CN114522692A - Heavy oil hydrotreating catalyst and heavy oil hydrotreating method - Google Patents
Heavy oil hydrotreating catalyst and heavy oil hydrotreating method Download PDFInfo
- Publication number
- CN114522692A CN114522692A CN202011188999.9A CN202011188999A CN114522692A CN 114522692 A CN114522692 A CN 114522692A CN 202011188999 A CN202011188999 A CN 202011188999A CN 114522692 A CN114522692 A CN 114522692A
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- Prior art keywords
- aging
- catalyst
- alumina
- pseudoboehmite
- temperature
- Prior art date
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- Granted
Links
- 239000003054 catalyst Substances 0.000 title claims abstract description 90
- 238000000034 method Methods 0.000 title claims abstract description 70
- 239000000295 fuel oil Substances 0.000 title claims abstract description 32
- VXAUWWUXCIMFIM-UHFFFAOYSA-M aluminum;oxygen(2-);hydroxide Chemical compound [OH-].[O-2].[Al+3] VXAUWWUXCIMFIM-UHFFFAOYSA-M 0.000 claims abstract description 130
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims abstract description 95
- 238000002360 preparation method Methods 0.000 claims abstract description 65
- 229910052751 metal Inorganic materials 0.000 claims abstract description 44
- 239000002184 metal Substances 0.000 claims abstract description 44
- 239000011148 porous material Substances 0.000 claims abstract description 38
- 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 abstract description 33
- 229910052708 sodium Inorganic materials 0.000 claims abstract description 33
- 239000011734 sodium Substances 0.000 claims abstract description 33
- 230000032683 aging Effects 0.000 claims description 105
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 58
- 238000006243 chemical reaction Methods 0.000 claims description 52
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 46
- 239000000203 mixture Substances 0.000 claims description 36
- 239000001569 carbon dioxide Substances 0.000 claims description 33
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 33
- 238000001035 drying Methods 0.000 claims description 26
- 238000001354 calcination Methods 0.000 claims description 23
- 239000007787 solid Substances 0.000 claims description 20
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 18
- 239000003921 oil Substances 0.000 claims description 17
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 claims description 14
- 229910001388 sodium aluminate Inorganic materials 0.000 claims description 14
- 238000004537 pulping Methods 0.000 claims description 13
- 239000007788 liquid Substances 0.000 claims description 12
- 238000000926 separation method Methods 0.000 claims description 10
- 229910052759 nickel Inorganic materials 0.000 claims description 9
- 230000014759 maintenance of location Effects 0.000 claims description 7
- 239000010941 cobalt Substances 0.000 claims description 6
- 229910017052 cobalt Inorganic materials 0.000 claims description 6
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical group [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 6
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical group [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 claims description 3
- 229910052750 molybdenum Inorganic materials 0.000 claims description 3
- 239000011733 molybdenum Substances 0.000 claims description 3
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 claims description 3
- 229910052721 tungsten Inorganic materials 0.000 claims description 3
- 239000010937 tungsten Substances 0.000 claims description 3
- 239000013078 crystal Substances 0.000 abstract description 10
- 230000003197 catalytic effect Effects 0.000 abstract description 3
- 239000000047 product Substances 0.000 description 46
- 239000002002 slurry Substances 0.000 description 36
- 239000000084 colloidal system Substances 0.000 description 28
- 239000008367 deionised water Substances 0.000 description 27
- 229910021641 deionized water Inorganic materials 0.000 description 27
- 239000000243 solution Substances 0.000 description 27
- 239000007789 gas Substances 0.000 description 24
- 239000012065 filter cake Substances 0.000 description 16
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 14
- 230000000052 comparative effect Effects 0.000 description 13
- 239000011259 mixed solution Substances 0.000 description 13
- 238000005406 washing Methods 0.000 description 13
- 238000001914 filtration Methods 0.000 description 12
- 239000000843 powder Substances 0.000 description 11
- 150000001875 compounds Chemical class 0.000 description 9
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 8
- 241000219782 Sesbania Species 0.000 description 8
- 229910017604 nitric acid Inorganic materials 0.000 description 8
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 8
- VCNTUJWBXWAWEJ-UHFFFAOYSA-J aluminum;sodium;dicarbonate Chemical compound [Na+].[Al+3].[O-]C([O-])=O.[O-]C([O-])=O VCNTUJWBXWAWEJ-UHFFFAOYSA-J 0.000 description 7
- APUPEJJSWDHEBO-UHFFFAOYSA-P ammonium molybdate Chemical compound [NH4+].[NH4+].[O-][Mo]([O-])(=O)=O APUPEJJSWDHEBO-UHFFFAOYSA-P 0.000 description 7
- 229940010552 ammonium molybdate Drugs 0.000 description 7
- 235000018660 ammonium molybdate Nutrition 0.000 description 7
- 239000011609 ammonium molybdate Substances 0.000 description 7
- 239000007864 aqueous solution Substances 0.000 description 7
- 229910001647 dawsonite Inorganic materials 0.000 description 7
- 229910052757 nitrogen Inorganic materials 0.000 description 7
- 239000004033 plastic Substances 0.000 description 7
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 6
- 239000002994 raw material Substances 0.000 description 6
- 229910052717 sulfur Inorganic materials 0.000 description 6
- 239000011593 sulfur Substances 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- 238000007796 conventional method Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 238000005984 hydrogenation reaction Methods 0.000 description 5
- KKCBUQHMOMHUOY-UHFFFAOYSA-N sodium oxide Chemical compound [O-2].[Na+].[Na+] KKCBUQHMOMHUOY-UHFFFAOYSA-N 0.000 description 5
- 229910001948 sodium oxide Inorganic materials 0.000 description 5
- 239000012752 auxiliary agent Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000001125 extrusion Methods 0.000 description 4
- 238000005470 impregnation Methods 0.000 description 4
- KBJMLQFLOWQJNF-UHFFFAOYSA-N nickel(ii) nitrate Chemical compound [Ni+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O KBJMLQFLOWQJNF-UHFFFAOYSA-N 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 238000004458 analytical method Methods 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 238000004523 catalytic cracking Methods 0.000 description 3
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 3
- UFMZWBIQTDUYBN-UHFFFAOYSA-N cobalt dinitrate Chemical compound [Co+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O UFMZWBIQTDUYBN-UHFFFAOYSA-N 0.000 description 3
- 229910001981 cobalt nitrate Inorganic materials 0.000 description 3
- 230000002349 favourable effect Effects 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000002791 soaking Methods 0.000 description 3
- 150000004684 trihydrates Chemical class 0.000 description 3
- 229910052720 vanadium Inorganic materials 0.000 description 3
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 description 3
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- 241000640882 Condea Species 0.000 description 2
- 238000002441 X-ray diffraction Methods 0.000 description 2
- 239000000654 additive Substances 0.000 description 2
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 2
- 238000010009 beating Methods 0.000 description 2
- 229920002678 cellulose Polymers 0.000 description 2
- 239000001913 cellulose Substances 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 238000000975 co-precipitation Methods 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 239000003292 glue Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- 238000005457 optimization Methods 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 229910052710 silicon Inorganic materials 0.000 description 2
- 239000010703 silicon Substances 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 238000004846 x-ray emission Methods 0.000 description 2
- 238000004876 x-ray fluorescence Methods 0.000 description 2
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 229920000881 Modified starch Polymers 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- 101000892301 Phomopsis amygdali Geranylgeranyl diphosphate synthase Proteins 0.000 description 1
- -1 VIB metal compound Chemical class 0.000 description 1
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- 230000029936 alkylation Effects 0.000 description 1
- 238000005804 alkylation reaction Methods 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 229910001570 bauxite Inorganic materials 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 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
- 238000004939 coking Methods 0.000 description 1
- 239000002872 contrast media Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000007323 disproportionation reaction Methods 0.000 description 1
- 125000001495 ethyl group Chemical group [H]C([H])([H])C([H])([H])* 0.000 description 1
- 238000011066 ex-situ storage Methods 0.000 description 1
- 230000002431 foraging effect Effects 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- 238000009616 inductively coupled plasma Methods 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 150000007529 inorganic bases Chemical class 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000011159 matrix material Substances 0.000 description 1
- 150000002736 metal compounds Chemical class 0.000 description 1
- 229910052976 metal sulfide Inorganic materials 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 235000019426 modified starch Nutrition 0.000 description 1
- MEFBJEMVZONFCJ-UHFFFAOYSA-N molybdate Chemical compound [O-][Mo]([O-])(=O)=O MEFBJEMVZONFCJ-UHFFFAOYSA-N 0.000 description 1
- 229910000476 molybdenum oxide Inorganic materials 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 150000007530 organic bases Chemical class 0.000 description 1
- PQQKPALAQIIWST-UHFFFAOYSA-N oxomolybdenum Chemical compound [Mo]=O PQQKPALAQIIWST-UHFFFAOYSA-N 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000013500 performance material Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 238000005096 rolling process Methods 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 238000007493 shaping process Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000004227 thermal cracking Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- PBYZMCDFOULPGH-UHFFFAOYSA-N tungstate Chemical compound [O-][W]([O-])(=O)=O PBYZMCDFOULPGH-UHFFFAOYSA-N 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Classifications
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- 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
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/85—Chromium, molybdenum or tungsten
- B01J23/88—Molybdenum
- B01J23/882—Molybdenum and cobalt
-
- 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
- B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
- B01J21/02—Boron or aluminium; Oxides or hydroxides thereof
- B01J21/04—Alumina
-
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- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/85—Chromium, molybdenum or tungsten
- B01J23/88—Molybdenum
- B01J23/883—Molybdenum and nickel
-
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- B01J35/40—Catalysts, in general, characterised by their form or physical properties characterised by dimensions, e.g. grain size
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- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
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- B01J35/615—100-500 m2/g
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- B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
- B01J35/63—Pore volume
- B01J35/635—0.5-1.0 ml/g
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
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- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
- B01J35/64—Pore diameter
- B01J35/647—2-50 nm
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F7/00—Compounds of aluminium
- C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
- C01F7/34—Preparation of aluminium hydroxide by precipitation from solutions containing aluminium salts
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F7/00—Compounds of aluminium
- C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
- C01F7/44—Dehydration of aluminium oxide or hydroxide, i.e. all conversions of one form into another involving a loss of water
- C01F7/441—Dehydration of aluminium oxide or hydroxide, i.e. all conversions of one form into another involving a loss of water by calcination
-
- 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
- C10G45/06—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 nickel or cobalt metal, or compounds thereof
- C10G45/08—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 nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/12—Surface area
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/14—Pore volume
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/16—Pore diameter
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/205—Metal content
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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Abstract
The invention relates to a heavy oil hydrotreating catalyst and a heavy oil hydrotreating method, wherein the catalyst comprises an alumina carrier and at least one metal component selected from VIII group and at least one metal component selected from VIB group which are loaded on the carrier, wherein the alumina carrier is prepared from high-crystallinity and large-grain pseudoboehmite, the relative crystallinity of the pseudoboehmite is higher than 65%, the grain size is 2-5nm, and the sodium content is not higher than 0.08 wt% based on the dry weight of the pseudoboehmite and calculated by oxide. The heavy oil hydrotreating catalyst provided by the invention adopts a carrier prepared from pseudoboehmite with high crystallinity and large crystal grains, and the alumina and the carrier prepared from the pseudoboehmite have the characteristics of high pore volume, large pore diameter and high specific surface area, and are particularly suitable for hydrotreating heavy oil. Compared with the prior art, the preparation cost of the carrier and the catalyst is greatly reduced, and when the catalyst is applied to heavy oil hydrotreating, the catalytic performance is superior to that of the existing catalyst.
Description
Technical Field
The invention relates to a hydrotreating catalyst and application thereof, in particular to a heavy oil hydrotreating catalyst and a heavy oil hydrotreating method.
Background
With the increasing shortage of petroleum resources, the contradiction between crude oil heaving and product lightening is increasingly sharp, and oil refining enterprises in various countries around the world are vigorously developing the catalytic cracking (RFCC) technology of blended or refined residual oil and the thermal cracking technology of coking and the like, wherein the RFCC technology becomes the most effective technology for lightening heavy oil. The alumina carrier is an important component of the catalyst cost, and the reduction of the preparation cost of the alumina carrier can greatly reduce the cost of the catalyst, thereby improving the market competitiveness.
Sodium metaaluminate (or sodium aluminate) -carbon dioxide process is one of the common methods for preparing pseudoboehmite and gamma-alumina. The method can combine the industrial practical situation of an aluminum factory, can use sodium metaaluminate (or sodium aluminate) solution produced by bauxite and carbon dioxide waste gas as raw materials to prepare the pseudoboehmite and the gamma-alumina, and is a cheap method, so the method has wide industrial application. The preparation of pseudoboehmite by sodium metaaluminate (or sodium aluminate) -carbon dioxide method generally includes two processes of glue formation and aging. In the prior art, the pH value of the final point of the gelling (or neutralizing) reaction of sodium metaaluminate (or sodium aluminate) solution and carbon dioxide is controlled to be about 10.5, and the gelling reaction is carried out under the condition of high pH value, so that pseudo-boehmite with higher crystallinity can be obtained, but the pore volume of gamma-alumina obtained after roasting is smaller and is generally less than 0.5 ml/g. This greatly limits the application of the catalyst in distillate oil hydrogenation, especially in heavy oil and residual oil hydrogenation catalysts.
CN103449485A discloses a method for continuously producing pseudoboehmite, which comprises the steps of continuously adding a sodium metaaluminate solution with the concentration of 15-80 g alumina/L into a reaction device, simultaneously introducing air-carbon dioxide mixed gas containing more than 30 volume percent of carbon dioxide for full mixing, controlling the flow rate of the mixed gas and the sodium metaaluminate solution to ensure that the reaction temperature is 25-55 ℃ and the pH value is 9.5-11, aging slurry after passing through a pipeline with a plurality of U-shaped pipes, wherein the aging temperature is not lower than 90 ℃, filtering and washing the aged slurry to be neutral, and drying a filter cake after washing with water at the temperature of 100-120 ℃ to obtain the pseudoboehmite. The process provides for the alumina obtained in the examples to have a pore volume in the range of 0.30 to 0.33 ml/g.
CN1091428C discloses a method for preparing pseudoboehmite, which uses sodium metaaluminate solution with the concentration of 5-120 g alumina/l to contact with gas with the carbon dioxide content of more than 20 vol% to gelatinize in a batch or continuous mode, the gelatinizing temperature is 10-100 ℃, the pH value of the gelatinizing end point (or process) is 6-9.5, and the gelatinizing reaction time or the retention time is not more than 40 minutes. After the colloid formation is finished, one or more of inorganic base, organic base and their water solution are added to raise the pH value of slurry to 9.5-11.5 or quickly make solid-liquid separation and washing. The method can be used for preparing the fibrous pseudo-boehmite with high crystallinity, and the pore volume of the gamma-alumina formed after roasting is between 0.5 and 2.0 ml/g. However, in order to avoid the formation of dawsonite at a lower pH value of the gelling end point (or process), an alkaline substance needs to be added in the aging process or solid-liquid separation is carried out immediately after gelling and then washing is carried out for aging, and the method is harsh in conditions and is not suitable for industrial production.
The alumina prepared from the pseudo-boehmite obtained by the existing preparation method has smaller pore diameter and pore volume, and is not suitable for being used as a carrier of a heavy oil hydrotreating catalyst; or the conditions are harsh, the cost is high, and the method is not suitable for industrial production.
Disclosure of Invention
The invention aims to provide a heavy oil hydrotreating catalyst and a heavy oil hydrotreating method. Specifically, the present invention includes the following:
the invention provides a heavy oil hydrotreating catalyst, which comprises an alumina carrier and at least one metal component selected from VIII group and at least one metal component selected from VIB group loaded on the carrier, wherein the alumina carrier is prepared from high-crystallinity and large-grain pseudo-boehmite, the relative crystallinity of the pseudo-boehmite is higher than 65%, the grain size is 2-5nm, and the sodium content of the pseudo-boehmite is not higher than 0.08 wt% on the basis of the dry weight of the pseudo-boehmite and calculated by oxide.
The invention also provides a heavy oil hydrotreating method, which comprises the step of carrying out contact reaction on heavy raw oil and the catalyst under the hydrotreating reaction condition.
The heavy oil hydrotreating catalyst provided by the invention adopts a carrier prepared from pseudo-boehmite with high crystallinity and large crystal grains, compared with the prior art, the preparation cost of the carrier and the catalyst is greatly reduced, and when the catalyst is applied to heavy oil hydrotreating, the catalytic performance is superior to the level of the existing catalyst.
Detailed Description
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.
In the present invention, room temperature means 25 ℃ unless otherwise specified.
As previously mentioned, the present invention provides a heavy oil hydroprocessing catalyst in which the hydrogenation-active metal component is conventionally selected, for example, the group VIII metal component can be cobalt and/or nickel, the group VIB metal component can be molybdenum and/or tungsten; the carrier and metal content of the catalyst are conventional, and generally, the content of the VIII group metal component is 0.5-10 wt%, preferably 1.5-5 wt%, and the content of the VIB group metal component is 5-35 wt%, preferably 6-30 wt%, calculated by oxide and based on the catalyst; the balance being the balance of the carrier.
The catalyst adopts a carrier prepared from pseudoboehmite with high crystallinity and large crystal grains, the relative crystallinity of the pseudoboehmite is higher than 65%, the crystal grain size is 2-5nm, and the sodium content is not higher than 0.08 wt% by taking the dry basis weight of the pseudoboehmite as the reference and calculating by oxide. Preferably, the relative crystallinity of the pseudoboehmite is 65 to 95%, preferably 70 to 90% by weight, the crystal grain size is 3 to 4.5nm, preferably 3.3 to 4nm, and the sodium content in terms of oxide is not more than 0.06% by weight, preferably 0.01 to 0.05% by weight, based on the dry weight of the pseudoboehmite.
The invention provides a preferable method for preparing the pseudoboehmite, which comprises the following steps:
(1) contacting sodium metaaluminate and/or sodium aluminate solution with gas containing carbon dioxide to carry out gelling reaction to obtain solid gelling product;
(2) sequentially carrying out first aging and second aging on the solid gelling product to obtain an aged mixture; the temperature of the second aging is higher than that of the first aging;
(3) and carrying out solid-liquid separation on the aged mixture to obtain a solid aged product, and drying the solid aged product to obtain the pseudoboehmite.
The inventor of the invention finds that the pseudoboehmite with better quality can be obtained by changing the aging process on the basis of the prior art without adding additives (such as soluble cellulose derivatives and soluble starch derivatives), namely, after two-stage aging of the solid gelling product. The two-stage aging comprises the steps of carrying out first aging on a solid colloid-forming product at a lower temperature, then heating for carrying out second aging, wherein the alumina prepared by roasting the pseudoboehmite obtained by the method has larger pore volume and pore diameter, and a carrier prepared by taking the pseudoboehmite as a raw material has high specific surface area and large pore diameter, and is particularly suitable for a carrier of a heavy oil and residual oil hydrogenation catalyst. Compared with the catalyst prepared by similar pseudo-boehmite or alumina obtained by other methods in the prior art, the catalyst of the invention not only has better performance than the prior art, but also has lower cost and more moderate conditions for preparing the pseudo-boehmite.
According to the invention, preferably, the gelling reaction in step (1) is carried out in a continuous or batch manner. Further preferably, the gelling reaction is carried out in a continuous manner. On one hand, the gelling reaction is carried out in a continuous mode, which is more favorable for controlling the pH value in the gelling reaction process, thereby being more favorable for improving the quality of the pseudoboehmite, and on the other hand, the continuous operation can increase the treatment capacity in unit time and improve the production benefit.
According to a preferred embodiment of the present invention, the contacting of step (1) comprises: the sodium metaaluminate and/or sodium aluminate solution is contacted with a carbon dioxide-containing gas in continuous countercurrent. In this case, it is advantageous to improve the quality of the pseudoboehmite.
The equipment for the gelling reaction is not particularly limited in the present invention and may be selected conventionally in the art. In particular, it can be carried out, for example, in a gel-forming pot.
According to a preferred embodiment of the present invention, the process for carrying out the gel-forming reaction in a continuous manner according to the present invention comprises: adding a certain amount of deionized water into the gelling tank in advance, introducing the gas containing carbon dioxide from the bottom of the gelling tank, and simultaneously introducing the sodium metaaluminate and/or sodium aluminate solution from the top of the gelling tank, so that the sodium metaaluminate and/or sodium aluminate solution is continuously in countercurrent contact with the gas containing carbon dioxide, the slurry generated by gelling reaction continuously flows out of the gelling tank, and the liquid level in the gelling tank is controlled to be constant.
In the present invention, the conditions of the gelling reaction are selected widely, and preferably, the conditions of the gelling reaction include: the pH value is 7-10, the retention time is 2-60min, and the temperature is 30-95 ℃.
According to a preferred embodiment of the present invention, the conditions of the gelling reaction include: the pH value is 7.5-9.5, the retention time is 7-50min, and the temperature is 35-85 ℃. In this preferred embodiment, it is more advantageous to improve the quality of the pseudo-boehmite. In the present invention, the pH during the gelling reaction is not too low, for example not lower than 7. Because the lower pH value in the gelling reaction process easily causes the generation of dawsonite which is insoluble in water and cannot be removed in the subsequent process, the content of sodium oxide in the pseudo-boehmite is higher, and the quality of the product is influenced; the pH during the gelling reaction should also not be too high, for example not higher than 10. Because the alumina trihydrate seed crystal is easily generated due to the higher pH value in the gelling reaction process, and the alumina trihydrate seed crystal can continue to grow in the subsequent aging process, the content of the alumina trihydrate of the product is higher, the pore volume and the specific surface area of the alumina product are low, and the quality of the product is influenced.
In the present invention, the concentration range of the sodium metaaluminate and/or sodium aluminate solution is selected widely, preferably, the concentration of the sodium metaaluminate and/or sodium aluminate solution is 5-40g/L, preferably 8-35g/L, calculated by alumina.
In the present invention, the content of carbon dioxide in the carbon dioxide containing gas is selected in a wide range, for example, the content of carbon dioxide in the carbon dioxide containing gas may be more than 5% by volume. In order to increase the reaction efficiency, it is preferable that the carbon dioxide-containing gas contains carbon dioxide in an amount of more than 20 vol%, preferably more than 30 vol%, and more preferably 30 to 100 vol%. In the present embodiment, the example of 99 vol% is given as an example, and the present invention is not limited thereto. In addition, the carbon dioxide-containing gas may contain an inert gas including, but not limited to, at least one of nitrogen, argon, and helium, or air in addition to carbon dioxide.
According to the invention, after the gelling reaction, the step (1) further comprises the step of carrying out solid-liquid separation on the product of the gelling reaction to obtain the solid gelling product. In the present invention, the solid-liquid separation is a conventional operation in the art, and specifically, may be at least one of sedimentation, filtration and centrifugal separation, for example. The skilled person can select them as required according to the actual need.
According to a preferred embodiment of the invention, the temperature of the second ageing is 10-100 c, preferably 25-85 c, more preferably 45-60 c higher than the temperature of the first ageing. The preferred embodiment is more favorable for further improving the pore volume and the pore diameter of the alumina prepared from the pseudo-boehmite.
On the basis that the temperature for the second aging is higher than the temperature for the first aging, the selection range of the conditions for the first aging and the second aging is wide, and in order to further preferably optimize the structural characteristics of the pseudoboehmite, the conditions for the first aging preferably include: the temperature is 0-45 ℃, preferably 10-40 ℃, and more preferably 30-40 ℃; the time is 2 to 240 hours, preferably 4 to 120 hours, more preferably 12 to 120 hours. The inventors of the present invention have found that the average pore diameter and pore volume of the alumina obtained by calcining the prepared pseudo-boehmite can be more controlled by controlling the conditions of the first aging including temperature and time.
According to the present invention, preferably, the conditions of the second aging include: the temperature is 50-100 ℃, preferably 65-95 ℃; the time is 1-24h, preferably 2-12 h. In this preferred case, it is more advantageous to improve the quality of the pseudoboehmite.
According to the invention, preferably, the first ageing and/or the second ageing is carried out in the presence of water.
In order to avoid the introduction of impurities, which may affect the alumina and the catalyst obtained subsequently, the water used in the preparation process of the present invention is preferably deionized water.
According to a preferred embodiment of the present invention, the step (2) comprises: and (3) carrying out first aging on the solid gelling product to obtain a first aged product, adding water (preferably deionized water) into the first aged product, pulping, and carrying out second aging to obtain an aged mixture. According to the present invention, it is preferred that the amount of water is such that the concentration of the slurry obtained after beating is 20 to 200g/L, preferably 50 to 150g/L, in terms of alumina.
According to a preferred embodiment of the present invention, the step (2) comprises: adding water (preferably deionized water) into the solid gelling product, pulping, performing first aging to obtain a first aged product, and performing second aging on the first aged product to obtain an aged mixture. In the present invention, the amount of water is such that the concentration of the slurry obtained after beating is 20 to 200g/L, preferably 50 to 150g/L, in terms of alumina.
In the present invention, the specific operation of the first aging and/or the second aging can be selected by those skilled in the art according to actual needs, for example, the process of the first aging and/or the second aging can also be performed under stirring conditions and/or ultrasonic conditions. In the present invention, the equipment for carrying out the first aging and/or the second aging is not particularly limited, and may be a conventional choice in the art, and specifically, may be carried out in an aging tank, for example.
In the present invention, the solid-liquid separation in step (3) is not particularly limited, and specifically, for example, at least one of sedimentation, filtration and centrifugal separation may be used, and those skilled in the art may select the solid-liquid separation according to actual needs.
According to the present invention, preferably, step (3) further comprises washing the solid aged product before the drying. In the present invention, the washing operation may be a conventional operation in the art, and a person skilled in the art may select the washing operation as needed according to actual needs, so long as the content of impurity ions in the solid aged product can be reduced, for example, the content of sodium oxide in the alumina obtained by calcining the pseudoboehmite is less than 0.1 wt%, preferably less than 0.06 wt%, and more preferably 0.01 to 0.05 wt%.
In the present invention, the drying is a conventional operation in the art as long as it is capable of removing free water contained in the pseudo-boehmite. The drying conditions are selected in a wide range, the drying temperature can be between room temperature and the crystal transformation temperature of the pseudo-boehmite, preferably, the drying temperature is 60-200 ℃, and more preferably 100-180 ℃.
The pseudoboehmite prepared by the method has larger grain size and lower sodium oxide content. Preferably, no dawsonite is detected in the pseudoboehmite prepared by the method of the invention, indicating that the pseudoboehmite prepared by the method of the invention does not contain or contains a very small amount (less than the lowest value detected) of dawsonite.
Therefore, the relative crystallinity (based on commercial SB powder from Condea) of the pseudoboehmite obtained in the step (3) is preferably 65 to 95% by weight, more preferably 70 to 90% by weight, and the crystal grain size is 3 to 4.5 nm; the grain size of the pseudoboehmite is preferably 3.3-4 nm.
In the present invention, the relative crystallinity, grain size and dawsonite content of the pseudoboehmite can be determined by X-ray diffraction (XRD).
Preferably, the sodium content is 0.01-0.05 wt% in terms of oxide based on the dry weight of the pseudoboehmite, which means the weight of the pseudoboehmite calcined at 550 ℃ for 5 hours.
According to the invention, the pseudoboehmite used as the raw material of the carrier can obtain alumina with high pore volume, preferably gamma alumina after being roasted. The obtained alumina has a pore volume of 0.8-1.3mL/g, an average pore diameter of more than 14nm, and a specific surface area of 200-260m2(ii)/g; preferably, the alumina pore volume obtained by roasting the pseudo-boehmite is 0.9-1.2mL/g, the average pore diameter is more than 15nm, and the specific surface area is 210-255m2(iv) g; the roasting conditions comprise: the temperature is 500-1200 ℃, and the time is 2-8 hours; preferably, the conditions of the calcination include: the temperature is 550-850 ℃, and the time is 3-6 hours. In the prior art, under the condition of not adding other additives, the pore volume of alumina obtained by roasting pseudo-boehmite prepared by a sodium metaaluminate (or sodium aluminate) -carbon dioxide method is generally less than 0.5 ml/g. According to a preferred embodiment of the present invention, the average pore diameter of the alumina is 16-20nm, and the specific surface area of the alumina is 210-255m2(ii) in terms of/g. In this preferred case, the alumina has better performance and is used as a raw materialThe thin aluminum hydroxide is more suitable as a carrier raw material of a heavy oil hydrotreating catalyst. The pore volume, average pore diameter and specific surface area of the alumina can be measured by a low-temperature nitrogen adsorption method.
The method for preparing the alumina carrier by adopting the pseudo-boehmite is a conventional method, for example, the pseudo-boehmite is mixed with other substances and then is extruded and molded, or the pseudo-boehmite can not be molded. In the present invention, the shaping method can be selected conventionally in the art, for example, the pseudoboehmite can be mixed with a proper amount of water (preferably deionized water), extruded and shaped, or the pseudoboehmite can be mixed with a proper amount of extrusion aid and/or adhesive and a proper amount of water (preferably deionized water) and then extruded and shaped. In the present invention, the extrusion aid and the peptizing agent can be used in the types and the amounts commonly used in the field.
The alumina carrier obtained by the method has the characteristics of large specific surface area and high pore volume, and the specific surface area of the alumina carrier is 200-300m2Per g, preferably 220-280m2The pore volume is more than 0.6mL/g, preferably 0.65-0.75mL/g, and the most probable pore diameter is 7.5-12nm, preferably 8-11 nm.
The alumina carrier prepared in the above steps can be used as an adsorbent or a catalyst, and particularly can be used as a carrier or a matrix of a catalyst in hydrotreating, hydrocracking, catalytic cracking, reforming, isomerization, alkylation, disproportionation and the like, and is particularly suitable for preparing the heavy oil hydrotreating catalyst.
The catalysts provided by the present invention may be prepared by methods conventional in the art, for example, the preparation method comprises: preparing a shaped alumina support and introducing at least one metal component selected from group VIII and at least one metal component selected from group VIB into the alumina support. The molding can be carried out by conventional methods such as tabletting, rolling, extruding and the like. In order to ensure the smooth process of the forming, it is usually necessary to introduce an auxiliary agent, water and the like into the material (here, pseudo-boehmite) during the forming, for example, when the strip extrusion method is adopted for forming, the pseudo-boehmite is mixed with a proper amount of water, a peptizer (such as one or more selected from nitric acid, acetic acid and citric acid), and an extrusion aid (such as one or more selected from sesbania powder and cellulose), and then the mixture is extruded and formed. And drying and roasting the formed product to obtain the carrier. The drying is carried out by conventional methods such as drying by using an oven, a mesh belt kiln and a fluidized bed, and when the drying is carried out by a heating method, the drying temperature is preferably 50 to 200 ℃ and the drying time is 0.3 to 6 hours, and further preferably 60 to 150 ℃ and the drying time is 0.5 to 2 hours. The roasting method and conditions are the conventional method and conditions for preparing the catalyst carrier, such as roasting by a mesh belt kiln, a vertical test furnace and a converter, and the roasting condition is preferably roasting at the temperature of 400-1200 ℃ for 1-6 hours, and further preferably roasting at the temperature of 500-1100 ℃ for 2-4 hours.
Any of the known hydrogenation-type catalyst preparation methods can be used, provided that it is sufficient to support the at least one group VIB and at least one group VIII metal component on the alumina. For example, the support may be contacted with a solution containing an effective amount of a compound containing a nickel and/or cobalt metal component selected from group VIII under conditions sufficient to deposit an effective amount of the nickel and/or cobalt metal component selected from group VIII on the support, such as by impregnation, co-precipitation, and the like, preferably impregnation, followed by drying, calcining or non-calcining. The drying conditions are those customary for the preparation of such catalysts, for example drying temperatures of from 80 to 350 ℃ and preferably from 100 to 300 ℃ for drying times of from 1 to 24 hours and preferably from 2 to 12 hours. When the catalyst needs to be calcined, the temperature is preferably 100-700 ℃, the calcination time is 1-6 hours, the further preferred temperature is preferably 200-500 ℃, and the calcination time is 2-4 hours.
The VIII group metal compound is selected from one or more VIII group metal soluble compounds, such as one or more of nitrate, acetate, soluble carbonate, chloride and soluble complex of cobalt and/or nickel metal.
The group VIB metal compound is selected from one or more of group VIB metal soluble compounds, such as one or more of molybdate, tungstate, metatungstate and ethyl metatungstate.
The catalyst according to the present invention is provided in which the content of at least one metal component selected from group VIII and at least one metal component selected from group VIB is the conventional content of heavy oil hydrotreating catalysts. In a preferred embodiment, the group VIII metal component is preferably cobalt and/or nickel, the group VIB metal component is molybdenum and/or tungsten, and the group VIII metal component is preferably contained in an amount of 0.5 to 10 wt%, more preferably 1.5 to 5 wt%, and the group VIB metal component is preferably contained in an amount of 5 to 35 wt%, more preferably 6 to 30 wt%, calculated as oxides and based on the catalyst.
The catalyst provided according to the present invention may further contain any substance that does not affect or can improve the catalytic performance of the catalyst provided by the present invention. If components such as silicon can be incorporated, the above-mentioned auxiliaries are incorporated in an amount of 0 to 10% by weight, preferably 0.5 to 5% by weight, calculated as the element and based on the catalyst.
When the catalyst also contains components such as silicon and the like, the introduction method can be that the compound containing the auxiliary agent is directly mixed with the pseudo-boehmite, formed and roasted; the compound containing the auxiliary agent and the compound containing the hydrogenation active metal component are prepared into a mixed solution and then are contacted with the alumina carrier; or preparing a compound containing the auxiliary agent into a solution separately, and then contacting the solution with the alumina carrier and roasting the solution. When the promoter and the second hydrogenation-active metal are introduced separately into the alumina support, it is preferable to first contact the alumina support with a solution containing a promoter compound and calcine it, and then contact it with a solution containing a compound of the hydrogenation-active metal component, for example, by ion exchange, impregnation, coprecipitation, etc., preferably impregnation, at a calcination temperature of 250-600 deg.C, preferably 350-500 deg.C, for a calcination time of 2-8 hours, preferably 3-6 hours.
The invention also provides a heavy oil hydrotreating method, which comprises the step of contacting heavy oil with the hydrogenation catalyst under heavy oil hydrotreating conditions. According to the method provided by the invention, the additionThe hydrotreating reaction conditions are the reaction conditions customary for hydrotreating heavy feed oils, and in a preferred embodiment are: the reaction temperature is 300-550 ℃, the further optimization is 330-480 ℃, the hydrogen partial pressure is 4-20 MPa, the further optimization is 6-18 MPa, and the volume space velocity is 0.1-3.0 hours-1More preferably 0.15 to 2 hours-1The hydrogen-oil volume ratio is 200-.
The hydrotreating reaction apparatus may be carried out in any reactor vessel sufficient for the feedstock oil to contact react with the catalyst under hydrotreating reaction conditions, for example, in the fixed bed reactor, moving bed reactor or ebullating bed reactor.
The hydroprocessing catalyst may be presulfided prior to use with sulfur, hydrogen sulfide or sulfur-containing feedstock, typically in the presence of hydrogen at a temperature of 140 ℃ and 370 ℃, either ex situ or in situ, to convert its supported active metal component to a metal sulfide component, according to conventional methods in the art. The catalyst provided by the invention is suitable for heavy oil, especially poor-quality residual oil, to be subjected to hydrotreating so as to remove sulfur, nitrogen and metals in the heavy oil. So as to provide qualified raw oil for subsequent processes (such as a catalytic cracking process).
The following examples further illustrate the invention.
The reagents used in the examples were all chemically pure reagents except where specifically indicated.
In the following preparation examples, the crystallinity, crystal grain size and dawsonite content of pseudo-boehmite, which is a relative crystallinity, were measured by X-ray diffraction (XRD) using aluminum hydroxide produced by Condea, germany, having a designation SB, as a standard sample, and the crystallinity of SB was 100%, and measured on a D5005 type diffractometer, Siemens, germany. The sodium oxide content was measured by X-ray fluorescence spectroscopy (XRF) on a 3271 type X-ray fluorescence spectrometer manufactured by Nippon chemical industries, Ltd. The specific surface area and pore volume were measured by using a nitrogen adsorption apparatus model ASAP2420 manufactured by Micrometrics corporation, USA.
Preparation example 1
The preparation of pseudo-boehmite and alumina is carried out according to the method provided by the invention, and the specific steps are as follows:
(1) adding 3L of deionized water into a colloid forming tank in advance, introducing carbon dioxide-containing gas (the mixed gas of carbon dioxide with the content of 99 vol% and air) from the bottom of the colloid forming tank, introducing a sodium metaaluminate solution from the upper part of the colloid forming tank, enabling the sodium metaaluminate solution to be in countercurrent contact with the carbon dioxide-containing gas for carrying out colloid forming reaction, enabling slurry after the colloid forming reaction to flow out of an overflow pipe of the colloid forming tank, keeping the liquid level in the colloid forming tank unchanged, starting slurry collection after the deionized water which is added in advance is replaced by the slurry after the colloid forming reaction, and then filtering to obtain a filter cake (solid colloid forming product);
wherein the concentration (calculated by alumina) of the sodium metaaluminate solution is 30g/L, the flow rate is 60mL/min, and the retention time is 50 minutes; adjusting the gas dosage to make the pH value of the gelling reaction process about 7.5; the temperature of the gelling reaction is 35 ℃;
(2) carrying out first aging on the filter cake, wherein the temperature of the first aging is 35 ℃ and the time is 24 hours, so as to obtain a first aging product, adding deionized water into the first aging product, pulping to obtain slurry, wherein the concentration of the slurry is 100g/L in terms of aluminum oxide, and then carrying out second aging, wherein the temperature of the second aging is 90 ℃ and the time is 2 hours, so as to obtain an aging mixture;
(3) filtering and washing the aged mixture in sequence (the amount of washing water (deionized water) is 100 times of the mass of a product obtained by filtering), and drying at 120 ℃ for 8 hours;
obtaining pseudo-boehmite N1(ii) a Calcining the obtained pseudoboehmite at 550 ℃ for 5h to obtain alumina A1The specific physicochemical properties are shown in Table 1.
Preparation of comparative example 1
The preparation of pseudo-boehmite and alumina was carried out according to the method of preparation example 1 except that, in the step (2), the filter cake was directly mixed with deionized water without first aging and beaten to obtain a slurry having a concentration of 100g/L in terms of alumina, and then aged at 90 ℃ for 2 hours to obtain pseudo-boehmiteStone DN1And alumina DA1The specific physicochemical properties are shown in Table 1.
Preparation example 2
The preparation of pseudo-boehmite and alumina is carried out according to the method provided by the invention, and the specific steps are as follows:
(1) same as in step (1) of preparation example 1;
(2) carrying out first aging on the filter cake, wherein the temperature of the first aging is 30 ℃ and the time is 240 hours, so as to obtain a first aging product, adding deionized water into the first aging product, pulping to obtain slurry, wherein the concentration of the slurry is 100g/L in terms of aluminum oxide, and then carrying out second aging, wherein the temperature of the second aging is 90 ℃ and the time is 2 hours, so as to obtain an aging mixture;
(3) same as in preparation example 1, step (3);
obtaining pseudo-boehmite N2(ii) a Calcining the obtained pseudoboehmite at 550 ℃ for 5h to obtain alumina A2The specific physicochemical properties are shown in Table 1.
Preparation example 3
The preparation of pseudo-boehmite and alumina is carried out according to the method provided by the invention, and the specific steps are as follows:
(1) same as in step (1) of preparation example 1;
(2) adding deionized water into the filter cake, pulping to obtain slurry, wherein the concentration of the slurry is 100g/L in terms of aluminum oxide, and then carrying out first aging at the temperature of 45 ℃ for 12 hours to obtain a first aged product; secondly, carrying out secondary ageing on the first aged product, wherein the temperature of the secondary ageing is 90 ℃, and the time is 2 hours, so as to obtain an aged mixture;
(3) same as in preparation example 1, step (3);
obtaining pseudo-boehmite N3(ii) a Calcining the obtained pseudoboehmite at 550 ℃ for 5h to obtain alumina A3Specific physicochemical properties are shown in Table 1.
Preparation example 4
The preparation of pseudo-boehmite and alumina is carried out according to the method provided by the invention, and the specific steps are as follows:
(1) adding 3L of deionized water into a colloid forming tank in advance, introducing carbon dioxide-containing gas (the mixed gas of carbon dioxide with the content of 99 vol% and air) from the bottom of the colloid forming tank, introducing a sodium metaaluminate solution from the upper part of the colloid forming tank, enabling the sodium metaaluminate solution to be in countercurrent contact with the carbon dioxide-containing gas for carrying out colloid forming reaction, enabling slurry after the colloid forming reaction to flow out of an overflow pipe of the colloid forming tank, keeping the liquid level in the colloid forming tank unchanged, starting slurry collection after the deionized water which is added in advance is replaced by the slurry after the colloid forming reaction, and then filtering to obtain a filter cake (solid colloid forming product);
wherein the concentration of the sodium metaaluminate solution (calculated by alumina) is 10g/L, the flow rate is 300mL/min, and the retention time is 10 minutes; adjusting the gas dosage to make the pH value of the gelling reaction process about 8.8; the temperature of the gelling reaction is 55 ℃;
(2) carrying out first aging on the filter cake, wherein the temperature of the first aging is 40 ℃ and the time is 120h to obtain a first aging product, adding deionized water into the first aging product for pulping to obtain slurry, wherein the concentration of the slurry is 100g/L in terms of aluminum oxide, and then carrying out second aging, wherein the temperature of the second aging is 90 ℃ and the time is 2h to obtain an aging mixture;
(3) filtering and washing the aged mixture in sequence (the amount of washing water (deionized water) is 100 times of the mass of a product obtained by filtering), and drying at 120 ℃ for 8 hours;
obtaining pseudo-boehmite N4(ii) a Calcining the obtained pseudoboehmite at 550 ℃ for 5h to obtain alumina A4Specific physicochemical properties are shown in Table 1.
Preparation of comparative example 2
The preparation of pseudoboehmite and alumina was carried out in accordance with the method of preparation example 4 except that, in the step (2), the filter cake was directly mixed with deionized water without first aging and slurried to obtain a slurry having a concentration of 100g/L in terms of alumina, and then aged at 90 ℃ for 2 hours to obtain pseudoboehmite DN2(ii) a Roasting the obtained pseudoboehmite at 550 ℃ for 5h to obtain alumina DA2The specific physicochemical properties are shown in Table 1.
Preparation example 5
The preparation of pseudo-boehmite and alumina is carried out according to the method provided by the invention, and the specific steps are as follows:
(1) same as in the step (1) of preparation example 4;
(2) carrying out first aging on the filter cake, wherein the temperature of the first aging is 30 ℃ and the time is 48h to obtain a first aging product, adding deionized water into the first aging product for pulping to obtain slurry, the concentration of the slurry is 100g/L calculated by alumina, and then carrying out second aging, wherein the temperature of the second aging is 90 ℃ and the time is 2h to obtain an aging mixture;
(3) same as in preparation example 4, step (3);
obtaining pseudo-boehmite N5(ii) a Calcining the obtained pseudoboehmite at 550 ℃ for 5h to obtain alumina A5The specific physicochemical properties are shown in Table 1.
Preparation example 6
The preparation of pseudo-boehmite and alumina is carried out according to the method provided by the invention, and the specific steps are as follows:
(1) same as in the step (1) of preparation example 4;
(2) adding deionized water into the filter cake, pulping to obtain slurry, wherein the concentration of the slurry is 100g/L in terms of aluminum oxide, and performing first aging at 45 ℃ for 24 hours to obtain a first aged product; secondly, carrying out secondary ageing on the first aged product, wherein the temperature of the secondary ageing is 90 ℃, and the time is 2 hours, so as to obtain an aged mixture;
(3) same as in preparation example 4, step (3);
obtaining pseudo-boehmite N6(ii) a Calcining the obtained pseudoboehmite at 550 ℃ for 5h to obtain alumina A6The specific physicochemical properties are shown in Table 1.
Preparation example 7
The preparation of the pseudo-boehmite and the alumina is carried out according to the method provided by the invention, and the specific steps are as follows:
(1) adding 3L of deionized water into a colloid forming tank in advance, introducing carbon dioxide-containing gas (the mixed gas of carbon dioxide with the content of 99 vol% and air) from the bottom of the colloid forming tank, introducing a sodium metaaluminate solution from the upper part of the colloid forming tank, enabling the sodium metaaluminate solution to be in countercurrent contact with the carbon dioxide-containing gas for carrying out colloid forming reaction, enabling slurry after the colloid forming reaction to flow out of an overflow pipe of the colloid forming tank, keeping the liquid level in the colloid forming tank unchanged, starting slurry collection after the deionized water which is added in advance is replaced by the slurry after the colloid forming reaction, and then filtering to obtain a filter cake (solid colloid forming product);
wherein the concentration (calculated by alumina) of the sodium metaaluminate solution is 15g/L, the flow rate is 200mL/min, and the retention time is 15 minutes; adjusting the gas dosage to make the pH value of the gelling reaction process about 8.3; the temperature of the gelling reaction is 72 ℃;
(2) carrying out first aging on the filter cake, wherein the temperature of the first aging is 40 ℃ and the time is 24 hours, so as to obtain a first aging product, adding deionized water into the first aging product, pulping to obtain slurry, wherein the concentration of the slurry is 100g/L in terms of aluminum oxide, and then carrying out second aging, wherein the temperature of the second aging is 90 ℃ and the time is 2 hours, so as to obtain an aging mixture;
(3) filtering and washing the aged mixture in sequence (the amount of washing water (deionized water) is 100 times of the mass of a product obtained by filtering), and drying at 120 ℃ for 8 hours;
obtaining pseudo-boehmite N7(ii) a Calcining the obtained pseudoboehmite at 550 ℃ for 5h to obtain alumina A7Specific physicochemical properties are shown in Table 1.
Preparation of comparative example 3
The preparation of the pseudo-boehmite and the alumina is carried out according to the following method, which comprises the following steps:
the preparation of pseudoboehmite and alumina was carried out in accordance with the method of preparation example 7, except that, in the step (2), the filter cake was directly mixed with deionized water without first aging and slurried to obtain a slurry having a concentration of 80g/L in terms of alumina, and then aged at 90 ℃ for 2 hours to obtain pseudoboehmite DN3And alumina DA3The specific physicochemical properties are shown in Table 1.
Preparation of comparative example 4
The preparation of pseudoboehmite and alumina was carried out in accordance with the method of comparative example 3 except that the aging time at 90 ℃ was 26 hours.
Obtaining pseudo-boehmite DN4And alumina DA4The specific physicochemical properties are shown in Table 1.
Preparation example 8
The preparation of pseudo-boehmite and alumina is carried out according to the method provided by the invention, and the specific steps are as follows:
(1) same as in step (1) of preparation example 7;
(2) carrying out first aging on the filter cake, wherein the temperature of the first aging is 25 ℃ and the time is 300h to obtain a first aging product, adding deionized water into the first aging product for pulping to obtain slurry, wherein the concentration of the slurry is 80g/L in terms of aluminum oxide, and then carrying out second aging, wherein the temperature of the second aging is 70 ℃ and the time is 6h to obtain an aging mixture;
(3) same as in preparation example 7, step (3);
obtaining pseudo-boehmite N8(ii) a Calcining the obtained pseudoboehmite at 650 ℃ for 4h to obtain alumina A8Specific physicochemical properties are shown in Table 1.
Preparation example 9
The preparation of pseudo-boehmite and alumina is carried out according to the method provided by the invention, and the specific steps are as follows:
(1) same as in step (1) of preparation example 7;
(2) adding deionized water into the filter cake, pulping to obtain slurry, wherein the concentration of the slurry is 150g/L in terms of aluminum oxide, and performing first aging at 45 ℃ for 48 hours to obtain a first aged product; secondly, carrying out secondary ageing on the first aged product, wherein the temperature of the secondary ageing is 80 ℃, and the time is 4 hours, so as to obtain an aged mixture;
(3) same as in preparation example 7, step (3);
obtaining pseudo-boehmite N9(ii) a Calcining the obtained pseudoboehmite at 550 ℃ for 5h to obtain alumina A9Concrete physicochemical PropertiesAre shown in Table 1.
Preparation example 10
Preparation of pseudoboehmite and alumina was carried out in the same manner as in preparation example 7 except that:
in the step (1), the pH value in the gelling reaction process is about 10.5 by adjusting the gas dosage;
step (2) and step (3) were the same as in preparation example 7;
obtaining pseudo-boehmite N10(ii) a Calcining the obtained pseudoboehmite at 550 ℃ for 5h to obtain alumina A10The specific physicochemical properties are shown in Table 1.
Preparation example 11
Preparation of pseudoboehmite and alumina was carried out in the same manner as in preparation example 7 except that:
in the step (1), the temperature of the gelling reaction is 97 ℃;
step (2) and step (3) were the same as in preparation example 7;
obtaining pseudo-boehmite N11(ii) a Calcining the obtained pseudoboehmite at 550 ℃ for 5h to obtain alumina A11The specific physicochemical properties are shown in Table 1.
Preparation example 12
Preparation of pseudoboehmite and alumina was carried out in the same manner as in preparation example 7 except that:
in the step (2), the temperature of the first aging is 60 ℃;
step (1) and step (3) were the same as in preparation example 7;
obtaining pseudo-boehmite N12(ii) a Calcining the obtained pseudoboehmite at 550 ℃ for 5h to obtain alumina A12Specific physicochemical properties are listed in table 1.
TABLE 1
TABLE 1
Note: "-" indicates no content was detected.
As can be seen from the results in Table 1, the relative crystallinity of the pseudoboehmite prepared by the method of the present invention is greater, up to 90% by weight, than that of comparative examples 1-4 using the conventional aging method; the grain size is larger and reaches 3.9nm at most; the sodium oxide content was lower and dawsonite was not detected; the average pore diameter of the alumina prepared by the pseudo-boehmite is larger and can reach 19.6nm to the maximum; the pore volume is larger and can reach 1.18mL/g at most.
Example 1
300g of pseudo-boehmite N1 and 9 g of sesbania powder are uniformly mixed, the mixture is uniformly mixed with 260 ml of 1% nitric acid aqueous solution at room temperature, after the mixture is continuously kneaded into plastic bodies on a double-screw extruder, butterfly-shaped strips with the diameter of 1.4 mm are extruded, after wet strips are dried for 4 hours at 120 ℃, the wet strips are roasted for 3 hours at 600 ℃, and a carrier Z1 is obtained, wherein the property of the carrier Z1 is shown in Table 2.
200g of vector Z1 were taken and 170 ml of MoO were used3The mixed solution of ammonium molybdate and cobalt nitrate with the content of 208 g/L and the CoO content of 48.7 g/L is soaked for 1 hour, dried for 2 hours at the temperature of 120 ℃ and roasted for 3 hours at the temperature of 420 ℃ to obtain the catalyst C1. The contents of molybdenum oxide and cobalt oxide in the catalyst C1 were determined by X-ray fluorescence method based on the total weight of the catalyst (see petrochemical analysis method RIPP133-90), and the results are shown in table 3.
Example 2
300g of pseudo-boehmite N4 and 9 g of sesbania powder are uniformly mixed, the mixture is uniformly mixed with 270 ml of 1% nitric acid aqueous solution at room temperature, the mixture is extruded into butterfly-shaped strips with the diameter of 1.4 mm after being continuously kneaded into plastic bodies on a double-screw extruder, the wet strips are dried for 4 hours at 120 ℃, and then are roasted for 3 hours at 600 ℃, and a carrier Z2 is obtained, wherein the property of the carrier Z2 is shown in Table 2.
200g of vector Z2 were taken and 170 ml of MoO were used3Soaking the mixed solution of ammonium molybdate and nickel nitrate with the content of 206 g/L and the NiO content of 45 g/L for 1 hour, and drying the mixed solution for 2 hours at the temperature of 120 DEG CThen, the catalyst was calcined at 420 ℃ for 3 hours to obtain catalyst C2. The active metal content results are shown in table 3.
Example 3
300g of pseudo-boehmite N5 and 9 g of sesbania powder are uniformly mixed, the mixture is uniformly mixed with 330 ml of 1% nitric acid aqueous solution at room temperature, the mixture is extruded into butterfly-shaped strips with the diameter of 1.4 mm after being continuously kneaded into plastic bodies on a double-screw extruder, the wet strips are dried for 4 hours at 120 ℃, and then are roasted for 3 hours at 930 ℃, and a carrier Z3 is obtained, wherein the property of the carrier Z3 is shown in Table 2.
200g of vector Z3 were taken and 200ml of MoO were used3The mixed solution of ammonium molybdate and nickel nitrate with the content of 85 g/L and the NiO content of 26 g/L is soaked for 1 hour, dried for 2 hours at the temperature of 120 ℃, and roasted for 3 hours at the temperature of 420 ℃ to obtain the catalyst C3. The active metal content results are shown in table 3.
Example 4
300g of pseudo-boehmite N7 and 9 g of sesbania powder are uniformly mixed, the mixture is uniformly mixed with 280 ml of 1% nitric acid aqueous solution at room temperature, after the mixture is continuously kneaded into plastic bodies on a double-screw extruder, butterfly-shaped strips with the diameter of 1.4 mm are extruded, after wet strips are dried for 4 hours at 120 ℃, the wet strips are roasted for 3 hours at 600 ℃, and a carrier Z4 is obtained, wherein the property of the carrier Z4 is shown in Table 2.
200g of vector Z4 were taken and 170 ml of MoO were used3The mixed solution of ammonium molybdate and cobalt nitrate with the content of 154 g/L and the CoO content of 37 g/L is soaked for 1 hour, dried for 2 hours at the temperature of 120 ℃ and roasted for 3 hours at the temperature of 420 ℃, and the catalyst C4 is obtained. The active metal content results are shown in table 3.
Example 5
A catalyst was prepared according to the procedure of example 4, wherein the pseudoboehmite was N8, the support was designated as Z5, and the catalyst was C5, the results of the active metal content being shown in Table 3.
Comparative example 1
300g of pseudo-boehmite CN2 and 9 g of sesbania powder are uniformly mixed, the mixture is uniformly mixed with 280 ml of 1 percent nitric acid aqueous solution at room temperature, after the mixture is continuously kneaded into plastic bodies on a double-screw extruder, butterfly-shaped strips with the diameter of 1.4 mm are extruded, after wet strips are dried for 4 hours at 120 ℃, the wet strips are roasted for 3 hours at 600 ℃, and a carrier DZ-1 is obtained, wherein the property of the carrier DZ-1 is shown in Table 2.
200g of vector DZ-1 was taken and 170 ml of MoO was used3The mixed solution of ammonium molybdate and cobalt nitrate with the content of 154 g/L and the CoO content of 37 g/L is soaked for 1 hour, dried for 2 hours at the temperature of 120 ℃ and roasted for 3 hours at the temperature of 420 ℃, and the catalyst DC1 is obtained. The active metal content results are shown in table 3.
Comparative example 2
A support and catalyst were prepared according to the method of example 4, except that the pseudoboehmite was DN3, the resulting support was DZ2, and the catalyst was DC 2. The active metal content results are shown in table 3.
Comparative example 3
A support and catalyst were prepared according to the method of example 4, except that the pseudoboehmite was DN4, the resulting support was DZ3, and the catalyst was DC 3. The active metal content results are shown in table 3.
Comparative example 4
300g of pseudo-boehmite P1 and 9 g of sesbania powder are uniformly mixed, the mixture is uniformly mixed with 280 ml of 1% nitric acid aqueous solution at room temperature, after the mixture is continuously kneaded into plastic bodies on a double-screw extruder, butterfly-shaped strips with the diameter of 1.4 mm are extruded, after wet strips are dried for 4 hours at 120 ℃, the wet strips are roasted for 3 hours at 600 ℃, and a carrier DZ4 is obtained, wherein the properties of the carrier DZ4 are shown in Table 2. P1: dry rubber powder (pore volume 0.9 ml/g, specific surface 280 m) from Changling catalyst division2Per gram.
200g of vector DZ4 was taken and 170 ml of MoO was used3And soaking the mixed solution of ammonium molybdate and nickel nitrate with the content of 206 g/L and the NiO content of 45 g/L for 1 hour, drying the mixed solution at the temperature of 120 ℃ for 2 hours, and roasting the mixed solution at the temperature of 420 ℃ for 3 hours to obtain the catalyst DC 4. The active metal content results are shown in table 3.
Comparative example 5
300g of pseudo-boehmite P2 and 9 g of sesbania powder are uniformly mixed, the mixture is uniformly mixed with 270 ml of 1 percent nitric acid aqueous solution at room temperature, the mixture is continuously kneaded into plastic bodies on a double-screw extruder and then extruded into butterfly-shaped strips with the diameter of 1.4 mm, and wet strips are dried at the temperature of 120 DEG CAfter drying for 4 hours, the mixture was calcined at 600 ℃ for 3 hours to obtain a carrier DZ5, and the properties of the carrier DZ5 are shown in Table 2. P2: zibo zimao catalyst limited production dry glue powder (pore volume 0.9 ml/g, specific surface 290 m2Per gram.
200g of vector DZ5 was taken and 200ml of MoO was added3And soaking the mixed solution of ammonium molybdate and nickel nitrate with the content of 85 g/L and the NiO content of 26 g/L for 1 hour, drying the mixed solution at the temperature of 120 ℃ for 2 hours, and roasting the dried mixed solution at the temperature of 420 ℃ for 3 hours to obtain the catalyst DC 5. The active metal content results are shown in table 3.
TABLE 2
TABLE 3
Examples 6 to 10 and comparative examples 6 to 10
The series of examples and comparative examples illustrate the effect of the method provided by the present invention.
The catalyst and the contrast agent were each crushed into particles of 2-3 mm in diameter and charged into the reactor. The reaction conditions are as follows: the reaction temperature is 380 ℃, the hydrogen partial pressure is 14 MPa, and the content of nickel and vanadium in the treated oil is measured by adopting an inductively coupled plasma emission spectrometer (ICP-AES). (the instrument is PE-5300 type plasma light meter of PE company, USA, the concrete method is shown in petrochemical analysis method RIPP124-90)
The sulfur and nitrogen content was measured by an electric method (see petrochemical analysis method RIPP 62-90).
The total removal rate of impurities was calculated according to the following formula:
wherein, the catalysts C1, C4, DC1, DC2 and DC3 are used for evaluating the desulfurization and demetallization performances, and the raw material oil is Kowitt slag with 29.3ppm of nickel content, 83ppm of vanadium content, 4.7% of sulfur content, 0.3% of nitrogen content and 15.1% of carbon residue. C2, C3, DC5 and DC6 catalysts are used for evaluating the carbon residue removal performance, and raw material oil is Maomina sand light VRDS with the nickel content of 15.6ppm, the vanadium content of 38.2ppm, the sulfur content of 3.3%, the nitrogen content of 0.24% and the carbon residue of 10.7%; the activity data for each catalyst are shown in table 4.
TABLE 4
From the results in table 4, it can be seen that the desulfurization activity, demetallization activity, and carbon residue and denitrification activity of the catalyst provided by the present invention in the inferior residual oil hydrotreating process reach the level of the existing catalyst, which indicates that the low-cost pseudoboehmite carrier of the present invention can be used in the residual oil hydrotreating catalyst. In addition, the invention adopts a specific method to prepare the alumina carrier with high pore volume and pore diameter, compared with the prior art, the production cost of the catalyst provided by the invention is greatly reduced.
Claims (11)
1. A heavy oil hydrotreating catalyst, which comprises an alumina carrier and at least one metal component selected from VIII group and at least one metal component selected from VIB group loaded on the carrier, wherein the alumina carrier is prepared from a high-crystallinity and large-grain pseudo-boehmite, the relative crystallinity of the pseudo-boehmite is higher than 65%, the grain size is 2-5nm, and the sodium content of the pseudo-boehmite is not higher than 0.08 wt% based on the dry weight of the pseudo-boehmite and calculated by oxide.
2. The catalyst according to claim 1, wherein the group VIII metal component is cobalt and/or nickel and the group VIB metal component is molybdenum and/or tungsten, the group VIII metal component being present in an amount of 0.5 to 10 wt.%, preferably 1.5 to 5 wt.%, and the group VIB metal component being present in an amount of 5 to 35 wt.%, preferably 6 to 30 wt.%, calculated as oxides and based on the catalyst.
3. The catalyst according to claim 1, wherein the relative crystallinity of the pseudoboehmite is 65-95%, preferably 70-90% by weight, and the crystallite size is 3-4.5nm, preferably 3.3-4nm, and the sodium content in terms of oxide is not higher than 0.06% by weight, preferably 0.01-0.05% by weight, based on the dry weight of the pseudoboehmite.
4. The catalyst according to any one of claims 1 to 3, wherein the preparation method of the pseudoboehmite comprises the steps of:
(1) contacting sodium metaaluminate and/or sodium aluminate solution with gas containing carbon dioxide to carry out gelling reaction to obtain solid gelling product;
(2) sequentially carrying out first aging and second aging on the solid gelling product to obtain an aged mixture; the temperature of the second aging is higher than that of the first aging;
(3) and carrying out solid-liquid separation on the aged mixture to obtain a solid aged product, and drying the solid aged product to obtain the pseudoboehmite.
5. The catalyst according to claim 4, wherein the gel-forming reaction in step (1) is carried out in a continuous or batch manner, preferably in a continuous manner;
preferably, the contacting of step (1) comprises: continuously counter-currently contacting sodium metaaluminate and/or a solution of sodium aluminate with a carbon dioxide-containing gas;
preferably, the conditions of the gelling reaction include: the pH value is 7-10, preferably 7.5-9.5; the retention time is 2-60min, preferably 7-50 min; the temperature is 30-95 deg.C, preferably 35-85 deg.C.
6. The catalyst according to claim 5, wherein the concentration of the sodium metaaluminate and/or sodium aluminate solution is 5-40g/L, preferably 8-35g/L, calculated as alumina;
preferably, the carbon dioxide-containing gas has a volume content of carbon dioxide of more than 20 volume%, preferably more than 30 volume%.
7. The catalyst according to claim 4, wherein the temperature of the second aging is 10-100 ℃, preferably 25-85 ℃, more preferably 45-60 ℃ higher than the temperature of the first aging.
8. The catalyst of claim 4 or 7, wherein the first aging conditions comprise: the temperature is 0-45 ℃, preferably 10-40 ℃; the time is 2 to 240 hours, preferably 4 to 120 hours;
preferably, the conditions of the second aging include: the temperature is 50-100 ℃, preferably 65-95 ℃; the time is 1-24h, preferably 2-12 h.
9. The catalyst of claim 4, wherein step (2) comprises: carrying out first aging on the solid gelling product to obtain a first aged product, adding water into the first aged product, pulping, and carrying out second aging to obtain an aged mixture; or,
the step (2) comprises the following steps: adding water into the solid gelling product, pulping, carrying out first aging to obtain a first aged product, and carrying out second aging on the first aged product to obtain an aged mixture.
10. The catalyst as claimed in claim 1, wherein the alumina pore volume obtained by calcining the pseudo-boehmite is 0.8-1.3mL/g, the average pore diameter is more than 14nm, and the specific surface area is 200-260m2(iv) g; preferably, the alumina pore volume obtained by roasting the pseudo-boehmite is 0.9-1.2mL/g, the average pore diameter is more than 15nm, and the specific surface area is 210-255m2(ii)/g; the roasting conditions comprise: the temperature is 500-1200 ℃, and the time is 2-8 hours; preferably, the conditions of the calcination include: the temperature is 550 ℃ and 850 ℃ and the time is 3-6 hours.
11. A heavy oil hydrotreating method, comprising contacting heavy raw oil with a catalyst under hydrotreating reaction conditions, wherein the catalyst is the catalyst according to any one of claims 1 to 10.
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| CN115301231A (en) * | 2022-08-15 | 2022-11-08 | 中国科学院生态环境研究中心 | Noble metal catalyst for catalytic oxidation of formaldehyde and preparation method thereof |
| WO2023232021A1 (en) * | 2022-05-30 | 2023-12-07 | 中国石油化工股份有限公司 | Pseudo-boehmite and preparation method therefor, and catalytic cracking catalyst comprising pseudo-boehmite and preparation and use thereof |
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