphoric acid, 16.2 g of nickel nitrate and 309 g of ammonium heptamolybdate dissolved in 150 ml of water. The carrier mixture is extruded through a 1.5 mm die, then dried at 150 ° C. and calcined at 500 ° C. for 5 hours. The moldings are impregnated with a solution consisting of nickel nitrate and ammonium heptamolybdate and dried and calcined again. The finished catalyst has the following composition (wt .-%): Al₂O₃ 51, SiO₂ 17, MoO₃ 18, NiO 5, [PO₄] ³⁻9.
Herstellung des Katalysators für die Entparaffinierung und hydrierende Stabilisierung:
Synthese des Borosilikatzeolithen:Preparation of the dewaxing and hydrating stabilization catalyst:
Synthesis of borosilicate zeolite:
Ein Borosilikatzeolith des Pentasil-Typs wird in einer hydrothermalen Synthese aus 640 g hochdispersem SiO₂, 122 g H₃BO₃, 8000 g einer wäßrigen 1,6-Hexandiamin-Lösung (Mischung 50:50 Gew.-%) bei 170°C unter autogenem Druck in einem Rührautoklaven ohne Alkalizusatz hergestellt. Nach Abfiltrieren und Auswaschen wird das kristalline Reaktionsprodukt bei 100°C/24 h getrocknet und bei 500°C/24 h calciniert. Dieser Borosilikatzeolith setzt sich zusammen aus 94,2 Gew.-% SiO₂ und 2,3 Gew.-% B₂O₃ (Glühverlust: 3,5 Gew.-%).A borosilicate zeolite of the pentasil type is in a hydrothermal synthesis from 640 g of highly disperse SiO₂, 122 g of H₃BO₃, 8000 g of an aqueous 1,6-hexanediamine solution (mixture 50:50 wt .-%) at 170 ° C under autogenous pressure in a stirred autoclave without added alkali. After filtering off and washing out, the crystalline reaction product is dried at 100 ° C./24 h and calcined at 500 ° C./24 h. This borosilicate zeolite is composed of 94.2 wt .-% SiO₂ and 2.3 wt .-% B₂O₃ (loss on ignition: 3.5 wt .-%).
Die Herstellung des Katalysators erfolgte wie bei Beispiel 1 beschrieben unter Zusatz des Borosilikatzeolithen. Der fertige Katalysator wies folgende Zusammensetzung auf (Gew.-%): Al₂O₃=18, Borpentasilzeolith=60, MoO₃=18, NiO=4The catalyst was prepared as described in Example 1 with the addition of the borosilicate zeolite. The finished catalyst had the following composition (% by weight): Al₂O₃ = 18, boron pentasil zeolite = 60, MoO₃ = 18, NiO = 4
Für das hier angeführte Beispiel wurde ein Vakuumgasöl aus Amna/Sahara mit folgenden Eigenschaften eingesetzt:
- Dichte 15°C
- 0,894 g/ml
- Viskosität 70°C
- 14,6 mm²/s
- Pourpoint
- 40°C
- Schwefelgehalt
- 0,34 Gew.-%
- Stickstoffgehalt
- 0,081 Gew.-%
- C aromatisch n. Brandes
- 16,5 Gew.-%
Siedeverlauf ASTM D 1160
- SB
- 260°C
- 10 Vol.-%
- 373°C
- 30 Vol.-%
- 432°C
- 50 Vol.-%
- 455°C
- 70 Vol.-%
- 480°C
- 90 Vol.-%
- 516°C
- SE
- 548°C
- Density 15 ° C
- 0.894 g / ml
- Viscosity 70 ° C
- 14.6 mm² / s
- Pour point
- 40 ° C
- Sulfur content
- 0.34% by weight
- Nitrogen content
- 0.081% by weight
- C aromatic after fire
- 16.5% by weight
Boiling curve ASTM D 1160
- SB
- 260 ° C
- 10 vol .-%
- 373 ° C
- 30 vol .-%
- 432 ° C
- 50 vol .-%
- 455 ° C
- 70 vol .-%
- 480 ° C
- 90 vol .-%
- 516 ° C
- SE
- 548 ° C
Nach der Hydrocrackstufe wurden in einem Hochdruckabscheider die gasförmigen Bestandteile abgetrennt und die gesamten flüssigen Anteile der Entparaffinierungsstufe zugeführt.After the hydrocracking stage, the gaseous constituents were separated off in a high-pressure separator and the entire liquid portions were fed to the dewaxing stage.
- H2S + NH3H2S + NH3
- 0,50.5
- C1 + C2C1 + C2
- 1,01.0
- C3 + C4C3 + C4
- 12,212.2
- C5 - 80°CC5 - 80 ° C
- 15,715.7
- 80 - 180°C80-180 ° C
- 11,211.2
- 180 - 360°C180 - 360 ° C
- 26,326.3
- > 360°C> 360 ° C
- 35,235.2
Mitteldestillat 180 - 360°C
- Dichte 15°C
- 0,842 g/ml
- Cetanindex
- 51
- Pourpoint
- - 42°C
- C aromatisch n. Brandes
- 9,5 Gew.-%
Fraktion > 360°C
- Dichte 15°C
- 0,846 g/ml
- Pourpoint
- - 13 °C
- Viskosität 100°C
- 4,8 mm2/s
- Viskositätsindex
- 119
- Zunahme des Koksrückstands
- < 1,2 %
nach DIN 51 352Middle distillate 180 - 360 ° C
- Density 15 ° C
- 0.842 g / ml
- Cetane index
- 51
- Pour point
- - 42 ° C
- C aromatic after fire
- 9.5% by weight
Fraction> 360 ° C
- Density 15 ° C
- 0.846 g / ml
- Pour point
- - 13 ° C
- Viscosity 100 ° C
- 4.8 mm2 / s
- Viscosity index
- 119
- Increase in coke residue
- <1.2%
according to DIN 51 352
Claims (6)
- A process for the preparation of a base oil and middle distillate which is stable to oxidation and low temperatures from a mineral oil fraction having a boiling range above 350°C, which comprises, in a first step, converting the mineral oil fraction, by means of hydrogen in the presence of a catalyst which has a support composed of aluminium oxide, an amorphous alumosilicate and/or a dealuminated Y zeolite, and which contains, as hydrogenating components, one or more metals from group VIb and/or VIII of the Periodic Table and phosphorus, at from 300 to 450°C and at from 40 to 150 bar, to an extent of from 20 to 80% by weight into fractions which boil below 360°C, separating the reactor effluent, if necessary, into liquid and gas phases in a high-pressure separator, treating the entire reactor effluent or only the liquid phase, directly or after removal of the fractions boiling below 360°C by distillation, in a second step with hydrogen at from 200 to 450°C and at from 20 to 150 bar in the presence of a catalyst which contains a crystalline pentasil-type borosilicate zeolite, alumina and/or amorphous alumosilicate as the carrier material and one or more metals from Group VIb and/or Group VIII of the Periodic Table and phosphorus, and, after distillation of the hydrogenation product, obtaining a middle distillate in the boiling range from 180 to 360°C having a pour point of below -30°C and an oxidation-stable residue having a boiling point >360°C, a viscosity index of from 110 to 135 and a pour point of below -12°C.
- A process as claimed in claim 1, wherein the hydrocracking catalyst contains from 1 to 40% by weight of dealuminated Y zeolite having an SiO₂:Al₂O₃ molar ratio in the range from 7 to 150.
- A process as claimed in claim 1, wherein the proportion of crystalline borosilicate zeolite in the catalyst in the second step is from 1 to 90% by weight.
- A process as claimed in claim 3, wherein the SiO₂ component in the borosilicate zeolite is a hydrogel having an SiO₂ content of from 10 to 20% by weight, characteristic bands in the IR spectrum at wave numbers of 1630 and 960 cm⁻¹, a sodium content of less than 0.01% by weight and a BET surface area of >400 m²/g.
- A process as claimed in claim 1, wherein the entire reactor effluent from the hydrocracking step, comprising liquid and gas phases, is fed to the 2nd step.
- The use of a residue obtained as claimed in claim 1 having a boiling point >360°C as a base oil for the preparation of high-quality lubricant oils.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE4003175A DE4003175A1 (en) | 1990-02-03 | 1990-02-03 | Oxidn.- and cold-stable middle distillates prodn. - from mineral oil fractions by hydrocracking using hydrocracking catalyst and hydrotreating using borosilicate pentasil zeolite |
DE4003175 | 1990-02-03 |
Publications (2)
Publication Number | Publication Date |
---|---|
EP0441195A1 EP0441195A1 (en) | 1991-08-14 |
EP0441195B1 true EP0441195B1 (en) | 1994-03-16 |
Family
ID=6399334
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP91100942A Expired - Lifetime EP0441195B1 (en) | 1990-02-03 | 1991-01-25 | Process for the preparation of base oils and middle distillates stabilized against oxydation and low temperatures |
Country Status (5)
Country | Link |
---|---|
US (1) | US5143595A (en) |
EP (1) | EP0441195B1 (en) |
JP (1) | JPH051290A (en) |
DE (2) | DE4003175A1 (en) |
ES (1) | ES2050462T3 (en) |
Families Citing this family (14)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5271828A (en) * | 1992-03-16 | 1993-12-21 | Amoco Corporation | Distillate hydrogenation |
CN1034586C (en) * | 1993-11-05 | 1997-04-16 | 中国石油化工总公司 | Catalytic conversion method of low-carbon olefines high-output |
JP3424053B2 (en) * | 1994-09-02 | 2003-07-07 | 新日本石油株式会社 | Method for producing low sulfur low aromatic gas oil |
US5855767A (en) * | 1994-09-26 | 1999-01-05 | Star Enterprise | Hydrorefining process for production of base oils |
ATE232416T1 (en) * | 1998-02-06 | 2003-02-15 | Kataleuna Gmbh Catalysts | CATALYST FOR HYDROGENATION OF AROMATICS IN SULFUR CONTAINING HYDROCARBON FRACTIONS |
FR2777290B1 (en) * | 1998-04-09 | 2000-05-12 | Inst Francais Du Petrole | METHOD FOR IMPROVING THE CETANE INDEX OF A GASOIL CUT |
JP2000269678A (en) * | 1999-03-16 | 2000-09-29 | Matsushita Electric Ind Co Ltd | High-frequency device |
US6635170B2 (en) | 2000-12-14 | 2003-10-21 | Exxonmobil Research And Engineering Company | Hydroprocessing process with integrated interstage stripping |
FR2852865B1 (en) * | 2003-03-24 | 2007-02-23 | Inst Francais Du Petrole | CATALYST AND USE THEREOF FOR IMPROVING THE FLOW POINT OF HYDROCARBON LOADS |
FR2852863B1 (en) * | 2003-03-24 | 2005-05-06 | Inst Francais Du Petrole | CATALYST AND USE THEREOF FOR IMPROVING THE FLOW POINT OF HYDROCARBON LOADS |
US20040256286A1 (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 |
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 |
JP5105557B2 (en) * | 2010-04-26 | 2012-12-26 | 東燃ゼネラル石油株式会社 | Lubricating oil composition for internal combustion engines |
DE202011052210U1 (en) | 2011-12-06 | 2012-12-19 | M. Schall Gmbh + Co. Kg. | Ventilation device for clean rooms and clean room with such a device |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2306254A1 (en) * | 1975-04-02 | 1976-10-29 | Shell France | PROCESS FOR PREPARING A LUBRICATING OIL |
US4347121A (en) * | 1980-10-09 | 1982-08-31 | Chevron Research Company | Production of lubricating oils |
US4561967A (en) * | 1981-04-23 | 1985-12-31 | Chevron Research Company | One-step stabilizing and dewaxing of lube oils |
US4921594A (en) * | 1985-06-28 | 1990-05-01 | Chevron Research Company | Production of low pour point lubricating oils |
DE3701570A1 (en) * | 1987-01-21 | 1988-08-04 | Basf Ag | METHOD FOR PRODUCING MEDIUM DISTILLATES WITH IMPROVED COLD PROPERTIES |
-
1990
- 1990-02-03 DE DE4003175A patent/DE4003175A1/en not_active Withdrawn
-
1991
- 1991-01-25 ES ES91100942T patent/ES2050462T3/en not_active Expired - Lifetime
- 1991-01-25 DE DE91100942T patent/DE59101172D1/en not_active Expired - Lifetime
- 1991-01-25 EP EP91100942A patent/EP0441195B1/en not_active Expired - Lifetime
- 1991-02-01 JP JP3012203A patent/JPH051290A/en not_active Withdrawn
- 1991-02-01 US US07/654,883 patent/US5143595A/en not_active Expired - Fee Related
Also Published As
Publication number | Publication date |
---|---|
DE4003175A1 (en) | 1991-08-08 |
EP0441195A1 (en) | 1991-08-14 |
ES2050462T3 (en) | 1994-05-16 |
DE59101172D1 (en) | 1994-04-21 |
JPH051290A (en) | 1993-01-08 |
US5143595A (en) | 1992-09-01 |
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