CN115404102A - Transformer oil base oil and preparation method thereof - Google Patents
Transformer oil base oil and preparation method thereof Download PDFInfo
- Publication number
- CN115404102A CN115404102A CN202211164676.5A CN202211164676A CN115404102A CN 115404102 A CN115404102 A CN 115404102A CN 202211164676 A CN202211164676 A CN 202211164676A CN 115404102 A CN115404102 A CN 115404102A
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- CN
- China
- Prior art keywords
- oil
- catalyst
- metal oxide
- hydrodewaxing
- catalyst carrier
- 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.)
- Pending
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- 239000003921 oil Substances 0.000 title claims abstract description 156
- 239000002199 base oil Substances 0.000 title claims abstract description 77
- 238000002360 preparation method Methods 0.000 title claims abstract description 54
- 239000003054 catalyst Substances 0.000 claims abstract description 157
- 238000002156 mixing Methods 0.000 claims abstract description 40
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 36
- 239000001257 hydrogen Substances 0.000 claims abstract description 36
- 238000007670 refining Methods 0.000 claims abstract description 29
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 26
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims abstract description 20
- 230000009471 action Effects 0.000 claims abstract description 16
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 13
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 12
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims abstract description 12
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 12
- 239000011593 sulfur Substances 0.000 claims abstract description 12
- 229910044991 metal oxide Inorganic materials 0.000 claims description 56
- 150000004706 metal oxides Chemical class 0.000 claims description 47
- 238000000034 method Methods 0.000 claims description 42
- 238000001035 drying Methods 0.000 claims description 28
- 238000006243 chemical reaction Methods 0.000 claims description 26
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 25
- 230000008569 process Effects 0.000 claims description 24
- 150000002431 hydrogen Chemical class 0.000 claims description 23
- 239000012752 auxiliary agent Substances 0.000 claims description 21
- 229910001868 water Inorganic materials 0.000 claims description 21
- 238000004519 manufacturing process Methods 0.000 claims description 20
- 239000002808 molecular sieve Substances 0.000 claims description 19
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 19
- 238000005984 hydrogenation reaction Methods 0.000 claims description 15
- 229910052751 metal Inorganic materials 0.000 claims description 15
- 239000002184 metal Substances 0.000 claims description 15
- 239000002994 raw material Substances 0.000 claims description 14
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 13
- 238000005553 drilling Methods 0.000 claims description 13
- 239000012530 fluid Substances 0.000 claims description 13
- 239000000314 lubricant Substances 0.000 claims description 13
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 12
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 11
- VXAUWWUXCIMFIM-UHFFFAOYSA-M aluminum;oxygen(2-);hydroxide Chemical compound [OH-].[O-2].[Al+3] VXAUWWUXCIMFIM-UHFFFAOYSA-M 0.000 claims description 11
- 239000003795 chemical substances by application Substances 0.000 claims description 11
- 229910052698 phosphorus Inorganic materials 0.000 claims description 11
- 239000011574 phosphorus Substances 0.000 claims description 11
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 claims description 10
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 10
- ZOXJGFHDIHLPTG-UHFFFAOYSA-N Boron Chemical compound [B] ZOXJGFHDIHLPTG-UHFFFAOYSA-N 0.000 claims description 9
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 claims description 9
- ZMANZCXQSJIPKH-UHFFFAOYSA-N Triethylamine Chemical compound CCN(CC)CC ZMANZCXQSJIPKH-UHFFFAOYSA-N 0.000 claims description 9
- -1 VIB group metal oxide Chemical class 0.000 claims description 9
- QCWXUUIWCKQGHC-UHFFFAOYSA-N Zirconium Chemical compound [Zr] QCWXUUIWCKQGHC-UHFFFAOYSA-N 0.000 claims description 9
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 9
- 229910052796 boron Inorganic materials 0.000 claims description 9
- 125000000753 cycloalkyl group Chemical group 0.000 claims description 9
- 238000001125 extrusion Methods 0.000 claims description 9
- 229910052731 fluorine Inorganic materials 0.000 claims description 9
- 239000011737 fluorine Substances 0.000 claims description 9
- 239000000047 product Substances 0.000 claims description 9
- 229910052726 zirconium Inorganic materials 0.000 claims description 9
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 8
- 125000005842 heteroatom Chemical group 0.000 claims description 8
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 claims description 8
- 239000010936 titanium Substances 0.000 claims description 8
- 229910052719 titanium Inorganic materials 0.000 claims description 8
- ZNOKGRXACCSDPY-UHFFFAOYSA-N tungsten trioxide Chemical compound O=[W](=O)=O ZNOKGRXACCSDPY-UHFFFAOYSA-N 0.000 claims description 8
- 239000000654 additive Substances 0.000 claims description 7
- 239000002002 slurry Substances 0.000 claims description 7
- KGBXLFKZBHKPEV-UHFFFAOYSA-N boric acid Chemical compound OB(O)O KGBXLFKZBHKPEV-UHFFFAOYSA-N 0.000 claims description 6
- 239000004327 boric acid Substances 0.000 claims description 6
- 238000007598 dipping method Methods 0.000 claims description 6
- 239000012065 filter cake Substances 0.000 claims description 6
- 239000012452 mother liquor Substances 0.000 claims description 6
- 238000012545 processing Methods 0.000 claims description 6
- 239000000243 solution Substances 0.000 claims description 6
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 5
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 claims description 5
- 239000011230 binding agent Substances 0.000 claims description 5
- 239000000706 filtrate Substances 0.000 claims description 5
- 229910000480 nickel oxide Inorganic materials 0.000 claims description 5
- GNRSAWUEBMWBQH-UHFFFAOYSA-N oxonickel Chemical compound [Ni]=O GNRSAWUEBMWBQH-UHFFFAOYSA-N 0.000 claims description 5
- RMAQACBXLXPBSY-UHFFFAOYSA-N silicic acid Chemical compound O[Si](O)(O)O RMAQACBXLXPBSY-UHFFFAOYSA-N 0.000 claims description 5
- 239000000126 substance Substances 0.000 claims description 5
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 claims description 4
- 239000004530 micro-emulsion Substances 0.000 claims description 4
- 238000000465 moulding Methods 0.000 claims description 4
- 150000003839 salts Chemical class 0.000 claims description 4
- 239000000377 silicon dioxide Substances 0.000 claims description 4
- 239000007787 solid Substances 0.000 claims description 4
- 238000005406 washing Methods 0.000 claims description 4
- 230000000996 additive effect Effects 0.000 claims description 3
- 239000002671 adjuvant Substances 0.000 claims description 3
- 238000001914 filtration Methods 0.000 claims description 3
- 239000012266 salt solution Substances 0.000 claims description 3
- 150000001875 compounds Chemical class 0.000 claims description 2
- 238000000748 compression moulding Methods 0.000 claims description 2
- 239000004064 cosurfactant Substances 0.000 claims description 2
- 239000010413 mother solution Substances 0.000 claims description 2
- 239000002904 solvent Substances 0.000 claims description 2
- 239000004094 surface-active agent Substances 0.000 claims description 2
- 244000275012 Sesbania cannabina Species 0.000 claims 1
- 238000009833 condensation Methods 0.000 abstract description 8
- 230000005494 condensation Effects 0.000 abstract description 7
- 125000004435 hydrogen atom Chemical class [H]* 0.000 abstract 3
- 230000000052 comparative effect Effects 0.000 description 11
- 238000005516 engineering process Methods 0.000 description 9
- 239000000843 powder Substances 0.000 description 9
- 241000219782 Sesbania Species 0.000 description 7
- 238000005194 fractionation Methods 0.000 description 7
- 239000011148 porous material Substances 0.000 description 7
- 230000000881 depressing effect Effects 0.000 description 6
- KBJMLQFLOWQJNF-UHFFFAOYSA-N nickel(ii) nitrate Chemical compound [Ni+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O KBJMLQFLOWQJNF-UHFFFAOYSA-N 0.000 description 6
- 238000000746 purification Methods 0.000 description 6
- 239000004927 clay Substances 0.000 description 5
- 238000002791 soaking Methods 0.000 description 5
- 238000005303 weighing Methods 0.000 description 5
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 4
- 239000000853 adhesive Substances 0.000 description 4
- 230000001070 adhesive effect Effects 0.000 description 4
- HYBBIBNJHNGZAN-UHFFFAOYSA-N furfural Chemical compound O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 229910017604 nitric acid Inorganic materials 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 238000012360 testing method Methods 0.000 description 4
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 3
- 150000001336 alkenes Chemical class 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 239000007795 chemical reaction product Substances 0.000 description 3
- 230000000295 complement effect Effects 0.000 description 3
- 239000008367 deionised water Substances 0.000 description 3
- 229910021641 deionized water Inorganic materials 0.000 description 3
- 239000002283 diesel fuel Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 229910000510 noble metal Inorganic materials 0.000 description 3
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 238000005096 rolling process Methods 0.000 description 3
- 229910052710 silicon Inorganic materials 0.000 description 3
- 239000010703 silicon Substances 0.000 description 3
- 238000003756 stirring Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 2
- PFRUBEOIWWEFOL-UHFFFAOYSA-N [N].[S] Chemical compound [N].[S] PFRUBEOIWWEFOL-UHFFFAOYSA-N 0.000 description 2
- 125000003118 aryl group Chemical group 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000007710 freezing Methods 0.000 description 2
- 238000010574 gas phase reaction Methods 0.000 description 2
- 238000004898 kneading Methods 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- JKQOBWVOAYFWKG-UHFFFAOYSA-N molybdenum trioxide Chemical compound O=[Mo](=O)=O JKQOBWVOAYFWKG-UHFFFAOYSA-N 0.000 description 2
- 239000012188 paraffin wax Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000011056 performance test Methods 0.000 description 2
- 238000004080 punching Methods 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- WRIDQFICGBMAFQ-UHFFFAOYSA-N (E)-8-Octadecenoic acid Natural products CCCCCCCCCC=CCCCCCCC(O)=O WRIDQFICGBMAFQ-UHFFFAOYSA-N 0.000 description 1
- LQJBNNIYVWPHFW-UHFFFAOYSA-N 20:1omega9c fatty acid Natural products CCCCCCCCCCC=CCCCCCCCC(O)=O LQJBNNIYVWPHFW-UHFFFAOYSA-N 0.000 description 1
- QSBYPNXLFMSGKH-UHFFFAOYSA-N 9-Heptadecensaeure Natural products CCCCCCCC=CCCCCCCCC(O)=O QSBYPNXLFMSGKH-UHFFFAOYSA-N 0.000 description 1
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 1
- 229910018104 Ni-P Inorganic materials 0.000 description 1
- 229910018536 Ni—P Inorganic materials 0.000 description 1
- ZQPPMHVWECSIRJ-UHFFFAOYSA-N Oleic acid Natural products CCCCCCCCC=CCCCCCCCC(O)=O ZQPPMHVWECSIRJ-UHFFFAOYSA-N 0.000 description 1
- 239000005642 Oleic acid Substances 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- FEWJPZIEWOKRBE-UHFFFAOYSA-N Tartaric acid Natural products [H+].[H+].[O-]C(=O)C(O)C(O)C([O-])=O FEWJPZIEWOKRBE-UHFFFAOYSA-N 0.000 description 1
- HIVGXUNKSAJJDN-UHFFFAOYSA-N [Si].[P] Chemical compound [Si].[P] HIVGXUNKSAJJDN-UHFFFAOYSA-N 0.000 description 1
- 239000011959 amorphous silica alumina Substances 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000006229 carbon black Substances 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000000994 depressogenic effect Effects 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- GVGUFUZHNYFZLC-UHFFFAOYSA-N dodecyl benzenesulfonate;sodium Chemical compound [Na].CCCCCCCCCCCCOS(=O)(=O)C1=CC=CC=C1 GVGUFUZHNYFZLC-UHFFFAOYSA-N 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 238000005470 impregnation Methods 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- QXJSBBXBKPUZAA-UHFFFAOYSA-N isooleic acid Natural products CCCCCCCC=CCCCCCCCCC(O)=O QXJSBBXBKPUZAA-UHFFFAOYSA-N 0.000 description 1
- 230000001050 lubricating effect Effects 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 229910000008 nickel(II) carbonate Inorganic materials 0.000 description 1
- ZULUUIKRFGGGTL-UHFFFAOYSA-L nickel(ii) carbonate Chemical compound [Ni+2].[O-]C([O-])=O ZULUUIKRFGGGTL-UHFFFAOYSA-L 0.000 description 1
- 150000004767 nitrides Chemical class 0.000 description 1
- 231100000989 no adverse effect Toxicity 0.000 description 1
- 231100000956 nontoxicity Toxicity 0.000 description 1
- ZQPPMHVWECSIRJ-KTKRTIGZSA-N oleic acid Chemical compound CCCCCCCC\C=C/CCCCCCCC(O)=O ZQPPMHVWECSIRJ-KTKRTIGZSA-N 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000002161 passivation Methods 0.000 description 1
- 239000008213 purified water Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000009738 saturating Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 229940080264 sodium dodecylbenzenesulfonate Drugs 0.000 description 1
- ITCAUAYQCALGGV-XTICBAGASA-M sodium;(1r,4ar,4br,10ar)-1,4a-dimethyl-7-propan-2-yl-2,3,4,4b,5,6,10,10a-octahydrophenanthrene-1-carboxylate Chemical compound [Na+].C([C@@H]12)CC(C(C)C)=CC1=CC[C@@H]1[C@]2(C)CCC[C@@]1(C)C([O-])=O ITCAUAYQCALGGV-XTICBAGASA-M 0.000 description 1
- 229910052596 spinel Inorganic materials 0.000 description 1
- 239000011029 spinel Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000005987 sulfurization reaction Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 235000002906 tartaric acid Nutrition 0.000 description 1
- 239000011975 tartaric acid Substances 0.000 description 1
- 239000001993 wax Substances 0.000 description 1
Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- B01J27/14—Phosphorus; Compounds thereof
- B01J27/186—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J27/188—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium with chromium, molybdenum, tungsten or polonium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
- B01J29/42—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing iron group metals, noble metals or copper
- B01J29/46—Iron group metals or copper
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
-
- B01J35/30—
-
- B01J35/40—
-
- B01J35/51—
-
- B01J35/61—
-
- B01J35/63—
-
- C—CHEMISTRY; METALLURGY
- C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
- C09K—MATERIALS FOR MISCELLANEOUS APPLICATIONS, NOT PROVIDED FOR ELSEWHERE
- C09K8/00—Compositions for drilling of boreholes or wells; Compositions for treating boreholes or wells, e.g. for completion or for remedial operations
- C09K8/02—Well-drilling compositions
- C09K8/03—Specific additives for general use in well-drilling compositions
- C09K8/035—Organic additives
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
- C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
- C10G45/12—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing 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
- C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
- C10G49/02—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 characterised by the catalyst used
- C10G49/04—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 characterised by the catalyst used containing nickel, cobalt, chromium, molybdenum, or tungsten metals, or compounds thereof
-
- C—CHEMISTRY; METALLURGY
- C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
- C09K—MATERIALS FOR MISCELLANEOUS APPLICATIONS, NOT PROVIDED FOR ELSEWHERE
- C09K2208/00—Aspects relating to compositions of drilling or well treatment fluids
- C09K2208/34—Lubricant additives
Abstract
The invention relates to transformer oil base oil and a preparation method thereof, wherein the preparation method comprises the following steps: (1) Mixing raw oil with hydrogen, and carrying out hydrotreating to obtain hydrotreating generated oil; (2) Mixing the hydroprocessing produced oil with hydrogen, and carrying out hydrodewaxing treatment under the action of a hydrodewaxing catalyst to obtain the hydrodewaxing produced oil; (3) And mixing the hydrodewaxing produced oil with hydrogen, refining, and fractionating at the temperature of more than 275 ℃ to obtain the transformer oil base oil. The preparation method provided by the invention can be used for preparing the transformer oil base oil with the characteristics of low sulfur, low nitrogen, low condensation and low aromatic hydrocarbon, and meets the requirements of T-40 ℃ transformer oil (general purpose) base oil in GB2536-2011 standard.
Description
Technical Field
The invention relates to the technical field of transformer oil base oil, in particular to transformer oil base oil and a preparation method thereof, and particularly relates to a preparation method of transformer oil base oil, naphtha and drilling fluid lubricant base oil and transformer oil base oil.
Background
The preparation of the base oil of the transformer oil is very important in the treatment and recovery of crude oil.
CN102676127A discloses a method for preparing a low-fluorescence lubricant for drilling fluid, which comprises the following steps: and (2) adding water into a reaction kettle, heating, adding sodium dodecyl benzene sulfonate, sodium abietate, oleic acid and white oil under continuous stirring, and stirring for reacting for a period of time to fully and uniformly mix the materials to obtain the low-fluorescence lubricant for the drilling fluid. The product disclosed by the method has the characteristics of no toxicity, no pollution, low fluorescence interference, anti-blocking property, good lubricating property and the like, is good in compatibility with various slurries, has no adverse effect on the rheological property of the slurries, and can meet the requirements of well exploration, detailed well exploration, geological logging and environmental protection.
CN106753555A discloses a method for preparing low-condensation-point transformer oil by high-pressure hydrogenation, which comprises the following steps: adding naphthenic oil and a hydrogenation catalyst subjected to sulfurization passivation treatment into a reaction kettle, introducing hydrogen, heating to perform a hydrocracking reaction, performing gas-liquid separation after the reaction is finished, adding a hydrodewaxing catalyst, introducing hydrogen, heating to perform a shape-selective cracking reaction, performing gas-liquid separation after the reaction is finished, and adding activated clay for refining to obtain the low-freezing-point transformer oil. The method for preparing the low-condensation-point transformer oil through high-pressure hydrogenation has the advantages of simple process flow operation and mild conditions, and the prepared transformer oil not only has excellent low-temperature flow performance, but also has light color and good electrical performance. The method needs two times of gas-liquid separation and liquid-solid separation, has complex operation and high energy consumption, and also needs clay refining, thereby bringing the problem of clay consumption.
CN106833740A discloses a preparation method of transformer oil base oil, which comprises the following steps: (1) Hydrofining naphthenic base distillate oil under the action of a catalyst to obtain hydrofined oil; (2) Subjecting the hydrofined oil to hydroisomerization to obtain hydroisomerization oil; (3) And (3) carrying out hydro-refining on the hydro-isomerization generated oil to obtain three-section hydro-generated oil, and then carrying out atmospheric and vacuum fractionation to obtain a fraction with the temperature of more than 280 ℃, namely the transformer oil base oil. The process is a total hydrogen process under a medium-pressure condition, the oxidation stability of the transformer oil is improved under the condition that the obtained transformer oil base oil is not added with a metal passivator, partial naphthenic base characteristics are reserved, and the requirements of a new transformer oil IEC60296-2012 standard can be met. The yield of the transformer oil base oil produced by the process can be improved by more than 8% compared with the traditional process. In the disclosed preparation method, the hydroisomerization catalyst is a noble metal catalyst which takes a mixture of SAPO-11 and ZSM-22 molecular sieves as a carrier and Pt/Pd as an active metal, and the cost is high, so that the production cost of the transformer oil base oil is high.
CN113234483A discloses a preparation method of a transformer oil base oil containing aromatic hydrocarbons. The method solves the problem that the conventional hydrogenation device and process technology are utilized to produce transformer oil base oil containing a proper amount of aromatic hydrocarbons without the transformation of an atmospheric and vacuum device in a fuel oil refinery, and the transformer oil base oil produced under the medium-pressure condition retains a proper amount of aromatic hydrocarbons by the transformation of the catalyst grading of a hydrogenation modified wax oil device. The hydrorefined product oil disclosed by the method needs high-pressure hydrogen stripping, the hydrogen consumption and the energy consumption of a device are increased, and especially the application range of the transformer oil base oil is limited because the pour point of the base oil is-32 ℃ and the sulfur content of the base oil is more than 70mg/kg at the reaction temperature of the heterogeneous pour point depressing catalyst of 370 ℃.
CN101386792A discloses transformer oil base oil and a preparation method and application thereof. The preparation method of the transformer oil base oil comprises the following steps: 1) Performing furfural refining on SZ36-1 normal second-line distillate to obtain refined oil, and removing furfural to obtain dealdehydized refined oil; 2) Removing nitrogen from the refined dealdehydized oil, and removing nitrogen slag to obtain refined denitrified oil; 3) Adding argil into the denitrified refined oil for argil refining; and obtaining the transformer oil base oil. The method disclosed by the method can not produce the transformer oil with lower pour point, and has the problems of low transformer oil yield, difficult treatment of the waste argil and the like.
In view of the above prior art, no processing technology for preparing low-freezing point and low-aromatic transformer oil base oil under medium pressure by using a sulfurized catalyst exists up to now, and the low-freezing point and low-aromatic transformer oil base oil production technology adopts a high-activity reduced noble metal catalyst or a sulfurized catalyst under high pressure, so that the device construction and production costs are increased.
Therefore, it is important to develop a preparation method capable of simply and inexpensively producing the transformer oil base oil with the characteristics of low sulfur, low nitrogen, low condensation and low aromatic hydrocarbon.
Disclosure of Invention
Aiming at the defects of the prior art, the invention aims to provide the transformer oil base oil and the preparation method thereof, the preparation method can be used for preparing the transformer oil base oil with the characteristics of low sulfur, low nitrogen, low condensation and low aromatic hydrocarbon, and meets the requirements of the T-40 ℃ transformer oil (general purpose) base oil in GB2536-2011 standard; the preparation method is simple and easy to operate, can meet production requirements at medium pressure, is low in cost, and can prepare naphtha and drilling fluid lubricant base oil meeting the Q/HX PF001-2019 standard by adjusting the fractionation temperature.
In order to achieve the purpose, the invention adopts the following technical scheme:
in a first aspect, the present invention provides a method for preparing a transformer oil base oil, comprising the steps of:
(1) Mixing raw oil with hydrogen, and carrying out hydrotreating to obtain hydrotreating generated oil;
(2) Mixing the hydro-processing generated oil with hydrogen, and carrying out hydro-dewaxing treatment under the action of a hydro-dewaxing catalyst to obtain hydro-dewaxing generated oil;
(3) And mixing the hydrodewaxing produced oil with hydrogen, refining, and fractionating at the temperature of more than 275 ℃ (such as 280 ℃, 290 ℃, 300 ℃ and the like) to obtain the transformer oil base oil.
In the invention, raw oil and hydrogen are mixed and subjected to hydrotreating to remove hetero atoms such as sulfur, nitrogen, oxygen and the like in the raw material and saturate aromatic hydrocarbon, thus obtaining hydrotreating generated oil; mixing the hydrotreating generated oil with hydrogen, and selectively removing macromolecular normal paraffin with high condensation point under the action of a hydrodewaxing catalyst to obtain hydrodewaxing generated oil; and mixing the hydrodewaxing produced oil with hydrogen to perform refining treatment, further saturating olefin and aromatic hydrocarbon, and then performing atmospheric and vacuum fractionation to obtain a fraction with the temperature of more than 275 ℃, namely the transformer oil base oil.
Preferably, in step (1), the hydrotreating is carried out under the action of a hydrotreating catalyst.
Preferably, the hydrotreating catalyst comprises an active metal oxide and a metal oxide promoter.
Preferably, the active metal oxide comprises a group VIII metal oxide and/or a group VIB metal oxide.
Preferably, the active metal oxide comprises nickel oxide and/or tungsten trioxide.
Preferably, the metal oxide adjuvant comprises any one of, or a combination of at least two of, SB, boric acid, phosphoric acid, or sesbania, where typical but non-limiting combinations include: combinations of SB and boric acid, phosphoric acid and sesbania, combinations of SB, boric acid, phosphoric acid and sesbania, and the like.
In the present invention, SB means: high purity pseudoboehmite.
Illustratively, SB and sesbania are powdered structures.
Preferably, the mass percent of the group VIII metal oxide is from 2.0% to 6.0%, such as 2.5%, 3%, 3.5%, 4%, 4.5%, 5%, 5.5%, etc., based on 100% of the total mass of the hydrotreating catalyst.
Preferably, the mass percent of the group VIB metal oxide is 15% -30%, such as 16%, 18%, 20%, 22%, 24%, 26%, 28%, etc., based on 100% of the total mass of the hydrotreating catalyst.
Preferably, the mass percent of the metal oxide promoter is 2.0% to 5.0%, such as 2.5%, 3%, 3.5%, 4%, 4.5%, etc., based on 100% of the total mass of the hydrotreating catalyst.
In the invention, the hydrotreating catalyst is preferred to remove hetero atoms such as sulfur, nitrogen, oxygen and the like and saturate aromatic hydrocarbon, so that the sulfur, nitrogen, oxygen and aromatic hydrocarbon content of the hydrogenated oil is reduced.
Preferably, the preparation method of the hydrotreating catalyst comprises the following steps:
mixing a compound containing an active metal element, a metal oxide auxiliary agent and the slurry, and filtering to obtain a filter cake and a filtrate;
and forming a binder from the filtrate, and performing compression molding, drying and roasting on the binder and the filter cake to obtain the hydrotreating catalyst.
Preferably, the slurry comprises water, silica and alumina.
Preferably, in step (1), the reaction pressure of the hydrotreatment is 8.0 to 10.0MPa, such as 8.2 MPa, 8.4MPa, 8.6MPa, 8.8MPa, 9MPa, 9.2MPa, 9.4MPa, 9.6MPa, 9.8MPa and the like.
Preferably, the reaction temperature of the hydrotreatment is 300 to 370 ℃, such as 310 ℃, 320 ℃, 330 ℃, 340 ℃,350 ℃, 360 ℃ and the like.
Preferably, the volume ratio of the hydrogen to the raw oil is (600-1200): 1, wherein 600-1200 can be 700, 800, 900, 1000, 1100 and the like.
Preferably, the volume space velocity of the hydrotreatment is 0.2-1.0h -1 E.g. 0.3h -1 、0.4h -1 、0.5h -1 、 0.6h -1 、0.7h -1 、0.8h -1 、0.9h -1 And the like.
Preferably, in the step (2), the hydrodewaxing catalyst comprises a catalyst carrier and an active metal oxide arranged in the catalyst carrier and/or on the surface of the catalyst carrier.
In the invention, the hydrodewaxing catalyst is preferably selected to selectively remove macromolecular normal paraffin with high condensation point, so that the pour point of the hydrogenated oil is reduced.
Preferably, the active metal oxide comprises a group VIII metal oxide and/or a group VIB metal oxide.
Preferably, the mass percent of the group VIII metal oxide is 1.0% -6.0%, such as 1.5%, 2%, 2.5%, 3%, 3.5%, 4%, 4.5%, 5%, 5.5%, etc., based on 100% of the total mass of the hydrodewaxing catalyst.
Preferably, the mass percentage of the VIB group metal oxide is 2.0% -10.0%, such as 3%, 4%, 5%, 6%, 7%, 8%, 9% and the like, based on the total mass of the hydrodewaxing catalyst being 100%.
Preferably, the active metal oxide comprises nickel oxide and/or tungsten trioxide.
Preferably, the catalyst support comprises a catalyst support and a molecular sieve disposed within and/or on the surface of the catalyst support.
Preferably, the mass percent of the molecular sieve is 8.0-40.0%, such as 10%, 15%, 20%, 25%, 30%, 35%, etc., based on 100% of the total mass of the hydrodewaxing catalyst.
Preferably, the mother liquor of the molecular sieve comprises aluminum sulfate, silica sol, an alkaline substance and water.
Preferably, the silica sol comprises silica.
Preferably, the basic substance comprises sodium hydroxide and/or triethylamine.
Preferably, the raw materials for preparing the catalyst carrier support body comprise pseudo-boehmite, peptizer, extrusion aid, pore-expanding agent, metal oxide aid and water.
According to the invention, the hydro-dewaxing catalyst is added with a pore-expanding agent with a certain particle size in the preparation process of the catalyst carrier support, so that the prepared support has a larger pore volume and a larger pore diameter, a large space is reserved for the subsequent synthesis of the molecular sieve, a certain auxiliary agent is added in the preparation process, and the hydro-dewaxing catalyst and alumina form a spinel structure after high-temperature roasting, so that the strength and the framework stability of the support are improved, and meanwhile, the molecular sieve is synthesized in the pore channel of the support and coated on the surface of the pore channel of the support, so that the molecular sieve is exposed outside, and the activity of the catalyst is further improved.
Preferably, the catalyst support has a solids content of 50% to 80%, such as 55%, 60%, 65%, 70%, 75%, etc.
Preferably, the mass percentage of the metal oxide auxiliary agent is 1.0-6.0%, such as 1.5%, 2%, 2.5%, 3%, 3.5%, 4%, 4.5%, 5%, 5.5%, etc., based on 100% of the total mass of the hydrodewaxing catalyst.
Preferably, the preparation method of the hydrodewaxing catalyst comprises the following steps: and (3) dipping the catalyst carrier in an active metal salt solution, drying and roasting to obtain the hydrodewaxing catalyst.
Preferably, the preparation method of the catalyst carrier comprises the following steps: and (2) soaking the catalyst carrier support in the molecular sieve mother liquor, and then crystallizing, washing, drying and roasting the catalyst carrier support to obtain the catalyst carrier.
Preferably, the method for preparing the catalyst carrier support comprises the steps of: mixing pseudo-boehmite, peptizing agent, extrusion aid and water, and then sequentially molding, drying and roasting to obtain the catalyst carrier support.
As a preferable technical scheme, the preparation method of the hydrodewaxing catalyst comprises the following steps:
mixing pseudo-boehmite, peptizing agent, extrusion aid and water, and then sequentially carrying out forming, drying and roasting to obtain a catalyst carrier support body;
mixing aluminum sulfate, silica sol, alkaline substances and water to obtain a molecular sieve mother liquor;
dipping the catalyst carrier support body in a molecular sieve mother solution, and then crystallizing, washing, drying and roasting the catalyst carrier support body to obtain a catalyst carrier;
and (3) dipping the catalyst carrier in an active metal salt solution, drying and roasting to obtain the hydrodewaxing catalyst.
Preferably, in the step (2), the reaction pressure of the hydrodewaxing treatment is 8.0-10.0MPa, such as 8.5MPa, 9MPa, 9.5MPa, etc.
Preferably, the reaction temperature of the hydrodewaxing treatment is 280-340 ℃, such as 290 ℃, 300 ℃, 310 ℃, 320 ℃, 330 ℃ and the like.
Preferably, the volume ratio of the hydrogen to the hydroprocessed product oil (600-1200): 1, wherein 600-1200 can be 700, 800, 900, 1000, 1100, etc.
Preferably, the volume space velocity of the hydrodewaxing treatment is 0.8-3.0h -1 E.g. 1h -1 、1.2h -1 、 1.4h -1 、1.6h -1 、1.8h -1 、2h -1 、2.2h -1 、2.4h -1 、2.6h -1 、2.8h -1 And the like.
Preferably, in the step (3), the purification treatment is carried out under the action of a supplementary purification catalyst.
Preferably, the post-refining catalyst comprises a catalyst carrier, and an active metal oxide and an auxiliary agent which are arranged in the catalyst carrier and/or on the surface of the catalyst carrier.
Preferably, the active metal oxide comprises a group VIII metal oxide and/or a group VIB metal oxide.
Preferably, the mass percentage of the group viii metal oxide is 4.0% to 10.0%, for example, 4.5%, 5%, 5.5%, 6%, 6.5%, 7%, 7.5%, 8%, 8.5%, 9%, 9.5%, etc., based on 100% of the total mass of the post-purification catalyst.
Preferably, the mass percentage of the group VIB metal oxide is 15% -30%, for example 16%, 18%, 20%, 22%, 24%, 26%, 28%, etc., based on 100% of the total mass of the post-refining catalyst.
Preferably, the adjuvant comprises a heteroatom.
Preferably, the heteroatoms include any one or a combination of at least two of phosphorus, fluorine, boron, titanium or zirconium, with typical but non-limiting combinations including: a combination of phosphorus and fluorine, a combination of boron, titanium and zirconium, a combination of phosphorus, fluorine, boron, titanium and zirconium.
Preferably, the promoter comprises any one of a phosphorus-containing promoter, a fluorine-containing promoter, a boron-containing promoter, a titanium-containing promoter, or a zirconium-containing promoter, or a combination of at least two thereof, wherein typical but non-limiting combinations include: the combination of the phosphorus-containing assistant and the fluorine-containing assistant, the combination of the boron-containing assistant, the titanium-containing assistant and the zirconium-containing assistant, the combination of the phosphorus-containing assistant, the fluorine-containing assistant, the boron-containing assistant, the titanium-containing assistant and the zirconium-containing assistant, and the like.
Preferably, the mass percentage of the heteroatoms in the auxiliary agent is 1.0% to 10.0%, such as 2%, 3%, 4%, 5%, 6%, 7%, 8%, 9%, etc., based on 100% of the total mass of the post-purification catalyst.
Preferably, the preparation raw materials of the catalyst carrier comprise pseudo-boehmite, a peptizing agent, an extrusion assistant and water.
In the present invention, the post-refining catalyst is preferred to reduce the olefin and aromatic content of the hydrogenated oil by further removing the olefin and aromatic.
Preferably, the preparation method of the replenished and refined catalyst comprises the following steps:
mixing any one or the combination of at least two of active metal, active metal salt or active metal oxide with a solvent, an auxiliary agent, an oil phase and other additives to form the water-in-oil microemulsion;
and (2) impregnating the water-in-oil microemulsion into the catalyst carrier, drying and roasting, impregnating the treated catalyst carrier into a solution containing any one or a combination of at least two of active metal, active metal salt or active metal oxide, and drying and roasting again to obtain the supplemented refined catalyst.
Preferably, the preparation method of the catalyst carrier comprises the following steps: mixing pseudo-boehmite, peptizing agent, extrusion assistant and water, and then sequentially molding, drying and roasting to obtain the catalyst carrier.
Preferably, the oil phase comprises any one of, or a combination of at least two of, n-octane, heptane, or cyclohexane, with typical but non-limiting combinations including: a combination of n-octane and heptane, a combination of heptane and cyclohexane, a combination of n-octane, heptane and cyclohexane, and the like.
Preferably, the further additives comprise surfactants and/or cosurfactants.
Preferably, in the step (3), the reaction pressure of the purification treatment is 8.0 to 10.0MPa, for example, 8.5MPa, 9MPa, 9.5MPa, etc.
Preferably, the reaction temperature of the purification treatment is 290 to 360 ℃, for example, 300 ℃, 310 ℃, 320 ℃, 330 ℃, 340 ℃,350 ℃ and the like.
Preferably, the volume ratio of the hydrogen gas to the hydrodewaxing produced oil (600-1200): 1, wherein 600-1200 can be 700, 800, 900, 1000, 1100, etc.
Preferably, the volume space velocity of the refining treatment is 0.3-2.0h -1 E.g. 0.4h -1 、0.6h -1 、0.8h -1 、 1h -1 、1.2h -1 、1.4h -1 、1.6h -1 、1.8h -1 And the like.
Preferably, the feedstock oil comprises any one of, or a combination of at least two of, cycloalkyl-normal-second-line, cycloalkyl-minus-one-line, or hydro-upgraded diesel, wherein typical but non-limiting combinations include: a combination of a cycloalkyl ordinary second line and a cycloalkyl minus first line, a combination of a cycloalkyl minus first line and a hydroupgraded diesel oil, a combination of a cycloalkyl ordinary second line, a cycloalkyl minus first line and a hydroupgraded diesel oil, and the like, and further preferred is a cycloalkyl ordinary second line and/or a cycloalkyl minus first line.
Preferably, the pressure of the single stage medium pressure hydrogenation is 8.0 to 10.0MPa, such as 8.8MPa, 9MPa, 9.5MPa, and the like.
In a second aspect, the present invention provides a transformer oil base oil prepared by the preparation method of the first aspect;
the transformer oil base oil has a sulfur content of < 1.0mg/kg (e.g., 0.8mg/kg, 0.6mg/kg, 0.4mg/kg, 0.2mg/kg, etc.), a nitrogen content of < 1.0mg/kg (e.g., 0.8mg/kg, 0.6mg/kg, 0.4mg/kg, 0.2mg/kg, etc.), total aromatics < 10% (e.g., 8%, 6%, 4%, etc.), and a pour point < -57 ℃ (e.g., -59 ℃, -60 ℃, -61 ℃, etc.).
In a third aspect, the present invention provides a process for producing naphtha, the process comprising the steps of:
(1) Mixing raw oil with hydrogen, and carrying out hydrotreatment to obtain hydrotreatment generated oil;
(2) Mixing the hydro-processing generated oil with hydrogen, and carrying out hydro-dewaxing treatment under the action of a hydro-dewaxing catalyst to obtain hydro-dewaxing generated oil;
(3) Mixing the hydrodewaxing produced oil with hydrogen gas, refining, and fractionating at < 215 deg.C (such as 210 deg.C, 205 deg.C, 200 deg.C, 195 deg.C, etc.) to obtain the naphtha.
In a fourth aspect, the present invention provides a method for preparing a base oil for a drilling fluid lubricant, comprising the steps of:
(1) Mixing raw oil with hydrogen, and carrying out hydrotreatment to obtain hydrotreatment generated oil;
(2) Mixing the hydro-processing generated oil with hydrogen, and carrying out hydro-dewaxing treatment under the action of a hydro-dewaxing catalyst to obtain hydro-dewaxing generated oil;
(3) Mixing the hydrodewaxing produced oil with hydrogen, refining, and fractionating at 215-275 deg.C (such as 220 deg.C, 230 deg.C, 240 deg.C, 250 deg.C, 260 deg.C, 270 deg.C, etc.) to obtain the base oil for drilling fluid lubricant.
In the invention, the process parameters and raw materials involved in the preparation method of the transformer oil base oil are suitable for the base oil and naphtha of the drilling fluid lubricant, and different products can be obtained only by adjusting the fractionation temperature.
Compared with the prior art, the invention has the following beneficial effects:
(1) The preparation method of the transformer oil base oil provided by the invention has the advantages that the sulfur content of the transformer oil base oil is less than 1.0mg/kg, the nitrogen content of the transformer oil base oil is less than 1.0mg/kg, the total aromatic hydrocarbon of the transformer oil base oil is less than 10%, the pour point of the transformer oil base oil is less than-57 ℃, the index requirements of the T-40 ℃ transformer oil (general) base oil in GB2536-2011 standard are met, and the transformer oil base oil has the characteristics of low sulfur, low nitrogen, low condensation and low aromatic hydrocarbon by adjusting the reaction gradation of a hydrogenation catalyst under the condition of the reaction pressure of 9.5 MPa.
(2) The invention solves the problems that a high-pressure hydrogenation process or a hydrotreating-furfural refining-clay refining process is needed when producing the low-condensation and low-aromatic transformer oil base oil, the former increases the energy consumption of a device and the production cost, and the latter influences the product yield and causes environmental pollution. The invention realizes high removal rate of sulfide, nitride and aromatic hydrocarbon in raw materials by adjusting the catalyst gradation, can directly produce the transformer oil base oil with low condensation point and low aromatic hydrocarbon under the condition of medium-pressure hydrogenation moderation process, has better product properties than the traditional transformer oil base oil production process and the high-pressure hydrogenation process, and reduces the production cost of industrial devices.
(3) The preparation method is simple and easy to operate, can meet production requirements at medium pressure, is low in cost, and can prepare naphtha and drilling fluid lubricant base oil meeting the Q/HX PF001-2019 standard by adjusting the fractionation temperature.
Drawings
FIG. 1 is a process flow diagram of the preparation process described in example 1 of the present invention.
Detailed Description
For the purpose of facilitating an understanding of the present invention, the following examples are set forth herein. It should be understood by those skilled in the art that the examples are only for the understanding of the present invention and should not be construed as the specific limitation of the present invention.
In the present invention, the raw materials used were obtained from Zhonghai bitumen Co., ltd, and the information on part of the raw materials is shown in Table 1:
TABLE 1
In the present invention, the process conditions in the hydrotreating process of each embodiment are shown in table 2:
TABLE 2
In table 2, example 4 and example 3 correspond to two process parameters, and the pour points of the hydrogenated oil obtained are different due to different temperatures of the hydrodewaxing reaction, which is designed to show that the pour point depressing catalyst still has better pour point depressing performance at lower temperature.
Example 1
The embodiment provides a preparation method of transformer oil base oil, wherein specific process parameters are shown in table 2, and a process flow diagram is shown in fig. 1, and the preparation method comprises the following steps:
(1) Mixing the raw oil (Suzhou 36-1 normal second line, performance shown in Table 1) with hydrogen, and carrying out hydrotreatment under the action of a hydrotreatment catalyst to obtain hydrotreatment generated oil;
(2) Mixing the hydro-processing generated oil with hydrogen, and carrying out hydro-dewaxing treatment under the action of a hydro-dewaxing catalyst to obtain hydro-dewaxing generated oil;
(3) Mixing the hydrodewaxing produced oil with hydrogen, refining under the action of a supplementary refining catalyst, and fractionating to obtain the transformer oil base oil;
wherein, the hydrotreating catalyst is obtained by the following preparation method, and the preparation method comprises the following steps:
(1) 100g of calcined silicon-and phosphorus-containing alumina powder (SiO, among others) 2 Is 3.3% by mass, P 2 O 5 Is 7% by mass, the balanceIn an amount of Al 2 O 3 ) Adding into 300m1 water (water content of the obtained slurry is 75 wt%), stirring for 5min, adding 18.7g boric acid (as B) 2 O 3 In terms of the mass of the catalyst (A), the amount of boric acid added was 4.6% of the mass of the prepared hydrorefining catalyst), 73g of ammonium metatungstate (in terms of WO) 3 The mass of ammonium metatungstate is 28.4 percent of the mass of the prepared hydrofining catalyst, 37g of nickel nitrate (the mass of nickel nitrate is 4.1 percent of the mass of the prepared hydrofining catalyst based on the mass of NiO) is continuously stirred for 1 hour, the mixture is kept stand for 2 hours and then filtered, and the filtrate is heated to 95 ℃, and is prepared into a binder with 55g of SB powder (the mass of the added nickel nitrate is 19 percent of the mass of the prepared hydrofining catalyst) and 4m1 of concentrated nitric acid (the mass of the silicon-containing and phosphorus-containing alumina powder is 3.6 percent of the mass of the prepared hydrofining catalyst) for later use.
(2) And drying the wet filter cake at 120 ℃ for 8 hours, crushing the filter cake into powder, mixing the powder with 4g of sesbania powder (the addition is 4 percent of the mass of the silicon-containing and phosphorus-containing alumina powder) and the adhesive, rolling, extruding the mixture into strips, forming the strips, standing and maintaining the strips at room temperature for 4 hours, drying the strips at 120 ℃ for 4 hours, roasting the strips at constant temperature of 230 ℃ for 1 hour, roasting the strips at constant temperature of 350 ℃ for 1 hour, and roasting the strips at constant temperature of 480 ℃ for 4 hours to obtain the hydrotreating catalyst.
The hydrodewaxing catalyst is prepared by the following preparation method, and the preparation method comprises the following steps:
(1) Weighing the aluminum sulfate method produced pore volume of 1.095mL/g and the specific surface area of 328m 2 500g of pseudo-boehmite with a dry basis of 71 percent, 18.4g of nitric acid with a concentration of 65 percent, 10g of sesbania powder, 71g of carbon black and a nickel nitrate additive (purchased from Huaishiang petrochemical company Limited, ni (NO) 3 ) 2 ·6H 2 O>98%) 60g and 754g of deionized water are added into a rolling machine for rolling and mixing, extruded into a cylindrical strip with the outer diameter of 6mm and the inner hollow diameter of 2.5mm, and the strip is dried under the conditions of constant humidity and constant temperature until the solid content is 65%.
Punching circular through holes with the diameter of 1.5mm uniformly arranged on the surface of the cylindrical strip by using punching equipment, preparing particles with the length of 3-10 mm, drying at 130 ℃ for 8 hours, and roasting at 900 ℃ for 3 hours to obtain the catalyst carrier support body.
(2) Weighing 7.52g of aluminum sulfate and 30 percent of silicon oxide320g of sol (purchased from Qingdao ocean chemical Co., ltd., siO) 2 30 percent of sodium hydroxide, 2.15g of sodium hydroxide, 1.81g of triethylamine and 80g of water are prepared into ZSM-5 molecular sieve mother liquor; and (2) soaking the carrier support body by using the prepared molecular sieve mother liquor, placing the soaked material on the upper part of a gas phase reaction kettle, adding deionized water into the bottom of the gas phase reaction kettle, reacting for 36 hours at 180 ℃, washing the reaction product to be neutral by using the deionized water after the reaction is finished, drying the reaction product for 8 hours at 130 ℃, and roasting the reaction product for 3 hours at 550 ℃ to obtain the catalyst carrier containing the ZSM-5 molecular sieve membrane.
(3) Weighing 30.3g of nickel nitrate to prepare a solution containing 0.019g/mL of nickel oxide, impregnating the catalyst carrier, drying the impregnated material at 120 ℃ for 8 hours, and roasting the dried material at 450 ℃ for 3 hours to obtain the hydrodewaxing catalyst.
The complementary refined catalyst is obtained by the following preparation method, and the preparation method comprises the following steps:
(1) Weighing the small-pore alumina (pore volume is 0.49mL/g, specific surface area is 229 m) 3 40.5 g), adding 69.4g of pure water and 8.1mL of concentrated nitric acid, and uniformly mixing to prepare an adhesive;
(2) Respectively weighing 126.3g of HZSM-5 molecular sieve, 3.0g of sesbania powder and the adhesive, kneading, extruding and forming;
(3) Drying the wet strips at 100 +/-10 ℃ for 4h, and roasting at 730 ℃ for 4h to prepare a carrier;
(4) 24.9g of nickel nitrate is dissolved by purified water to prepare 200ml of solution;
(5) And (3) putting 100g of the carrier into the impregnation liquid, impregnating for 2h, filtering, drying for 4h at the temperature of 100 ℃, and roasting for 3h at the temperature of 480 ℃ to obtain the complementary refined catalyst.
Taking Chinese patent CN105195231A as a comparative example, the reference pour point depressing catalyst is obtained by the following preparation method, and the preparation method comprises the following steps:
(1) Taking 50g of modified alumina, 100g of amorphous silica-alumina, 45g of USY molecular sieve and 310g of adhesive prepared by peptizing nitric acid and SB alumina, mixing, kneading, grinding to prepare paste capable of extruding strips, and extruding the strips for molding. Drying at 110 deg.C for 6 hr, and calcining at 550 deg.C for 4 hr to obtain carrier;
(2) Dissolving 7g of basic nickel carbonate, 20g of molybdenum trioxide and 4g of phosphoric acid in 70m1 of water solution, then soaking the Mo-Ni-P co-soaking solution on 80g of carrier for 2 hours by adopting an isovolumetric soaking method, drying at 110 ℃ for 6 hours, and roasting at 350 ℃ for 2 hours to obtain the catalyst.
(3) Dissolving 20g of tartaric acid in 15m1 of water, then fixing the volume to 70m1, dipping 110g of the catalyst by an isometric dipping method, drying in the shade after 2 hours, drying at 100 ℃ for 2 hours, and roasting at 350 ℃ for 2 hours to obtain the reference pour point depressing catalyst.
Specifically, the information of the hydrotreating catalyst, the hydrodewaxing catalyst, the complementary refining catalyst and the reference dewaxing catalyst is shown in table 3:
TABLE 3
Example 2
The difference between this example and example 1 is that the feedstock oil is a line reduced from Suizhong 36-1, the process parameters are shown in Table 2, and the rest is the same as example 1.
Example 3
This example is different from example 1 in the process parameters, and is the same as example 1 except as shown in table 2.
Example 4
The difference between this example and example 1 is the process parameters, as shown in table 2, the rest is the same as example 1.
Comparative example 1
This comparative example differs from example 1 in that the hydrodewaxing catalyst was replaced with a commercially available reference pour point depressant, the process parameters are as shown in Table 2, and the remainder is the same as in example 1.
Comparative example 2
The comparative example is different from example 1 in that the preparation method of the transformer oil base oil is a traditional production process, namely a hydrotreating-furfural refining-clay refining process.
Comparative example 3
The difference between the comparative example and the example 1 is that the raw material oil is hydro-upgrading diesel oil, and the raw material is subjected to a hydrodewaxing-supplementary refining test under a high pressure condition (the catalyst loading is 200mL, and new hydrogen passes through the catalyst loading in one step, which is produced by Shanghai Michelle Experimental facility Co., ltd.); and finally, distilling the obtained hydrogenated oil, wherein the distillate with the distillation range of more than or equal to 275 ℃ is the transformer oil base oil.
Performance testing
1. The fractionation temperatures of examples 1-4 and comparative examples 1-3 were controlled to > 275 ℃ to obtain transformer oil base oils, performance tests were performed at T-40 ℃ in GB2536-2011, and the test results are summarized in tables 4 and 5.
TABLE 4
TABLE 5
The data in the table 4 are analyzed, and it can be seen that in the preparation method of the invention, the transformer oil base oil is prepared by adopting a 9.5MPa medium-pressure process, and the obtained transformer oil base oil has the sulfur and nitrogen contents of less than or equal to 1.0mg/kg, and the pour point<-54℃、C A Value of<1% of total aromatic hydrocarbons<10 percent. As can be seen from the kinetics of hydrogenation, the higher the pressure, the more favorable the effective removal of aromatic hydrocarbons, especially for the deep removal of aromatic hydrocarbons, which is currently carried out under high pressure conditions or by using noble metal catalysts at home and abroad.
Compared with the production technology of the traditional transformer oil base oil of the comparative example 2: the sulfur nitrogen content, the aromatic hydrocarbon and the pour point of the transformer oil base oil produced by medium-pressure hydrogenation are superior to those of the traditional transformer oil, and meanwhile, the problems that the waste carclazyte is difficult to treat and the like do not exist; compared with the production technology of the base oil of the transformer oil under the high-pressure condition of the comparative example 3: the sulfur nitrogen content, the aromatic hydrocarbon and the pour point of the transformer oil base oil produced by adopting medium-pressure hydrogenation are all equivalent to those of a high-pressure production technology, and meanwhile, the construction and production cost of the device is reduced.
Therefore, the preparation method of the transformer oil base oil is superior to the traditional transformer oil base oil production technology and is equivalent to the high-voltage transformer oil base oil production technology, and the technology has no relevant application at home and abroad.
The data in the table 5 are analyzed, it can be seen that the hydrodewaxing catalyst of the invention still has higher pour point depressing activity at the reaction temperature of 310 ℃, and compared with the commercial industrial catalyst, under the same catalyst gradation condition, the hydrodewaxing section reaction temperature of the invention is 50 ℃ lower, and the yield of the transformer oil base oil obtained is 10.9% higher than that of the commercial industrial catalyst. The hydrodewaxing catalyst has higher activity, thus solving the influence of future pour point fluctuation of raw materials on the product properties of a refinery and widening the raw material sources of a device.
2. The temperatures of examples 1-2 and comparative examples 2-3 were controlled at 215-275 ℃ to obtain drilling fluid lubricant base oils, performance tests were performed with reference to Q/HX PF001-2019, and the test results are summarized in Table 6.
TABLE 6
Analysis of the data in table 6 shows that the preparation method provided by the invention can be used for preparing the base oil of the drilling fluid lubricant by adjusting the fractionation temperature, and the obtained base oil of the drilling fluid lubricant meets the requirements of Q/HX PF 001-2019.
The applicant states that the present invention is illustrated in detail by the above examples, but the present invention is not limited to the above detailed methods, i.e. it is not meant that the present invention must rely on the above detailed methods for its implementation. It should be understood by those skilled in the art that any modification of the present invention, equivalent substitutions of the raw materials of the product of the present invention, addition of auxiliary components, selection of specific modes, etc., are within the scope and disclosure of the present invention.
Claims (10)
1. The preparation method of the transformer oil base oil is characterized by comprising the following steps:
(1) Mixing raw oil with hydrogen, and carrying out hydrotreatment to obtain hydrotreatment generated oil;
(2) Mixing the hydroprocessing produced oil with hydrogen, and carrying out hydrodewaxing treatment under the action of a hydrodewaxing catalyst to obtain the hydrodewaxing produced oil;
(3) And mixing the hydrodewaxing produced oil with hydrogen, refining, and fractionating at the temperature of more than 275 ℃ to obtain the transformer oil base oil.
2. The production method according to claim 1, wherein in the step (1), the hydrotreating is performed under the action of a hydrotreating catalyst;
preferably, the hydrotreating catalyst comprises an active metal oxide and a metal oxide promoter;
preferably, the active metal oxide comprises a group viii metal oxide and/or a group vib metal oxide;
preferably, the active metal oxide comprises nickel oxide and/or tungsten trioxide;
preferably, the metal oxide additive comprises any one or a combination of at least two of SB, boric acid, phosphoric acid, or sesbania;
preferably, the mass percent of the group VIII metal oxide is 2.0% -6.0% based on 100% of the total mass of the hydrotreating catalyst;
preferably, the mass percent of the VIB group metal oxide is 15-30% based on 100% of the total mass of the hydrotreating catalyst;
preferably, the mass percent of the metal oxide auxiliary agent is 2.0-5.0% based on 100% of the total mass of the hydrotreating catalyst;
preferably, the preparation method of the hydrotreating catalyst comprises the following steps:
mixing a compound containing an active metal element, a metal oxide auxiliary agent and the slurry, and filtering to obtain a filter cake and a filtrate;
forming a binder from the filtrate, and performing compression molding, drying and roasting on the binder and the filter cake to obtain the hydrotreating catalyst;
preferably, the slurry comprises water, silica and alumina.
3. The production method according to claim 1 or 2, wherein in the step (1), the reaction pressure of the hydrotreatment is 8.0 to 10.0MPa;
preferably, the reaction temperature of the hydrotreatment is 300-370 ℃;
preferably, the volume ratio of the hydrogen to the raw oil is (600-1200) to 1;
preferably, the volume space velocity of the hydrotreatment is 0.2-1.0h -1 。
4. The method according to any one of claims 1 to 3, wherein in the step (2), the hydrodewaxing catalyst comprises a catalyst carrier and an active metal oxide disposed inside and/or on the surface of the catalyst carrier;
preferably, the active metal oxide comprises a group viii metal oxide and/or a group vib metal oxide;
preferably, the mass percent of the VIII group metal oxide is 1.0-6.0% based on 100% of the total mass of the hydrodewaxing catalyst;
preferably, the mass percent of the VIB group metal oxide is 2.0-10.0% by taking the total mass of the hydrodewaxing catalyst as 100%;
preferably, the active metal oxide comprises nickel oxide and/or tungsten trioxide;
preferably, the catalyst carrier comprises a catalyst carrier support and a molecular sieve arranged inside and/or on the surface of the catalyst carrier support;
preferably, the mass percent of the molecular sieve is 8.0-40.0% by taking the total mass of the hydrodewaxing catalyst as 100%;
preferably, the mother liquor of the molecular sieve comprises aluminum sulfate, silica sol, alkaline substances and water;
preferably, the silica sol comprises silica;
preferably, the basic substance comprises sodium hydroxide and/or triethylamine;
preferably, the preparation raw materials of the catalyst carrier support body comprise pseudo-boehmite, peptizing agent, extrusion assistant, pore-expanding agent, metal oxide assistant and water;
preferably, the catalyst support has a solids content of 50% to 80%;
preferably, the mass percent of the metal oxide additive is 1.0-6.0% by taking the total mass of the hydrodewaxing catalyst as 100%;
preferably, the preparation method of the hydrodewaxing catalyst comprises the following steps: dipping a catalyst carrier in an active metal salt solution, drying and roasting to obtain the hydrodewaxing catalyst;
preferably, the preparation method of the catalyst carrier comprises the following steps: impregnating a catalyst carrier support in a molecular sieve mother solution, and crystallizing, washing, drying and roasting the catalyst carrier support to obtain a catalyst carrier;
preferably, the method for preparing the catalyst carrier support comprises the steps of: mixing pseudo-boehmite, peptizing agent, extrusion assistant and water, and then sequentially molding, drying and roasting to obtain the catalyst carrier support body.
5. The process according to any one of claims 1 to 4, wherein in the step (2), the reaction pressure of the hydrodewaxing treatment is 8.0 to 10.0MPa;
preferably, the reaction temperature of the hydrodewaxing treatment is 280-340 ℃;
preferably, the volume ratio of the hydrogen to the hydroprocessed product oil (600-1200): 1;
preferably, the volume space velocity of the hydrodewaxing treatment is 0.8-3.0h -1 。
6. The production method according to any one of claims 1 to 5, wherein in the step (3), the refining treatment is carried out under the action of a supplementary refining catalyst;
preferably, the supplementary refined catalyst comprises a catalyst carrier, and an active metal oxide and an auxiliary agent which are arranged in the catalyst carrier and/or on the surface of the catalyst carrier;
preferably, the active metal oxide comprises a group viii metal oxide and/or a group vib metal oxide;
preferably, the mass percent of the VIII group metal oxide is 4.0-10.0% based on 100% of the total mass of the supplementary refined catalyst;
preferably, the mass percent of the VIB group metal oxide is 15-30% based on 100% of the total mass of the supplementary refined catalyst;
preferably, the adjuvant comprises a heteroatom;
preferably, the heteroatoms comprise any one or a combination of at least two of phosphorus, fluorine, boron, titanium or zirconium;
preferably, the auxiliary agent comprises any one of a phosphorus-containing auxiliary agent, a fluorine-containing auxiliary agent, a boron-containing auxiliary agent, a titanium-containing auxiliary agent or a zirconium-containing auxiliary agent or a combination of at least two of the phosphorus-containing auxiliary agent, the fluorine-containing auxiliary agent, the boron-containing auxiliary agent and the zirconium-containing auxiliary agent;
preferably, the mass percent of the heteroatom in the auxiliary agent is 1.0-10.0% based on the total mass of the supplementary refined catalyst being 100%;
preferably, the raw materials for preparing the catalyst carrier comprise pseudo-boehmite, a peptizing agent, an extrusion assistant and water;
preferably, the preparation method of the replenished and refined catalyst comprises the following steps:
mixing any one or the combination of at least two of active metal, active metal salt or active metal oxide with a solvent, an auxiliary agent, an oil phase and other additives to form the water-in-oil microemulsion;
impregnating the water-in-oil microemulsion into the catalyst carrier, drying and roasting, then impregnating the treated catalyst carrier into a solution containing any one or the combination of at least two of active metal, active metal salt or active metal oxide, and drying and roasting again to obtain the supplemented refined catalyst;
preferably, the preparation method of the catalyst carrier comprises the following steps: mixing pseudo-boehmite, a peptizing agent, an extrusion aid and water, and then sequentially carrying out forming, drying and roasting to obtain the catalyst carrier;
preferably, the oil phase comprises any one of n-octane, heptane or cyclohexane or a combination of at least two thereof;
preferably, the further additives comprise surfactants and/or cosurfactants.
7. The production method according to any one of claims 1 to 6, wherein in the step (3), the reaction pressure of the refining treatment is 8.0 to 10.0MPa;
preferably, the reaction temperature of the refining treatment is 290-360 ℃;
preferably, the volume ratio of the hydrogen gas to the hydrodewaxing produced oil (600-1200): 1;
preferably, the volume space velocity of the refining treatment is 0.3-2.0h -1 ；
Preferably, the reaction of the hydrotreating, hydrodewaxing treatment and refining treatment is independently single-stage medium-pressure hydrogenation;
preferably, the pressure of the single-stage medium-pressure hydrogenation is 8.0-10.0MPa;
preferably, the feedstock oil comprises any one of cycloalkyl normal second-line, cycloalkyl minus one-line or hydro-upgraded diesel or a combination of at least two thereof.
8. A transformer oil base oil, characterized in that it is prepared by the preparation method according to any one of claims 1 to 7;
in the transformer oil base oil, the sulfur content is less than 1.0mg/kg, the nitrogen content is less than 1.0mg/kg, the total aromatic hydrocarbon is less than 10 percent, and the pour point is less than-57 ℃.
9. A method for producing naphtha, characterized by comprising the steps of:
(1) Mixing raw oil with hydrogen, and carrying out hydrotreatment to obtain hydrotreatment generated oil;
(2) Mixing the hydro-processing generated oil with hydrogen, and carrying out hydro-dewaxing treatment under the action of a hydro-dewaxing catalyst to obtain hydro-dewaxing generated oil;
(3) And mixing the hydrodewaxing produced oil with hydrogen, refining, and fractionating at the temperature of less than 215 ℃ to obtain the naphtha.
10. The preparation method of the base oil of the drilling fluid lubricant is characterized by comprising the following steps:
(1) Mixing raw oil with hydrogen, and carrying out hydrotreatment to obtain hydrotreatment generated oil;
(2) Mixing the hydroprocessing produced oil with hydrogen, and carrying out hydrodewaxing treatment under the action of a hydrodewaxing catalyst to obtain the hydrodewaxing produced oil;
(3) And mixing the hydrodewaxing produced oil with hydrogen, refining, and fractionating at 215-275 ℃ to obtain the base oil of the drilling fluid lubricant.
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| CN106311263A (en) * | 2016-07-29 | 2017-01-11 | 武汉凯迪工程技术研究总院有限公司 | Highly-supported modified boron hydrofining catalyst and the preparation method thereof |
| CN106833740A (en) * | 2015-12-04 | 2017-06-13 | 中国石油天然气股份有限公司 | A kind of preparation method of transformer oil base oil |
| CN111841560A (en) * | 2019-04-25 | 2020-10-30 | 中国海洋石油集团有限公司 | Hydrotreating catalyst and preparation method and application thereof |
| CN112625773A (en) * | 2019-10-09 | 2021-04-09 | 中国海洋石油集团有限公司 | Preparation method of transformer oil base oil |
| CN114410347A (en) * | 2021-12-13 | 2022-04-29 | 中海油天津化工研究设计院有限公司 | Method for preparing low-aromatic transformer oil by medium-pressure hydrogenation of naphthenic base distillate oil |
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2022
- 2022-09-23 CN CN202211164676.5A patent/CN115404102A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106833740A (en) * | 2015-12-04 | 2017-06-13 | 中国石油天然气股份有限公司 | A kind of preparation method of transformer oil base oil |
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| CN111841560A (en) * | 2019-04-25 | 2020-10-30 | 中国海洋石油集团有限公司 | Hydrotreating catalyst and preparation method and application thereof |
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