CN116273015A - Petroleum resin hydrogenation catalyst and its preparation method and application - Google Patents
Petroleum resin hydrogenation catalyst and its preparation method and application Download PDFInfo
- Publication number
- CN116273015A CN116273015A CN202310205104.5A CN202310205104A CN116273015A CN 116273015 A CN116273015 A CN 116273015A CN 202310205104 A CN202310205104 A CN 202310205104A CN 116273015 A CN116273015 A CN 116273015A
- Authority
- CN
- China
- Prior art keywords
- petroleum resin
- slurry
- hydrogenation catalyst
- mixed
- treatment
- 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
Links
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 141
- 229920005989 resin Polymers 0.000 title claims abstract description 136
- 239000011347 resin Substances 0.000 title claims abstract description 136
- 239000003054 catalyst Substances 0.000 title claims abstract description 134
- 239000003208 petroleum Substances 0.000 title claims abstract description 132
- 238000002360 preparation method Methods 0.000 title abstract description 21
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical group [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims abstract description 75
- 229910052759 nickel Inorganic materials 0.000 claims abstract description 37
- HECLRDQVFMWTQS-RGOKHQFPSA-N 1755-01-7 Chemical compound C1[C@H]2[C@@H]3CC=C[C@@H]3[C@@H]1C=C2 HECLRDQVFMWTQS-RGOKHQFPSA-N 0.000 claims abstract description 34
- 239000011148 porous material Substances 0.000 claims abstract description 32
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims abstract description 30
- 239000011777 magnesium Substances 0.000 claims abstract description 30
- 229910052749 magnesium Inorganic materials 0.000 claims abstract description 30
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 claims abstract description 28
- 229910052725 zinc Inorganic materials 0.000 claims abstract description 28
- 239000011701 zinc Substances 0.000 claims abstract description 28
- 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 20
- 238000004042 decolorization Methods 0.000 claims abstract description 6
- 239000002002 slurry Substances 0.000 claims description 142
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 78
- 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 description 41
- 239000011734 sodium Substances 0.000 claims description 41
- 229910052708 sodium Inorganic materials 0.000 claims description 41
- 239000001569 carbon dioxide Substances 0.000 claims description 39
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 39
- 238000006243 chemical reaction Methods 0.000 claims description 38
- 239000011259 mixed solution Substances 0.000 claims description 38
- 229910052782 aluminium Inorganic materials 0.000 claims description 36
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 36
- 230000032683 aging Effects 0.000 claims description 34
- 239000007864 aqueous solution Substances 0.000 claims description 33
- 239000007789 gas Substances 0.000 claims description 33
- 238000002156 mixing Methods 0.000 claims description 29
- 239000000843 powder Substances 0.000 claims description 27
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 25
- 239000011268 mixed slurry Substances 0.000 claims description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 22
- 238000000034 method Methods 0.000 claims description 21
- 238000002161 passivation Methods 0.000 claims description 21
- 239000000243 solution Substances 0.000 claims description 18
- 229910052757 nitrogen Inorganic materials 0.000 claims description 14
- 239000003570 air Substances 0.000 claims description 13
- 238000001035 drying Methods 0.000 claims description 12
- 239000003960 organic solvent Substances 0.000 claims description 12
- 239000003795 chemical substances by application Substances 0.000 claims description 11
- 238000001914 filtration Methods 0.000 claims description 11
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 10
- 239000001257 hydrogen Substances 0.000 claims description 7
- 229910052739 hydrogen Inorganic materials 0.000 claims description 7
- 125000004435 hydrogen atom Chemical group [H]* 0.000 claims description 7
- 150000001924 cycloalkanes Chemical class 0.000 claims description 6
- 239000002904 solvent Substances 0.000 claims description 5
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 4
- 238000009835 boiling Methods 0.000 claims description 4
- 150000002681 magnesium compounds Chemical class 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 150000002816 nickel compounds Chemical class 0.000 claims description 4
- 150000003752 zinc compounds Chemical class 0.000 claims description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 3
- 238000000975 co-precipitation Methods 0.000 claims description 3
- 239000001301 oxygen Substances 0.000 claims description 3
- 229910052760 oxygen Inorganic materials 0.000 claims description 3
- 239000012716 precipitator Substances 0.000 claims description 3
- 238000005406 washing Methods 0.000 claims description 3
- 238000011068 loading method Methods 0.000 abstract description 6
- MFUVDXOKPBAHMC-UHFFFAOYSA-N magnesium;dinitrate;hexahydrate Chemical compound O.O.O.O.O.O.[Mg+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O MFUVDXOKPBAHMC-UHFFFAOYSA-N 0.000 description 26
- 238000006386 neutralization reaction Methods 0.000 description 23
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 18
- 239000000047 product Substances 0.000 description 17
- AOPCKOPZYFFEDA-UHFFFAOYSA-N nickel(2+);dinitrate;hexahydrate Chemical compound O.O.O.O.O.O.[Ni+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O AOPCKOPZYFFEDA-UHFFFAOYSA-N 0.000 description 15
- XIOUDVJTOYVRTB-UHFFFAOYSA-N 1-(1-adamantyl)-3-aminothiourea Chemical compound C1C(C2)CC3CC2CC1(NC(=S)NN)C3 XIOUDVJTOYVRTB-UHFFFAOYSA-N 0.000 description 13
- 230000000052 comparative effect Effects 0.000 description 13
- 230000001105 regulatory effect Effects 0.000 description 10
- 239000008367 deionised water Substances 0.000 description 9
- 229910021641 deionized water Inorganic materials 0.000 description 9
- 230000000694 effects Effects 0.000 description 9
- 229910000029 sodium carbonate Inorganic materials 0.000 description 9
- 238000003756 stirring Methods 0.000 description 9
- ATRRKUHOCOJYRX-UHFFFAOYSA-N Ammonium bicarbonate Chemical group [NH4+].OC([O-])=O ATRRKUHOCOJYRX-UHFFFAOYSA-N 0.000 description 8
- 229910000013 Ammonium bicarbonate Inorganic materials 0.000 description 8
- 235000012538 ammonium bicarbonate Nutrition 0.000 description 8
- 239000001099 ammonium carbonate Substances 0.000 description 8
- 239000000706 filtrate Substances 0.000 description 8
- 229910001415 sodium ion Inorganic materials 0.000 description 8
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 description 7
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 description 7
- 229910052794 bromium Inorganic materials 0.000 description 7
- 230000003472 neutralizing effect Effects 0.000 description 7
- 230000009286 beneficial effect Effects 0.000 description 5
- 238000007086 side reaction Methods 0.000 description 5
- HECLRDQVFMWTQS-UHFFFAOYSA-N Dicyclopentadiene Chemical compound C1C2C3CC=CC3C1C=C2 HECLRDQVFMWTQS-UHFFFAOYSA-N 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 229910000510 noble metal Inorganic materials 0.000 description 4
- 239000012267 brine Substances 0.000 description 3
- 230000015556 catabolic process Effects 0.000 description 3
- 238000006731 degradation reaction Methods 0.000 description 3
- DMEGYFMYUHOHGS-UHFFFAOYSA-N heptamethylene Natural products C1CCCCCC1 DMEGYFMYUHOHGS-UHFFFAOYSA-N 0.000 description 3
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 3
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 3
- 238000005303 weighing Methods 0.000 description 3
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 2
- RGSFGYAAUTVSQA-UHFFFAOYSA-N Cyclopentane Chemical compound C1CCCC1 RGSFGYAAUTVSQA-UHFFFAOYSA-N 0.000 description 2
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 description 2
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 2
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000004364 calculation method Methods 0.000 description 2
- SNRUBQQJIBEYMU-UHFFFAOYSA-N dodecane Chemical compound CCCCCCCCCCCC SNRUBQQJIBEYMU-UHFFFAOYSA-N 0.000 description 2
- 238000010304 firing Methods 0.000 description 2
- YIXJRHPUWRPCBB-UHFFFAOYSA-N magnesium nitrate Chemical compound [Mg+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O YIXJRHPUWRPCBB-UHFFFAOYSA-N 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- BKIMMITUMNQMOS-UHFFFAOYSA-N nonane Chemical compound CCCCCCCCC BKIMMITUMNQMOS-UHFFFAOYSA-N 0.000 description 2
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 2
- IIYFAKIEWZDVMP-UHFFFAOYSA-N tridecane Chemical compound CCCCCCCCCCCCC IIYFAKIEWZDVMP-UHFFFAOYSA-N 0.000 description 2
- RSJKGSCJYJTIGS-UHFFFAOYSA-N undecane Chemical compound CCCCCCCCCCC RSJKGSCJYJTIGS-UHFFFAOYSA-N 0.000 description 2
- 229930195735 unsaturated hydrocarbon Natural products 0.000 description 2
- ONDPHDOFVYQSGI-UHFFFAOYSA-N zinc nitrate Chemical compound [Zn+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O ONDPHDOFVYQSGI-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- 239000004831 Hot glue Substances 0.000 description 1
- 239000013032 Hydrocarbon resin Substances 0.000 description 1
- 239000004820 Pressure-sensitive adhesive Substances 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- VXAUWWUXCIMFIM-UHFFFAOYSA-M aluminum;oxygen(2-);hydroxide Chemical compound [OH-].[O-2].[Al+3] VXAUWWUXCIMFIM-UHFFFAOYSA-M 0.000 description 1
- 239000012752 auxiliary agent Substances 0.000 description 1
- 230000002902 bimodal effect Effects 0.000 description 1
- 239000011230 binding agent Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 1
- 238000012993 chemical processing Methods 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- LMGZGXSXHCMSAA-UHFFFAOYSA-N cyclodecane Chemical compound C1CCCCCCCCC1 LMGZGXSXHCMSAA-UHFFFAOYSA-N 0.000 description 1
- GPTJTTCOVDDHER-UHFFFAOYSA-N cyclononane Chemical compound C1CCCCCCCC1 GPTJTTCOVDDHER-UHFFFAOYSA-N 0.000 description 1
- WJTCGQSWYFHTAC-UHFFFAOYSA-N cyclooctane Chemical compound C1CCCCCCC1 WJTCGQSWYFHTAC-UHFFFAOYSA-N 0.000 description 1
- 239000004914 cyclooctane Substances 0.000 description 1
- KYTNZWVKKKJXFS-UHFFFAOYSA-N cycloundecane Chemical compound C1CCCCCCCCCC1 KYTNZWVKKKJXFS-UHFFFAOYSA-N 0.000 description 1
- DIOQZVSQGTUSAI-NJFSPNSNSA-N decane Chemical compound CCCCCCCCC[14CH3] DIOQZVSQGTUSAI-NJFSPNSNSA-N 0.000 description 1
- 238000007598 dipping method Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 159000000011 group IA salts Chemical class 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 229920006270 hydrocarbon resin Polymers 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- 239000000395 magnesium oxide Substances 0.000 description 1
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 1
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 1
- 229910052748 manganese Inorganic materials 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- DIOQZVSQGTUSAI-UHFFFAOYSA-N n-butylhexane Natural products CCCCCCCCCC DIOQZVSQGTUSAI-UHFFFAOYSA-N 0.000 description 1
- 229910000480 nickel oxide Inorganic materials 0.000 description 1
- KBJMLQFLOWQJNF-UHFFFAOYSA-N nickel(ii) nitrate Chemical compound [Ni+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O KBJMLQFLOWQJNF-UHFFFAOYSA-N 0.000 description 1
- 238000000643 oven drying Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- GNRSAWUEBMWBQH-UHFFFAOYSA-N oxonickel Chemical compound [Ni]=O GNRSAWUEBMWBQH-UHFFFAOYSA-N 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 238000002791 soaking Methods 0.000 description 1
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 1
- 235000017557 sodium bicarbonate Nutrition 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 238000012719 thermal polymerization Methods 0.000 description 1
- 229920001169 thermoplastic Polymers 0.000 description 1
- 239000004416 thermosoftening plastic Substances 0.000 description 1
- 239000011787 zinc oxide Substances 0.000 description 1
Classifications
-
- 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
- B01J23/80—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 zinc, cadmium or mercury
-
- 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
- B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
- B01J35/61—Surface area
- B01J35/615—100-500 m2/g
-
- 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
- B01J35/60—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
-
- 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
- B01J35/60—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
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F8/00—Chemical modification by after-treatment
- C08F8/04—Reduction, e.g. hydrogenation
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- General Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Catalysts (AREA)
Abstract
The invention provides a petroleum resin hydrogenation catalyst which is applied to hydrogenation decolorization of dicyclopentadiene petroleum resin, wherein the petroleum resin hydrogenation catalyst comprises an active component and a carrier, the active component is nickel, zinc and magnesium, and the carrier is an alumina carrier; the catalyst comprises, by mass, 40-80% of nickel, 1-10% of zinc, 1-7% of magnesium and 10-58% of alumina carrier; the specific surface area of the petroleum resin hydrogenation catalyst is 200-400 square meters per gram, the pore volume is 0.5-1.0 cubic centimeter per gram, and the pore diameter is 10-100nm. The invention solves the problems of high price, low active component loading and non-uniformity of the existing petroleum resin hydrogenation catalyst. The invention also provides a preparation method and application of the petroleum resin hydrogenation catalyst.
Description
Technical Field
The invention relates to the technical field of petrochemical catalysts, in particular to a petroleum resin hydrogenation catalyst and a preparation method and application thereof.
Background
Petrochemical catalysts are an important product in the catalyst industry and are used in chemical processing in petrochemical product production. Petrochemical catalysts include hydrogenation catalysts, which are widely used in refining processes of raw materials and products, in addition to product production processes.
Dicyclopentadiene petroleum resins are typically produced from dicyclopentadiene by thermal polymerization, a thermoplastic hydrocarbon resin having a relatively low number average molecular weight. Dicyclopentadiene petroleum resin has good compatibility with other resins, is often used as a tackifier and a binder, and has been widely used in hot melt adhesives, pressure-sensitive adhesive tapes, ink printing and rubber. At present, a great part of dicyclopentadiene is derived from a carbon five fraction separation product of an ethylene byproduct produced by petroleum pyrolysis, and petroleum resin produced by dicyclopentadiene generally has the problems of deep hue, odor, high unsaturated hydrocarbon bond content, low thermal stability and oxidation stability and poor adhesive force, and is not well compatible with a plurality of resin matrixes, so that the use effect of the dicyclopentadiene as a tackifier is poor. Generally, hydrogenation is adopted to improve the performance of dicyclopentadiene petroleum resin, and the content of unsaturated hydrocarbon bonds can be effectively reduced through hydrogenation, so that the thermal stability and compatibility of the dicyclopentadiene petroleum resin are improved.
Chinese patent publication No. CN1189493a discloses a hydrogenation catalyst for preparing dicyclopentadiene hydrogenated petroleum resin, which has noble metal Pt, is expensive, and the softening point of the obtained petroleum resin is severely reduced; the Chinese patent with publication number of CN101157029A discloses a catalyst special for dicyclopentadiene hydrogenation and a preparation method thereof, which has noble metal Pt and is high in price and not suitable for large-scale production.
Chinese patent publication No. CN107252688A discloses a DCPD petroleum resin hydrogenation catalyst, its preparation method and application, and gamma-Al is added 2 O 3 Soaking the carrier in Ni-containing solution, and oven drying and roasting to disperse the active components unevenly on the carrier, or even to agglomerate and further to shadowResponding to the activity of the catalyst; chinese patent publication No. CN106268725A discloses hydrogenation catalyst of DCPD resin, preparation method and application, gamma-Al 2 O 3 Is a carrier, active components Pd, mo and Mn are carried on the carrier after molding step by step in a dipping mode, and the catalyst is prepared by drying and roasting, and adopts gamma-Al 2 O 3 As a carrier, the loading amount of the active metal is low, when the carrier is used for the hydrogenation reaction of DCPD petroleum resin, the hydrogenation rate is low, and the active metal is easy to run off.
Therefore, there is a need to develop a novel petroleum resin hydrogenation catalyst, and a preparation method and application thereof, so as to avoid the above-mentioned problems in the prior art.
Disclosure of Invention
The invention aims to provide a novel petroleum resin hydrogenation catalyst, a preparation method and application thereof, and solves the problems of high price, low active component loading and non-uniformity of the existing petroleum resin hydrogenation catalyst.
In order to achieve the above purpose, the invention provides a petroleum resin hydrogenation catalyst, which is applied to the hydrogenation and decoloration of dicyclopentadiene petroleum resin, wherein the petroleum resin hydrogenation catalyst comprises an active component and a carrier, the active component is nickel, zinc and magnesium, and the carrier is an alumina carrier;
the catalyst comprises, by mass, 40-80% of nickel, 1-10% of zinc, 1-7% of magnesium and 10-58% of alumina carrier;
the specific surface area of the petroleum resin hydrogenation catalyst is 200-400 square meters per gram, the pore volume is 0.5-1.0 cubic centimeter per gram, and the pore diameter is 10-100 nanometers.
The petroleum resin hydrogenation catalyst has the beneficial effects that: the petroleum resin hydrogenation catalyst comprises an active component and a carrier, wherein the active component is nickel, zinc and magnesium, the carrier is an alumina carrier, the content of zinc is 1-10% based on the mass percent of the petroleum resin hydrogenation catalyst, and the addition of the zinc and the content thereof ensure that the nickel and the magnesium are uniformly distributed on the surface of the alumina carrier, and the stability of the microcosmic appearance of the active site of the nickel on the alumina carrier can be maintained; the content of magnesium is 1-7% by mass of the petroleum resin hydrogenation catalyst, and the addition and content of magnesium improve the pH value of the surface of the petroleum resin hydrogenation catalyst, so that the hydrogenation activity and selectivity of the petroleum resin hydrogenation catalyst are improved, the occurrence of hydrogenation degradation side reaction is reduced, the petroleum resin hydrogenation catalyst does not contain noble metal, and the petroleum resin hydrogenation catalyst is low in cost and suitable for large-scale use. Therefore, the invention solves the problems of high price, low active component loading and non-uniformity of the existing petroleum resin hydrogenation catalyst.
Another object of the present invention is to provide a method for preparing a petroleum resin hydrogenation catalyst, comprising the steps of:
s0: providing a mixed source slurry and an aluminum source slurry, wherein the mixed source slurry comprises nickel, zinc and magnesium, and the volume ratio of the mixed source slurry to the aluminum source slurry is (2-4): 1;
s1: mixing the mixed source slurry and the aluminum source slurry to obtain mixed slurry, and sequentially performing first aging treatment, filtering washing treatment and drying treatment on the mixed slurry to obtain catalyst powder;
s2: and (3) roasting, reducing and passivating the catalyst powder in sequence to obtain the petroleum resin hydrogenation catalyst.
The preparation method of the petroleum resin hydrogenation catalyst has the beneficial effects that: the mixed source slurry comprises nickel, zinc and magnesium, and the volume ratio of the mixed source slurry to the aluminum source slurry is (2-4) 1, so that the nickel, zinc and magnesium in the mixed source slurry are more uniformly mixed with the aluminum source slurry, active components of nickel, zinc and magnesium are more uniformly distributed on an alumina carrier, meanwhile, the addition of zinc and the content thereof ensure that the nickel and magnesium are uniformly distributed on the surface of the alumina carrier, and the stability of the microcosmic appearance of the active sites of nickel on the alumina carrier can be maintained; the petroleum resin hydrogenation catalyst is obtained after the catalyst powder is subjected to roasting treatment, reduction treatment and passivation treatment in sequence, and the selectivity of the petroleum resin hydrogenation catalyst is improved through the reduction treatment and the passivation treatment.
Optionally, the preparation method of the aluminum source slurry comprises the following steps: introducing a mixed gas containing carbon dioxide into a sodium metaaluminate aqueous solution in a flowing state to carry out a gelling reaction until a gelling slurry with the pH value of 9.0-10.5 is obtained, carrying out second aging treatment on the gelling slurry to obtain an aged gelling slurry, and adding a pore-expanding agent into the aged gelling slurry to carry out pore-expanding treatment to obtain the aluminum source slurry.
Optionally, the molar ratio of the pore expanding agent to sodium metaaluminate in the sodium metaaluminate aqueous solution is (1-2): 1.
Optionally, the temperature of the reaming treatment is 70-150 ℃, the time of the reaming treatment is 12-24 hours, the temperature of the roasting treatment is 180-700 ℃, and the time of the roasting treatment is 2-8 hours.
Optionally, the temperature of the reduction treatment is 200-700 ℃, the time of the reduction treatment is 2-12 hours, and the air source of the reduction treatment is hydrogen or hydrogen-nitrogen mixed gas.
Optionally, the passivation treatment is performed at a temperature of 20-200 ℃, the passivation treatment time is 2-24 hours, the passivation treatment step is to treat the reduced catalyst powder by using a mixed gas containing nitrogen, and the mixed gas further comprises any one of air, oxygen or carbon dioxide.
Optionally, the volume flow rate of the mixed gas containing carbon dioxide is 1-4 standard meters per hour, the carbon dioxide accounts for 40-90% of the volume of the mixed gas containing carbon dioxide, and each liter of the aqueous solution of sodium metaaluminate contains 50-150 g of sodium metaaluminate.
Optionally, the preparation method of the mixed source slurry comprises the following steps: and performing coprecipitation treatment on the mixed solution by using an alkaline saline solution as a precipitator to obtain mixed source slurry, wherein the mixed solution is prepared by dissolving a nickel compound, a zinc compound and a magnesium compound in water.
It is still another object of the present invention to provide an application of the petroleum resin hydrogenation catalyst, the petroleum resin hydrogenation catalyst is placed in a high-pressure reaction kettle, dicyclopentadiene petroleum resin solution is added into the high-pressure reaction kettle to perform a hydrogenation and decoloration reaction with hydrogen, the temperature of the hydrogenation and decoloration reaction is 180-280 ℃, the pressure of the hydrogenation and decoloration reaction is 5-10 mpa, the dicyclopentadiene petroleum resin solution is obtained by dissolving dicyclopentadiene petroleum resin in an organic solvent, the mass ratio of the organic solvent to dicyclopentadiene is (0.001-0.2): 1, the organic solvent comprises at least one of alkane, cycloalkane and solvent oil, and the boiling point of the alkane is less than 250 ℃.
The petroleum resin hydrogenation catalyst has the beneficial effects that: the petroleum resin hydrogenation catalyst reduces side reactions in the hydrogenation and decoloration reaction of dicyclopentadiene petroleum resin, improves the selectivity of the hydrogenation and decoloration reaction, and improves the yield of dicyclopentadiene petroleum resin.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the embodiments of the present invention more apparent, the technical solutions in the embodiments of the present invention will be clearly and completely described below, and it is apparent that the described embodiments are some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention. Unless otherwise defined, technical or scientific terms used herein should be given the ordinary meaning as understood by one of ordinary skill in the art to which this invention belongs. As used herein, the word "comprising" and the like means that elements or items preceding the word are included in the element or item listed after the word and equivalents thereof without precluding other elements or items.
After the petroleum resin is hydrogenated, the petroleum resin can become water white or transparent, and the stability is enhanced. In addition, hydrogenation may also improve adhesion, weatherability, and compatibility with EVA. The western famous company adopts a catalytic hydrogenation process to saturate unsaturated bonds in petroleum resin, and the hydrogenated petroleum resin with white or nearly colorless water is prepared. Hydrogenated petroleum resins are rapidly developing in developed countries such as the united states, and have been formed on a comparable production scale, resulting in good economic benefits.
The petroleum resin hydrogenation catalyst has almost no hydrogenation activity when the pore diameter of the carrier is too small, and the carrier has bimodal or multimodal pores with small pores of 10-30nm and large pores of about 100nm because the petroleum resin has certain molecular weight distribution. The selective auxiliary agent is used for regulating the pH value of the surface of the catalyst and is compounded with active components, so that the hydrogenation activity and selectivity of the catalyst are improved, the side reaction of hydrogenation degradation is reduced, and the yield of petroleum resin is improved.
The petroleum resin hydrogenation catalyst improves the sulfur poisoning resistance of the petroleum resin catalyst by adjusting the ratio of reduced nickel to total nickel on the petroleum resin catalyst, a loading method and adding IIB and IIA elements, inhibits the sintering of nickel metal and prolongs the service life of the petroleum resin hydrogenation catalyst.
The embodiment of the invention provides a petroleum resin hydrogenation catalyst, which is applied to hydrogenation decolorization of dicyclopentadiene petroleum resin, wherein the petroleum resin hydrogenation catalyst comprises an active component and a carrier, the active component is nickel, zinc and magnesium, and the carrier is an alumina carrier;
the catalyst comprises, by mass, 40-80% of nickel, 1-10% of zinc, 1-7% of magnesium and 10-58% of alumina carrier;
the specific surface area of the petroleum resin hydrogenation catalyst is 200-400 square meters per gram, the pore volume is 0.5-1.0 cubic centimeter per gram, and the pore diameter is 10-100 nanometers.
Specifically, the petroleum resin hydrogenation catalyst comprises an active component and a carrier, wherein the active component is nickel, zinc and magnesium, the carrier is an alumina carrier, the content of zinc is 1-10% based on the mass percent of the petroleum resin hydrogenation catalyst, and the addition of the zinc and the content thereof ensure that the nickel and the magnesium are uniformly distributed on the surface of the alumina carrier, and the stability of the microcosmic appearance of the active site of the nickel on the alumina carrier can be maintained; the content of magnesium is 1-7% by mass of the petroleum resin hydrogenation catalyst, and the addition and content of magnesium improve the pH value of the surface of the petroleum resin hydrogenation catalyst, so that the hydrogenation activity and selectivity of the petroleum resin hydrogenation catalyst are improved, the occurrence of hydrogenation degradation side reaction is reduced, the petroleum resin hydrogenation catalyst does not contain noble metal, and the petroleum resin hydrogenation catalyst is low in cost and suitable for large-scale use. Therefore, the invention solves the problems of high price, low active component loading and non-uniformity of the existing petroleum resin hydrogenation catalyst.
The embodiment of the invention provides a preparation method of a petroleum resin hydrogenation catalyst, which comprises the following steps:
s0: providing a mixed source slurry and an aluminum source slurry, wherein the mixed source slurry comprises nickel, zinc and magnesium, and the volume ratio of the mixed source slurry to the aluminum source slurry is (2-4): 1;
s1: mixing the mixed source slurry and the aluminum source slurry to obtain mixed slurry, and sequentially performing first aging treatment, filtering washing treatment and drying treatment on the mixed slurry to obtain catalyst powder;
s2: and (3) roasting, reducing and passivating the catalyst powder in sequence to obtain the petroleum resin hydrogenation catalyst.
Specifically, the mixed source slurry comprises nickel, zinc and magnesium, and the volume ratio of the mixed source slurry to the aluminum source slurry is controlled to be (2-4): 1, so that the nickel, zinc and magnesium in the mixed source slurry are more uniformly mixed with the aluminum source slurry, active components of nickel, zinc and magnesium are more uniformly distributed on an alumina carrier, meanwhile, the addition of zinc and the content thereof ensure that the nickel and magnesium are uniformly distributed on the surface of the alumina carrier, and the stability of the microcosmic appearance of the active site of nickel on the alumina carrier can be maintained; the petroleum resin hydrogenation catalyst is obtained after the catalyst powder is subjected to roasting treatment, reduction treatment and passivation treatment in sequence, and the selectivity of the petroleum resin hydrogenation catalyst is improved through the reduction treatment and the passivation treatment.
In some embodiments of the invention, the volume ratio of the mixed source slurry to the aluminum source slurry is any one of 2.5:1, 3:1, and 3.5:1.
In some embodiments of the invention, the nickel compound is nickel nitrate, the zinc compound is zinc nitrate, the magnesium compound is magnesium nitrate, and the alkaline brine solution is any one of sodium carbonate aqueous solution and sodium bicarbonate aqueous solution.
In some embodiments of the invention, the step of co-precipitating the mixed solution using the alkaline brine solution as a precipitant to obtain a mixed source slurry comprises: and (3) carrying out parallel flow mixing on the mixed solution and the alkaline saline solution at a flow rate of 10-40 ml/min respectively, wherein in the process of carrying out parallel flow mixing, the mixed solution obtained by parallel flow mixing is subjected to neutralization treatment with a neutralization temperature of 30-80 ℃ and a neutralization time of 20-100 min at a stirring rate of not lower than 300rpm, deionized water is used for regulating the pH value in the neutralization treatment to obtain a neutralization slurry with the pH value of 7.5-9.5, and then the neutralization slurry is subjected to third aging treatment to obtain the mixed source slurry.
In some embodiments of the present invention, the mixed solution contains 25-100 g of nickel oxide per liter of the mixed solution, 2-20 g of zinc oxide per liter of the mixed solution, and 2-20 g of magnesium oxide per liter of the mixed solution, wherein the volume ratio of the mixed solution to the aqueous solution of the alkaline salt is (1-5): 1.
In some embodiments of the invention, the alkaline brine solution has a pH of 10-14.
In some embodiments of the invention, the method of preparing an aluminum source slurry comprises: introducing a mixed gas containing carbon dioxide into a sodium metaaluminate aqueous solution in a flowing state to carry out a gelling reaction until a gelling slurry with the pH value of 9.0-10.5 is obtained, carrying out second aging treatment on the gelling slurry to obtain an aged gelling slurry, and adding a pore-expanding agent into the aged gelling slurry to carry out pore-expanding treatment to obtain the aluminum source slurry.
In some embodiments of the invention, the pore-expanding agent is ammonium bicarbonate.
In some embodiments of the invention, the aluminum source slurry may be selected from pseudo-boehmite slurries.
In some embodiments of the invention, the molar ratio of the pore-expanding agent to sodium metaaluminate in the aqueous sodium metaaluminate solution is (1-2): 1. In some embodiments, the molar ratio of the pore-expanding agent to sodium metaaluminate in the aqueous sodium metaaluminate solution is any one of 1.1:1, 1.2:1, 1.3:1, 1.4:1, 1.5:1, 1.6:1, 1.7:1, 1.8:1, 1.9:1.
In some embodiments of the invention, the temperature of the reaming process is 70-150 degrees celsius, the time of the reaming process is 12-24 hours, the temperature of the firing process is 180-700 degrees celsius, the time of the firing process is 2-8 hours,
in some embodiments of the invention, the temperature of the reduction treatment is 200-700 ℃, the time of the reduction treatment is 2-12 hours, and the air source of the reduction treatment is hydrogen or hydrogen-nitrogen mixture.
According to some embodiments of the invention, the passivation treatment temperature is 20-200 ℃, the passivation treatment time is 2-24 hours, and the passivation treatment step is to treat the reduced catalyst powder by using a mixed gas containing nitrogen, wherein the mixed gas also comprises any one of air, oxygen or carbon dioxide.
In some embodiments of the present invention, the volume flow rate of the mixed gas containing carbon dioxide is 1-4 standard meters per hour, the carbon dioxide accounts for 40-90% of the volume of the mixed gas containing carbon dioxide, and each liter of the aqueous solution of sodium metaaluminate contains 50-150 grams of sodium metaaluminate.
In some embodiments of the present invention, the temperature of the gelling reaction and the first aging process is between 30 and 65 degrees celsius, the sum of the time of the gelling reaction and the time of the first aging process is less than 90 minutes, and the time of the first aging process is between 20 and 40 minutes.
In some embodiments of the invention, the method of preparing a mixed source slurry comprises: and performing coprecipitation treatment on the mixed solution by using an alkaline saline solution as a precipitator to obtain mixed source slurry, wherein the mixed solution is prepared by dissolving a nickel compound, a zinc compound and a magnesium compound in water.
The embodiment of the invention provides an application of a petroleum resin hydrogenation catalyst, which is characterized in that the petroleum resin hydrogenation catalyst is placed in a high-pressure reaction kettle, dicyclopentadiene petroleum resin solution is added into the high-pressure reaction kettle to carry out hydrogenation and decoloration reaction with hydrogen, the temperature of the hydrogenation and decoloration reaction is 180-280 ℃, the pressure of the hydrogenation and decoloration reaction is 5-10 megapascals, the dicyclopentadiene petroleum resin solution is obtained by dissolving dicyclopentadiene petroleum resin in an organic solvent, the mass ratio of the organic solvent to dicyclopentadiene is (0.001-0.2): 1, the organic solvent comprises at least one of alkane, cycloalkane and solvent oil, and the boiling point of alkane is less than 250 ℃.
Specifically, the petroleum resin hydrogenation catalyst reduces side reactions in the hydrogenation and decoloration reaction of dicyclopentadiene petroleum resin, improves the selectivity of the hydrogenation and decoloration reaction, and improves the yield of dicyclopentadiene petroleum resin.
Some embodiments of the invention, the alkane comprises at least one of methane, ethane, propane, n-butane, n-pentane, hexane, heptane, n-octane, nonane, decane, undecane, dodecane, and tridecane; the cycloalkane includes at least one of cyclopentane, cyclohexane, cycloheptane, cyclooctane, cyclononane, cyclodecane, and cycloundecane.
In some embodiments of the present invention, the solvent oil refers to a light oil that dissolves, dilutes, washes and extracts certain substances in chemical production, and generally refers to a light petroleum fraction, so long as it is composed of alkanes, cycloalkanes, and small amounts of aromatics.
Example 1
Preparation of sample 1
Weighing 467 g of nickel nitrate hexahydrate, 14.6 g of zinc nitrate hexahydrate and 24.5 g of magnesium nitrate hexahydrate, dissolving the nickel nitrate hexahydrate, 14.6 g of zinc nitrate hexahydrate and 24.5 g of magnesium nitrate hexahydrate in water to prepare 2L of mixed solution, mixing 2L of mixed solution with 1L of sodium carbonate aqueous solution with the pH value of 10 in parallel flow at the flow rate of 10 ml/min, neutralizing the mixed solution obtained by parallel flow mixing at the stirring rate of 300rpm for 100 minutes at the neutralization temperature of 30 ℃, regulating the pH value by deionized water to obtain a neutralized slurry with the pH value of 7.5, and performing third aging treatment on the neutralized slurry at the temperature of 30 ℃ for 60 minutes to obtain mixed source slurry;
introducing 1 liter of sodium metaaluminate aqueous solution in a flowing state into the mixed gas containing carbon dioxide at a volume flow rate of 1 standard cubic meter per hour, performing a gelling reaction at a temperature of 30 ℃ for 60 minutes to obtain a gelling slurry with a pH value of 9.0, performing first aging treatment on the gelling slurry at the temperature of 65 ℃ for 25 minutes to obtain an aged gelling slurry, adding 57.8 grams of ammonium bicarbonate into the aged gelling slurry, and performing reaming treatment at 70 ℃ for 24 hours to obtain an aluminum source slurry, wherein the carbon dioxide accounts for 40 percent of the volume of the mixed gas containing carbon dioxide, and each liter of sodium metaaluminate aqueous solution contains 60 grams of sodium metaaluminate;
mixing 3 liters of mixed source slurry and 1 liter of aluminum source slurry at normal temperature to obtain mixed slurry, performing second aging treatment on the mixed slurry at 30 ℃ for 90 minutes, then performing filtration treatment until the content of sodium ions in filtrate is less than 1%, and finally performing drying treatment at 80 ℃ for 16 hours to obtain dry powder;
roasting the catalyst powder for 8 hours at 200 ℃, then carrying out reduction treatment for 8 hours at 250 ℃, finally carrying out passivation treatment for 12 hours at 20 ℃ by introducing nitrogen mixed air to obtain the petroleum resin hydrogenation catalyst, wherein the specific surface area of the petroleum resin hydrogenation catalyst is 300 square meters per gram, the pore volume is 0.5 cubic centimeters per gram, and the pore diameter is 20nm, and the petroleum resin hydrogenation catalyst is marked as sample 1.
Example 2
Preparation of sample 2
467 g of nickel nitrate hexahydrate, 73 g of zinc nitrate hexahydrate and 24.5 g of magnesium nitrate hexahydrate are weighed and dissolved in water to prepare 2 liters of mixed solution, the 2 liters of mixed solution and 1 liter of sodium carbonate aqueous solution with the pH value of 10 are mixed in parallel at the flow rate of 20 milliliters/minute, the mixed solution obtained by parallel flow mixing is subjected to neutralization treatment with the stirring rate of 400rpm at the temperature of 80 ℃ for the neutralization time of 20 minutes, the pH value of the neutralized slurry is regulated by deionized water to obtain neutralized slurry with the pH value of 9.5, and the neutralized slurry is subjected to third aging treatment at the temperature of 80 ℃ for 5 minutes to obtain mixed source slurry;
introducing 1 liter of sodium metaaluminate aqueous solution in a flowing state into the mixed gas containing carbon dioxide at a volume flow rate of 4 standard cubic meters per hour, performing a gelling reaction at a temperature of 65 ℃ for 50 minutes to obtain a gelling slurry with a pH value of 10.5, performing first aging treatment on the gelling slurry at the temperature of 65 ℃ for 35 minutes to obtain an aged gelling slurry, adding 57.8 grams of ammonium bicarbonate into the aged gelling slurry, and performing reaming treatment at 150 ℃ for 12 hours to obtain an aluminum source slurry, wherein the carbon dioxide accounts for 90 percent of the volume of the mixed gas containing carbon dioxide, and each liter of sodium metaaluminate aqueous solution contains 60 grams of sodium metaaluminate;
mixing 3 liters of mixed source slurry and 1 liter of aluminum source slurry at normal temperature to obtain mixed slurry, performing second aging treatment on the mixed slurry at 80 ℃ for 30 minutes, then performing filtration treatment until the content of sodium ions in filtrate is less than 1%, and finally performing drying treatment at 150 ℃ for 6 hours to obtain dry powder;
roasting the catalyst powder for 6 hours at 400 ℃, then reducing for 6 hours at 500 ℃, finally introducing nitrogen mixed air for passivation for 8 hours at 30 ℃ to obtain the petroleum resin hydrogenation catalyst, wherein the specific surface area of the petroleum resin hydrogenation catalyst is 320 square meters/gram, the pore volume is 0.6 cubic centimeters/gram, and the pore diameter is 30nm, and the petroleum resin hydrogenation catalyst is marked as sample 2.
Example 3
Preparation of sample 3
467 g of nickel nitrate hexahydrate, 73 g of zinc nitrate hexahydrate and 70 g of magnesium nitrate hexahydrate, and dissolving the nickel nitrate hexahydrate, the zinc nitrate hexahydrate and the 70 g of magnesium nitrate hexahydrate in water to prepare 2 liters of mixed solution, mixing the 2 liters of mixed solution with 1 liter of sodium carbonate aqueous solution with the pH value of 10 at the flow rate of 10 milliliters/minute in parallel flow, neutralizing the mixed solution obtained by parallel flow mixing at the stirring rate of 500rpm for the neutralization treatment with the neutralization temperature of 50 ℃ for 65 minutes, regulating the pH value by using deionized water to obtain a neutralized slurry with the pH value of 8.0, and carrying out third aging treatment on the neutralized slurry at the temperature of 50 ℃ for 30 minutes to obtain mixed source slurry;
introducing 1 liter of sodium metaaluminate aqueous solution in a flowing state into the mixed gas containing carbon dioxide at a volume flow rate of 2 standard cubic meters per hour, performing a gelling reaction at a temperature of 40 ℃ for 55 minutes to obtain a gelling slurry with a pH value of 9.0, performing first aging treatment on the gelling slurry at the temperature of 65 ℃ for 25 minutes to obtain an aged gelling slurry, adding 57.8 grams of ammonium bicarbonate into the aged gelling slurry, and performing reaming treatment at the temperature of 90 ℃ for 14 hours to obtain an aluminum source slurry, wherein the carbon dioxide accounts for 50 percent of the volume of the mixed gas containing carbon dioxide, and each liter of sodium metaaluminate aqueous solution contains 60 grams of sodium metaaluminate;
mixing 3 liters of mixed source slurry and 1 liter of aluminum source slurry at normal temperature to obtain mixed slurry, performing second aging treatment on the mixed slurry at 40 ℃ for 80 minutes, then performing filtration treatment until the content of sodium ions in filtrate is less than 1%, and finally performing drying treatment at 100 ℃ for 14 hours to obtain dry powder;
roasting the catalyst powder for 4 hours at 600 ℃, then reducing for 4 hours at 700 ℃, finally introducing nitrogen mixed air for passivation at 50 ℃ for 6 hours to obtain the petroleum resin hydrogenation catalyst, wherein the specific surface area of the petroleum resin hydrogenation catalyst is 320 square meters/gram, the pore volume is 0.7 cubic centimeters/gram, and the pore diameter is 30nm, and the petroleum resin hydrogenation catalyst is marked as sample 3.
Example 4
Preparation of sample 4
467 g of nickel nitrate hexahydrate, 73 g of zinc nitrate hexahydrate and 70 g of magnesium nitrate hexahydrate, and dissolving the nickel nitrate hexahydrate, the zinc nitrate hexahydrate and the 70 g of magnesium nitrate hexahydrate in water to prepare 2 liters of mixed solution, mixing the 2 liters of mixed solution with 1 liter of sodium carbonate aqueous solution with the pH value of 10 at the flow rate of 10 milliliters/minute in parallel flow, neutralizing the mixed solution obtained by parallel flow mixing at the stirring rate of 500rpm for the neutralization treatment of 70 ℃ for 35 minutes, regulating the pH value by using deionized water to obtain a neutralized slurry with the pH value of 8.5, and carrying out third aging treatment on the neutralized slurry at the temperature of 70 ℃ for 13 minutes to obtain mixed source slurry;
introducing 1 liter of sodium metaaluminate aqueous solution in a flowing state into the mixed gas containing carbon dioxide at a volume flow rate of 3 standard cubic meters per hour, performing a gelling reaction at a temperature of 50 ℃ for 50 minutes to obtain a gelling slurry with a pH value of 10.0, performing first aging treatment on the gelling slurry at the temperature of 50 ℃ for 30 minutes to obtain an aged gelling slurry, adding 96 grams of ammonium bicarbonate into the aged gelling slurry, and performing reaming treatment at 110 ℃ for 16 hours to obtain an aluminum source slurry, wherein the carbon dioxide accounts for 60 percent of the volume of the mixed gas containing carbon dioxide, and each liter of sodium metaaluminate aqueous solution contains 100 grams of sodium metaaluminate;
mixing 3 liters of mixed source slurry and 1 liter of aluminum source slurry at normal temperature to obtain mixed slurry, performing second aging treatment on the mixed slurry at 50 ℃ for 70 minutes, then performing filtration treatment until the content of sodium ions in filtrate is less than 1%, and finally performing drying treatment at 120 ℃ for 8 hours to obtain dry powder;
roasting the catalyst powder for 4 hours at 500 ℃, then carrying out reduction treatment for 4 hours at 500 ℃, finally carrying out passivation treatment for 10 hours at 20 ℃ by introducing nitrogen mixed air to obtain the petroleum resin hydrogenation catalyst, wherein the specific surface area of the petroleum resin hydrogenation catalyst is 320 square meters per gram, the pore volume is 0.8 cubic centimeters per gram, and the pore diameter is 30nm, and the petroleum resin hydrogenation catalyst is marked as sample 4.
Example 5
Preparation of sample 5
467 g of nickel nitrate hexahydrate, 73 g of zinc nitrate hexahydrate and 70 g of magnesium nitrate hexahydrate, and dissolving the nickel nitrate hexahydrate, the zinc nitrate hexahydrate and the 70 g of magnesium nitrate hexahydrate in water to prepare 2 liters of mixed solution, mixing the 2 liters of mixed solution with 1 liter of sodium carbonate aqueous solution with the pH value of 10 in parallel at the flow rate of 20 milliliters/minute, neutralizing the mixed solution obtained by the parallel mixing at the stirring rate of 500rpm for the neutralization treatment with the neutralization temperature of 55 ℃ for 70 minutes, regulating the pH value by using deionized water to obtain a neutralization slurry with the pH value of 9.0, and carrying out third aging treatment on the neutralization slurry at the temperature of 55 ℃ for 32 minutes to obtain mixed source slurry;
introducing 1 liter of sodium metaaluminate aqueous solution in a flowing state into the mixed gas containing carbon dioxide at a volume flow rate of 2.5 standard cubic meters per hour, performing a gelling reaction at 46 ℃ for 55 minutes to obtain a gelling slurry with a pH value of 9.0, performing first aging treatment on the gelling slurry at 46 ℃ for 30 minutes to obtain an aged gelling slurry, adding 145 grams of ammonium bicarbonate into the aged gelling slurry, and performing reaming treatment at 110 ℃ for 24 hours to obtain an aluminum source slurry, wherein the carbon dioxide accounts for 65% of the volume of the mixed gas containing carbon dioxide, and each liter of sodium metaaluminate aqueous solution contains 100 grams of sodium metaaluminate;
mixing 3 liters of mixed source slurry and 1 liter of aluminum source slurry at normal temperature to obtain mixed slurry, performing second aging treatment on the mixed slurry at 55 ℃ for 60 minutes, then performing filtration treatment until the content of sodium ions in filtrate is less than 1%, and finally performing drying treatment at 115 ℃ for 11 hours to obtain dry powder;
roasting the catalyst powder for 6 hours at 400 ℃, then reducing for 6 hours at 400 ℃, finally introducing nitrogen mixed air at 50 ℃ for passivation treatment for 4 hours to obtain the petroleum resin hydrogenation catalyst, wherein the specific surface area of the nickel-based hydrogenation catalyst is 360 square meters per gram, the pore volume is 1.0 cubic centimeter per gram, the pore diameter is 60nm, and the sample is marked as sample 5.
Comparative example 1
Comparative sample 1 preparation
Weighing 467 g of nickel nitrate hexahydrate and 24.5 g of magnesium nitrate hexahydrate, dissolving the nickel nitrate hexahydrate and the magnesium nitrate hexahydrate in water to prepare 2 liters of mixed solution, mixing the 2 liters of mixed solution with 1 liter of sodium carbonate aqueous solution with the pH value of 10 at the flow rate of 10 milliliters/minute in parallel flow, neutralizing the mixed solution obtained by parallel flow mixing at the stirring rate of 300rpm for a neutralization treatment with the neutralization temperature of 30 ℃ for 100 minutes, regulating the pH value by using deionized water to obtain a neutralization slurry with the pH value of 7.5, and carrying out third aging treatment on the neutralization slurry at the temperature of 30 ℃ for 60 minutes to obtain mixed source slurry;
introducing 1 liter of sodium metaaluminate aqueous solution in a flowing state into the mixed gas containing carbon dioxide at a volume flow rate of 1 standard cubic meter per hour, performing a gelling reaction at a temperature of 30 ℃ for 60 minutes to obtain a gelling slurry with a pH value of 9.0, performing first aging treatment on the gelling slurry at the temperature of 65 ℃ for 25 minutes to obtain an aged gelling slurry, adding 57.8 grams of ammonium bicarbonate into the aged gelling slurry, and performing reaming treatment at 70 ℃ for 24 hours to obtain an aluminum source slurry, wherein the carbon dioxide accounts for 40 percent of the volume of the mixed gas containing carbon dioxide, and each liter of sodium metaaluminate aqueous solution contains 60 grams of sodium metaaluminate;
mixing 3 liters of mixed source slurry and 1 liter of aluminum source slurry at normal temperature to obtain mixed slurry, performing second aging treatment on the mixed slurry at 30 ℃ for 90 minutes, then performing filtration treatment until the content of sodium ions in filtrate is less than 1%, and finally performing drying treatment at 80 ℃ for 16 hours to obtain dry powder;
roasting the catalyst powder for 8 hours at 200 ℃, then carrying out reduction treatment for 8 hours at 250 ℃, finally carrying out passivation treatment for 12 hours at 20 ℃ by introducing nitrogen mixed air to obtain the petroleum resin hydrogenation catalyst, wherein the specific surface area of the petroleum resin hydrogenation catalyst is 280 square meters per gram, the pore volume is 0.5 cubic centimeters per gram, and the pore diameter is 20nm, and the petroleum resin hydrogenation catalyst is recorded as a comparative sample 1.
Comparative example 2
Comparative sample 2 preparation
Weighing 467 g of nickel nitrate hexahydrate and 14.6 g of zinc nitrate hexahydrate, dissolving the nickel nitrate hexahydrate and 14.6 g of zinc nitrate hexahydrate in water to prepare 2 liters of mixed solution, mixing 2 liters of mixed solution with 1 liter of sodium carbonate aqueous solution with the pH value of 10 at the flow rate of 10 milliliters/minute in parallel, neutralizing the mixed solution obtained by parallel mixing at the stirring rate of 300rpm for the neutralization treatment with the neutralization temperature of 30 ℃ for 100 minutes, regulating the pH value by using deionized water to obtain a neutralized slurry with the pH value of 7.5, and carrying out third aging treatment on the neutralized slurry at the temperature of 30 ℃ for 60 minutes to obtain mixed source slurry;
introducing 1 liter of sodium metaaluminate aqueous solution in a flowing state into the mixed gas containing carbon dioxide at a volume flow rate of 1 standard cubic meter per hour, performing a gelling reaction at a temperature of 30 ℃ for 60 minutes to obtain a gelling slurry with a pH value of 9.0, performing first aging treatment on the gelling slurry at the temperature of 65 ℃ for 25 minutes to obtain an aged gelling slurry, adding 57.8 grams of ammonium bicarbonate into the aged gelling slurry, and performing reaming treatment at 70 ℃ for 24 hours to obtain an aluminum source slurry, wherein the carbon dioxide accounts for 40 percent of the volume of the mixed gas containing carbon dioxide, and each liter of sodium metaaluminate aqueous solution contains 60 grams of sodium metaaluminate;
mixing 3 liters of mixed source slurry and 1 liter of aluminum source slurry at normal temperature to obtain mixed slurry, performing second aging treatment on the mixed slurry at 30 ℃ for 90 minutes, then performing filtration treatment until the content of sodium ions in filtrate is less than 1%, and finally performing drying treatment at 80 ℃ for 16 hours to obtain dry powder;
roasting the catalyst powder for 8 hours at 200 ℃, then carrying out reduction treatment for 8 hours at 250 ℃, finally carrying out passivation treatment for 12 hours at 20 ℃ by introducing nitrogen mixed air to obtain the petroleum resin hydrogenation catalyst, wherein the specific surface area of the petroleum resin hydrogenation catalyst is 290 square meters per gram, the pore volume is 0.5 cubic centimeters per gram, and the pore diameter is 20nm, and the petroleum resin hydrogenation catalyst is recorded as a comparative sample 2.
Comparative example 3
Comparative sample 3 preparation
467 g of nickel nitrate hexahydrate, 73 g of zinc nitrate hexahydrate and 70 g of magnesium nitrate hexahydrate, and dissolving the nickel nitrate hexahydrate, the zinc nitrate hexahydrate and the 70 g of magnesium nitrate hexahydrate in water to prepare 2 liters of mixed solution, mixing the 2 liters of mixed solution with 1 liter of sodium carbonate aqueous solution with the pH value of 10 at the flow rate of 10 milliliters/minute in parallel flow, neutralizing the mixed solution obtained by parallel flow mixing at the stirring rate of 500rpm for the neutralization treatment of 70 ℃ for 35 minutes, regulating the pH value by using deionized water to obtain a neutralized slurry with the pH value of 8.5, and carrying out third aging treatment on the neutralized slurry at the temperature of 70 ℃ for 13 minutes to obtain mixed source slurry;
introducing 1 liter of sodium metaaluminate aqueous solution in a flowing state into the mixed gas containing carbon dioxide at a volume flow rate of 3 standard cubic meters per hour, performing a gel forming reaction at a temperature of 50 ℃ for 50 minutes to obtain a gel forming slurry with a pH value of 10.0, and performing first aging treatment on the gel forming slurry at the temperature of 50 ℃ for 30 minutes to obtain an aged gel forming slurry, wherein the carbon dioxide accounts for 60 percent of the volume of the mixed gas containing carbon dioxide, and each liter of sodium metaaluminate aqueous solution contains 100 grams of sodium metaaluminate;
mixing 3 liters of mixed source slurry and 1 liter of aluminum source slurry at normal temperature to obtain mixed slurry, performing second aging treatment on the mixed slurry at 50 ℃ for 70 minutes, then performing filtration treatment until the content of sodium ions in filtrate is less than 1%, and finally performing drying treatment at 120 ℃ for 8 hours to obtain dry powder;
roasting the catalyst powder for 4 hours at 500 ℃, then carrying out reduction treatment for 4 hours at 500 ℃, finally carrying out passivation treatment for 10 hours at 20 ℃ by introducing nitrogen mixed air to obtain the petroleum resin hydrogenation catalyst, wherein the specific surface area of the petroleum resin hydrogenation catalyst is 200 square meters per gram, the pore volume is 0.4 cubic centimeters per gram, the pore diameter is 6nm, and the petroleum resin hydrogenation catalyst is marked as a comparative sample 3.
Table 1 shows the composition and physical parameters of samples 1-5 and comparative samples 1-3. Wherein the specific surface area unit is square meter/g, the pore volume unit is cubic centimeter/g, the pore diameter is nanometer, and the nickel content, the zinc content, the magnesium content and the aluminum oxide content are all in mass percent.
TABLE 1
The conditions of the hydrogenation and decoloration reaction are as follows: the petroleum resin hydrogenation catalyst is placed in a high-pressure reaction kettle, dicyclopentadiene petroleum resin solution is added into the high-pressure reaction kettle to carry out hydrogenation and decoloration reaction with hydrogen, the temperature of the hydrogenation and decoloration reaction is 230 ℃, the pressure of the hydrogenation and decoloration reaction is 6 megapascals, the dicyclopentadiene petroleum resin solution is obtained by dissolving dicyclopentadiene petroleum resin in an organic solvent, the mass ratio of the organic solvent to dicyclopentadiene is 0.01:1, the organic solvent is a mixture of one or more hydrocarbons in alkanes, cycloalkanes and solvent oil, and the boiling point of alkane is less than 250 ℃.
The product color number, bromine number, softening point and product yield are compared with the hydrogenation effect of the petroleum resin hydrogenation catalyst by analyzing the product color number, bromine number, softening point and product yield.
Color number was analyzed using GB/T22295-2008 Gardner chromaticity.
The softening point of the product is analyzed by adopting a GB/T2294-2019 coking solid soft change point analysis method.
The bromine number is analyzed by adopting GB/T24138-2009 petroleum resin bromine number analysis standard, and the hydrogenation rate is calculated, wherein the calculation formula of the hydrogenation rate is as follows: (raw bromine number-product bromine number)/raw bromine number 100%.
The calculation formula of the product yield is as follows: product yield = product resin mass/raw resin mass 100%.
The nickel-based hydrogenation catalysts of samples 1-5 and comparative samples 1-3 were used for the hydrodecoloration of DCPD petroleum resins and the resulting effect experimental data are shown in Table 2.
TABLE 2
As can be seen from table 2, comparing sample 1 with comparative sample 1, the hydrogenation rate and yield of the product are both improved by adding zinc as an active component, and the addition of zinc can make nickel more uniformly distributed on the surface of the carrier and maintain the stability of the micro morphology of the active site of nickel on the carrier; as can be seen by comparing the sample 1 with the comparative sample 2, the softening point, hydrogenation rate and yield of the product are all improved by adding the magnesium as an active component, and the addition of magnesium is beneficial to adjusting the surface pH value of the nickel-based hydrogenation catalyst, improving the hydrogenation activity and selectivity of the nickel-based hydrogenation catalyst and reducing the production of byproducts with low molecular weight; as can be seen from comparison of the sample 1, the sample 5 and the comparison sample 3, the hydrogenation rate of the product can be improved by adding the pore-enlarging agent or increasing the proportion of the pore-enlarging agent, the pore-enlarging agent can increase the specific surface and the pore diameter of the catalyst, and the catalyst is more beneficial to the resin hydrogenation reaction and improves the hydrogenation rate.
The foregoing examples are illustrative only and serve to explain some features of the method of the invention. The appended claims are intended to claim the broadest possible scope and the embodiments presented herein are merely illustrative of selected implementations based on combinations of all possible embodiments. It is, therefore, not the intention of the applicant that the appended claims be limited by the choice of examples illustrating the features of the invention. Some numerical ranges used in the claims also include sub-ranges within which variations in these ranges should also be construed as being covered by the appended claims where possible.
Claims (10)
1. The petroleum resin hydrogenation catalyst is applied to hydrogenation decolorization of dicyclopentadiene petroleum resin, and is characterized by comprising an active component and a carrier, wherein the active component is nickel, zinc and magnesium, and the carrier is an alumina carrier;
the catalyst comprises, by mass, 40-80% of nickel, 1-10% of zinc, 1-7% of magnesium and 10-58% of alumina carrier;
the specific surface area of the petroleum resin hydrogenation catalyst is 200-400 square meters per gram, the pore volume is 0.5-1.0 cubic centimeter per gram, and the pore diameter is 10-100nm.
2. A method for preparing the petroleum resin hydrogenation catalyst according to claim 1, comprising the steps of:
s0: providing a mixed source slurry and an aluminum source slurry, wherein the mixed source slurry comprises nickel, zinc and magnesium, and the volume ratio of the mixed source slurry to the aluminum source slurry is (2-4): 1;
s1: mixing the mixed source slurry and the aluminum source slurry to obtain mixed slurry, and sequentially performing first aging treatment, filtering washing treatment and drying treatment on the mixed slurry to obtain catalyst powder;
s2: and (3) roasting, reducing and passivating the catalyst powder in sequence to obtain the petroleum resin hydrogenation catalyst.
3. The method for preparing a petroleum resin hydrogenation catalyst according to claim 2, wherein said method for preparing an aluminum source slurry comprises: introducing a mixed gas containing carbon dioxide into a sodium metaaluminate aqueous solution in a flowing state to carry out a gelling reaction until a gelling slurry with the pH value of 9.0-10.5 is obtained, carrying out second aging treatment on the gelling slurry to obtain an aged gelling slurry, and adding a pore-expanding agent into the aged gelling slurry to carry out pore-expanding treatment to obtain the aluminum source slurry.
4. The method for preparing a petroleum resin hydrogenation catalyst according to claim 3, wherein the molar ratio of said pore-expanding agent to sodium metaaluminate in said aqueous sodium metaaluminate solution is (1-2): 1.
5. The method for preparing a petroleum resin hydrogenation catalyst according to claim 3, wherein the temperature of said reaming is 70-150 ℃, the time of said reaming is 12-24 hours, the temperature of said roasting is 180-700 ℃, and the time of said roasting is 2-8 hours.
6. The method for preparing a petroleum resin hydrogenation catalyst according to claim 2, wherein the temperature of the reduction treatment is 200-700 ℃, the time of the reduction treatment is 2-12 hours, and the gas source of the reduction treatment is hydrogen or hydrogen-nitrogen mixture.
7. The method for preparing a petroleum resin hydrogenation catalyst according to claim 2, wherein the temperature of said passivation treatment is 20-200 degrees celsius, the time of said passivation treatment is 2-24 hours, said passivation treatment step is to treat the reduced catalyst powder with a mixed gas containing nitrogen, said mixed gas further comprising any one of air, oxygen or carbon dioxide.
8. The method for preparing a petroleum resin hydrogenation catalyst according to claim 3, wherein the volume flow rate of said mixed gas containing carbon dioxide is 1-4 cm/hr, the volume percentage of carbon dioxide in said mixed gas containing carbon dioxide is 40-90%, and 50-150 g of said sodium metaaluminate is contained per liter of said aqueous sodium metaaluminate solution.
9. The method for preparing a petroleum resin hydrogenation catalyst according to claim 2, wherein said method for preparing a mixed source slurry comprises: and performing coprecipitation treatment on the mixed solution by using an alkaline saline solution as a precipitator to obtain mixed source slurry, wherein the mixed solution is prepared by dissolving a nickel compound, a zinc compound and a magnesium compound in water.
10. The use of the petroleum resin hydrogenation catalyst according to claim 1, wherein the petroleum resin hydrogenation catalyst is placed in a high-pressure reaction kettle, dicyclopentadiene petroleum resin solution is added into the high-pressure reaction kettle to carry out hydrogenation and decolorization reaction with hydrogen, the temperature of the hydrogenation and decolorization reaction is 180-280 ℃, the pressure of the hydrogenation and decolorization reaction is 5-10 megapascals, the dicyclopentadiene petroleum resin solution is obtained by dissolving dicyclopentadiene petroleum resin in an organic solvent, the mass ratio of the organic solvent to dicyclopentadiene is (0.001-0.2): 1, the organic solvent comprises at least one of alkane, cycloalkane and solvent oil, and the boiling point of the alkane is less than 250 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310205104.5A CN116273015A (en) | 2023-03-06 | 2023-03-06 | Petroleum resin hydrogenation catalyst and its preparation method and application |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310205104.5A CN116273015A (en) | 2023-03-06 | 2023-03-06 | Petroleum resin hydrogenation catalyst and its preparation method and application |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN116273015A true CN116273015A (en) | 2023-06-23 |
Family
ID=86828261
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202310205104.5A Pending CN116273015A (en) | 2023-03-06 | 2023-03-06 | Petroleum resin hydrogenation catalyst and its preparation method and application |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN116273015A (en) |
Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH11286514A (en) * | 1998-03-31 | 1999-10-19 | Arakawa Chem Ind Co Ltd | Production of hydrogenated peteroleum resin and hydrogenating catalyst used for the same production |
| JP2002275212A (en) * | 2001-03-21 | 2002-09-25 | Arakawa Chem Ind Co Ltd | Method for producing hydrogenated petroleum resin and hydrogenation catalyst used for the production method |
| CN101590411A (en) * | 2008-05-28 | 2009-12-02 | 北京三聚环保新材料股份有限公司 | A kind of non-noble metal hydrogenation catalyst and preparation method thereof |
| CN102451691A (en) * | 2010-10-15 | 2012-05-16 | 中国石油化工股份有限公司 | Preparation method of nickel-based hydrogenation catalyst |
| CN104117359A (en) * | 2013-04-27 | 2014-10-29 | 中国石油化工股份有限公司 | Preparation method of hydrogenation catalyst |
| CN107252688A (en) * | 2017-05-15 | 2017-10-17 | 北京石油化工学院 | A kind of DCPD hydrogenation of petroleum resin catalyst and its preparation method and application |
| CN107876056A (en) * | 2016-09-29 | 2018-04-06 | 中国石油化工股份有限公司 | A kind of hydrogenation of petroleum resin nickel catalyst, preparation method and applications |
| CN108864368A (en) * | 2017-05-15 | 2018-11-23 | 中国石油天然气股份有限公司 | Hydrogenation method for C-V petroleum resin |
| CN109261153A (en) * | 2017-12-27 | 2019-01-25 | 上海迅凯新材料科技有限公司 | A kind of loading type nickel-based catalyst and its preparation method and application |
| CN111548450A (en) * | 2020-06-17 | 2020-08-18 | 武汉科林化工集团有限公司 | Hydrogenation method of high-chlorine C9 petroleum resin |
| WO2020246765A1 (en) * | 2019-06-03 | 2020-12-10 | 한화솔루션 주식회사 | Method for preparing hydrogenated petroleum resin |
-
2023
- 2023-03-06 CN CN202310205104.5A patent/CN116273015A/en active Pending
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH11286514A (en) * | 1998-03-31 | 1999-10-19 | Arakawa Chem Ind Co Ltd | Production of hydrogenated peteroleum resin and hydrogenating catalyst used for the same production |
| JP2002275212A (en) * | 2001-03-21 | 2002-09-25 | Arakawa Chem Ind Co Ltd | Method for producing hydrogenated petroleum resin and hydrogenation catalyst used for the production method |
| CN101590411A (en) * | 2008-05-28 | 2009-12-02 | 北京三聚环保新材料股份有限公司 | A kind of non-noble metal hydrogenation catalyst and preparation method thereof |
| CN102451691A (en) * | 2010-10-15 | 2012-05-16 | 中国石油化工股份有限公司 | Preparation method of nickel-based hydrogenation catalyst |
| CN104117359A (en) * | 2013-04-27 | 2014-10-29 | 中国石油化工股份有限公司 | Preparation method of hydrogenation catalyst |
| CN107876056A (en) * | 2016-09-29 | 2018-04-06 | 中国石油化工股份有限公司 | A kind of hydrogenation of petroleum resin nickel catalyst, preparation method and applications |
| CN107252688A (en) * | 2017-05-15 | 2017-10-17 | 北京石油化工学院 | A kind of DCPD hydrogenation of petroleum resin catalyst and its preparation method and application |
| CN108864368A (en) * | 2017-05-15 | 2018-11-23 | 中国石油天然气股份有限公司 | Hydrogenation method for C-V petroleum resin |
| CN109261153A (en) * | 2017-12-27 | 2019-01-25 | 上海迅凯新材料科技有限公司 | A kind of loading type nickel-based catalyst and its preparation method and application |
| WO2020246765A1 (en) * | 2019-06-03 | 2020-12-10 | 한화솔루션 주식회사 | Method for preparing hydrogenated petroleum resin |
| CN111548450A (en) * | 2020-06-17 | 2020-08-18 | 武汉科林化工集团有限公司 | Hydrogenation method of high-chlorine C9 petroleum resin |
Non-Patent Citations (5)
| Title |
|---|
| JIANG MING 等: "C9 Petroleum Resin Hydrogenation over a PEG1000-Modified Nickel Catalyst Supported on a Recyclable Fluid Catalytic Cracking Catalyst Residue", 《ACS OMEGA》, vol. 5, no. 32, 18 August 2020 (2020-08-18), pages 20291 - 20298 * |
| LIU QUNHONG 等: "Tuning the properties of Ni-based catalyst via La incorporation for efficient hydrogenation of petroleum resin", 《CHINESE JOURNAL OF CHEMICAL ENGINEERING》, vol. 45, 20 July 2021 (2021-07-20), pages 41 - 50, XP087098577, DOI: 10.1016/j.cjche.2021.03.053 * |
| 任正操 等: "助剂对Ni/Al2O3催化剂在石油树脂加氢过程中抗硫性能的影响", 《当代化工》, vol. 39, no. 6, 28 December 2010 (2010-12-28), pages 620 - 621 * |
| 曾丰 等: "采用NaAlO2-CO2连续中和法制备拟薄水铝石", 《石油学报(石油加工)》, vol. 31, no. 5, 25 October 2015 (2015-10-25), pages 1069 - 1074 * |
| 李广超: "C9石油树脂加氢催化剂的开发", 《中国优秀硕士学位论文全文数据库 工程科技Ⅰ辑》, no. 6, 15 June 2020 (2020-06-15), pages 016 - 434 * |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102470343B (en) | Fischer-tropsch catalyst | |
| US4307248A (en) | Process for hydrogenating organic compounds by use of non-ferrous group VIII aluminum coprecipitated catalysts | |
| CN101426577B (en) | Bismuth molybdate-based catalysts, method of preparing thereof and method of preparing 1,3-butadiene using thereof | |
| US4273680A (en) | Supported non-ferrous group VIII aluminate coprecipitated hydrogenation catalysts and process for their preparation | |
| TWI637001B (en) | Process and catalyst for resin hydrogenation | |
| CN102002130B (en) | Preparation method of hydrogenated C9 petroleum resin | |
| CN111085241B (en) | Method for preparing aniline by nitrobenzene hydrogenation and preparation method of catalyst thereof | |
| CN102391426B (en) | Method for performing hydrogenating pretreatment on C9 petroleum resin | |
| CN101157029A (en) | A dicyclopentadiene hydrogenation special-purpose catalyzer and its preparing method | |
| CN106423284B (en) | Vinyl acetate catalyst and preparation method thereof | |
| CN106391073B (en) | A kind of cobalt-base catalyst directly preparing alkene for synthesis gas and its preparation method and application | |
| CN103819295A (en) | Application of catalyst to selective hydrogenation reaction of aromatic nitro compound | |
| CN112191261A (en) | Heterogeneous catalyst for catalytic hydrogenation reaction of C5 petroleum resin and application thereof | |
| EP3991842A1 (en) | Catalyst for hydrogenation reaction and method for producing same | |
| TW592809B (en) | Activation of passivated iron | |
| CN109529912B (en) | Composite nano-structure copper catalyst for preparing furfuryl alcohol by furfural hydrogenation and preparation method thereof | |
| US4318829A (en) | Non-ferrous group VIII aluminum coprecipitated hydrogenation catalysts | |
| CN116273015A (en) | Petroleum resin hydrogenation catalyst and its preparation method and application | |
| US4273939A (en) | Process for hydrogenating organic compounds by use of non-ferrous group VIII aluminum coprecipitated catalysts | |
| CN110508290B (en) | High-dispersion palladium/cobalt hydroxide catalyst and preparation method and application thereof | |
| JP7144208B2 (en) | Catalyst for producing cumene and its application | |
| CN110871075B (en) | Iron-cobalt-potassium-loaded zirconium dioxide catalyst, preparation method and application thereof | |
| CN109092301A (en) | It is used to prepare the catalyst and preparation method thereof of isopropylbenzene | |
| CN109092295A (en) | Isopropylbenzene catalyst and preparation method thereof | |
| CN109096029A (en) | The preparation method of isopropylbenzene |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |