CN108722402B - A kind of method of propane dehydrogenation catalyst and preparation method thereof and preparing propylene by dehydrogenating propane - Google Patents
A kind of method of propane dehydrogenation catalyst and preparation method thereof and preparing propylene by dehydrogenating propane Download PDFInfo
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- CN108722402B CN108722402B CN201710260709.9A CN201710260709A CN108722402B CN 108722402 B CN108722402 B CN 108722402B CN 201710260709 A CN201710260709 A CN 201710260709A CN 108722402 B CN108722402 B CN 108722402B
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- propane
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- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 222
- 239000001294 propane Substances 0.000 title claims abstract description 111
- 239000003054 catalyst Substances 0.000 title claims abstract description 84
- 238000006356 dehydrogenation reaction Methods 0.000 title claims abstract description 73
- 238000002360 preparation method Methods 0.000 title claims abstract description 42
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 title claims abstract description 36
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 title claims abstract description 36
- 238000000034 method Methods 0.000 title claims abstract description 35
- 239000002131 composite material Substances 0.000 claims abstract description 48
- 238000009826 distribution Methods 0.000 claims abstract description 24
- 239000011148 porous material Substances 0.000 claims abstract description 24
- 238000006243 chemical reaction Methods 0.000 claims abstract description 23
- 230000002902 bimodal effect Effects 0.000 claims abstract description 15
- 229910052751 metal Inorganic materials 0.000 claims abstract description 15
- 239000002184 metal Substances 0.000 claims abstract description 15
- 239000002245 particle Substances 0.000 claims abstract description 11
- 239000012065 filter cake Substances 0.000 claims description 37
- 150000003839 salts Chemical class 0.000 claims description 24
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 23
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 23
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 22
- 239000000243 solution Substances 0.000 claims description 19
- 239000000741 silica gel Substances 0.000 claims description 18
- 229910002027 silica gel Inorganic materials 0.000 claims description 18
- 239000013335 mesoporous material Substances 0.000 claims description 17
- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical compound [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 claims description 15
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 14
- BOTDANWDWHJENH-UHFFFAOYSA-N Tetraethyl orthosilicate Chemical compound CCO[Si](OCC)(OCC)OCC BOTDANWDWHJENH-UHFFFAOYSA-N 0.000 claims description 14
- 235000019353 potassium silicate Nutrition 0.000 claims description 14
- 150000007522 mineralic acids Chemical class 0.000 claims description 13
- 238000000498 ball milling Methods 0.000 claims description 12
- RPACBEVZENYWOL-XFULWGLBSA-M sodium;(2r)-2-[6-(4-chlorophenoxy)hexyl]oxirane-2-carboxylate Chemical compound [Na+].C=1C=C(Cl)C=CC=1OCCCCCC[C@]1(C(=O)[O-])CO1 RPACBEVZENYWOL-XFULWGLBSA-M 0.000 claims description 12
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 11
- 239000000908 ammonium hydroxide Substances 0.000 claims description 11
- 239000000463 material Substances 0.000 claims description 11
- 239000000843 powder Substances 0.000 claims description 10
- 239000000047 product Substances 0.000 claims description 10
- 239000007787 solid Substances 0.000 claims description 10
- LZZYPRNAOMGNLH-UHFFFAOYSA-M Cetrimonium bromide Chemical compound [Br-].CCCCCCCCCCCCCCCC[N+](C)(C)C LZZYPRNAOMGNLH-UHFFFAOYSA-M 0.000 claims description 8
- 239000001257 hydrogen Substances 0.000 claims description 8
- 229910052739 hydrogen Inorganic materials 0.000 claims description 8
- 238000007598 dipping method Methods 0.000 claims description 7
- 238000005470 impregnation Methods 0.000 claims description 7
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 6
- 229910021529 ammonia Inorganic materials 0.000 claims description 6
- 239000003795 chemical substances by application Substances 0.000 claims description 6
- 238000006555 catalytic reaction Methods 0.000 claims description 5
- 239000002904 solvent Substances 0.000 claims description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 4
- 239000011259 mixed solution Substances 0.000 claims description 4
- 230000035484 reaction time Effects 0.000 claims description 4
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims description 2
- 240000007594 Oryza sativa Species 0.000 claims description 2
- 235000007164 Oryza sativa Nutrition 0.000 claims description 2
- 229910017604 nitric acid Inorganic materials 0.000 claims description 2
- 125000000913 palmityl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 claims description 2
- 235000009566 rice Nutrition 0.000 claims description 2
- HRHBQGBPZWNGHV-UHFFFAOYSA-N azane;bromomethane Chemical compound N.BrC HRHBQGBPZWNGHV-UHFFFAOYSA-N 0.000 claims 1
- 150000001875 compounds Chemical class 0.000 claims 1
- XYIBRDXRRQCHLP-UHFFFAOYSA-N ethyl acetoacetate Chemical compound CCOC(=O)CC(C)=O XYIBRDXRRQCHLP-UHFFFAOYSA-N 0.000 claims 1
- 150000002431 hydrogen Chemical class 0.000 claims 1
- 229910052710 silicon Inorganic materials 0.000 claims 1
- 239000010703 silicon Substances 0.000 claims 1
- 230000003197 catalytic effect Effects 0.000 abstract description 5
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 19
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 8
- 239000004810 polytetrafluoroethylene Substances 0.000 description 8
- 239000011734 sodium Substances 0.000 description 8
- 238000005406 washing Methods 0.000 description 8
- 238000001035 drying Methods 0.000 description 7
- 238000004519 manufacturing process Methods 0.000 description 7
- 239000000203 mixture Substances 0.000 description 7
- VWDWKYIASSYTQR-UHFFFAOYSA-N sodium nitrate Chemical compound [Na+].[O-][N+]([O-])=O VWDWKYIASSYTQR-UHFFFAOYSA-N 0.000 description 7
- 238000001694 spray drying Methods 0.000 description 7
- 229910002621 H2PtCl6 Inorganic materials 0.000 description 6
- 229910021627 Tin(IV) chloride Inorganic materials 0.000 description 6
- -1 polypropylene Polymers 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- 239000012265 solid product Substances 0.000 description 6
- 239000007864 aqueous solution Substances 0.000 description 5
- 239000007795 chemical reaction product Substances 0.000 description 5
- 230000000052 comparative effect Effects 0.000 description 5
- HPGGPRDJHPYFRM-UHFFFAOYSA-J tin(iv) chloride Chemical compound Cl[Sn](Cl)(Cl)Cl HPGGPRDJHPYFRM-UHFFFAOYSA-J 0.000 description 5
- 239000012153 distilled water Substances 0.000 description 4
- 238000001914 filtration Methods 0.000 description 4
- 238000000227 grinding Methods 0.000 description 4
- 229910052708 sodium Inorganic materials 0.000 description 4
- 229910001415 sodium ion Inorganic materials 0.000 description 4
- 229910052718 tin Inorganic materials 0.000 description 4
- 238000002441 X-ray diffraction Methods 0.000 description 3
- 238000004458 analytical method Methods 0.000 description 3
- 239000003125 aqueous solvent Substances 0.000 description 3
- 235000013339 cereals Nutrition 0.000 description 3
- 238000002242 deionisation method Methods 0.000 description 3
- 239000008367 deionised water Substances 0.000 description 3
- 229910021641 deionized water Inorganic materials 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 229910052738 indium Inorganic materials 0.000 description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical class [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 238000006467 substitution reaction Methods 0.000 description 3
- 239000003643 water by type Substances 0.000 description 3
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 2
- UXAMZEYKWGPDBI-UHFFFAOYSA-N C(CCCCCCCCCCCCCCC)Br(C)(C)C Chemical compound C(CCCCCCCCCCCCCCC)Br(C)(C)C UXAMZEYKWGPDBI-UHFFFAOYSA-N 0.000 description 2
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 229910052804 chromium Inorganic materials 0.000 description 2
- 239000011651 chromium Substances 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 239000006185 dispersion Substances 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 229910000510 noble metal Inorganic materials 0.000 description 2
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 2
- 229910052697 platinum Inorganic materials 0.000 description 2
- FHMDYDAXYDRBGZ-UHFFFAOYSA-N platinum tin Chemical compound [Sn].[Pt] FHMDYDAXYDRBGZ-UHFFFAOYSA-N 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 238000001228 spectrum Methods 0.000 description 2
- 239000002023 wood Substances 0.000 description 2
- NLHHRLWOUZZQLW-UHFFFAOYSA-N Acrylonitrile Chemical compound C=CC#N NLHHRLWOUZZQLW-UHFFFAOYSA-N 0.000 description 1
- 238000004438 BET method Methods 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- NIPNSKYNPDTRPC-UHFFFAOYSA-N N-[2-oxo-2-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)ethyl]-2-[[3-(trifluoromethoxy)phenyl]methylamino]pyrimidine-5-carboxamide Chemical compound O=C(CNC(=O)C=1C=NC(=NC=1)NCC1=CC(=CC=C1)OC(F)(F)F)N1CC2=C(CC1)NN=N2 NIPNSKYNPDTRPC-UHFFFAOYSA-N 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- GOOHAUXETOMSMM-UHFFFAOYSA-N Propylene oxide Chemical compound CC1CO1 GOOHAUXETOMSMM-UHFFFAOYSA-N 0.000 description 1
- 239000004115 Sodium Silicate Substances 0.000 description 1
- WGLPBDUCMAPZCE-UHFFFAOYSA-N Trioxochromium Chemical compound O=[Cr](=O)=O WGLPBDUCMAPZCE-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- SWLVFNYSXGMGBS-UHFFFAOYSA-N ammonium bromide Chemical compound [NH4+].[Br-] SWLVFNYSXGMGBS-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910000423 chromium oxide Inorganic materials 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 239000003989 dielectric material Substances 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000000415 inactivating effect Effects 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 125000002347 octyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- JTXAHXNXKFGXIT-UHFFFAOYSA-N propane;prop-1-ene Chemical group CCC.CC=C JTXAHXNXKFGXIT-UHFFFAOYSA-N 0.000 description 1
- 239000010453 quartz Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 235000019795 sodium metasilicate Nutrition 0.000 description 1
- 229910052911 sodium silicate Inorganic materials 0.000 description 1
- 230000003595 spectral effect Effects 0.000 description 1
- 238000004230 steam cracking Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000000967 suction filtration Methods 0.000 description 1
- 239000012974 tin catalyst Substances 0.000 description 1
- 238000004876 x-ray fluorescence Methods 0.000 description 1
- 229910003158 γ-Al2O3 Inorganic materials 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
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/56—Platinum group metals
- B01J23/62—Platinum group metals with gallium, indium, thallium, germanium, tin or lead
- B01J23/622—Platinum group metals with gallium, indium, thallium, germanium, tin or lead with germanium, tin or lead
- B01J23/626—Platinum group metals with gallium, indium, thallium, germanium, tin or lead with germanium, tin or lead with tin
-
- 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
- B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
- B01J21/08—Silica
-
- 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
- B01J23/002—Mixed oxides other than spinels, e.g. perovskite
-
- 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
- B01J35/50—Catalysts, in general, characterised by their form or physical properties characterised by their shape or configuration
- B01J35/51—Spheres
-
- 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
- B01J35/633—Pore volume less than 0.5 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
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
- C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
- C07C5/333—Catalytic processes
- C07C5/3332—Catalytic processes with metal oxides or metal sulfides
-
- 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
- B01J2523/00—Constitutive chemical elements of heterogeneous catalysts
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
- C07C2521/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
- C07C2521/08—Silica
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
- C07C2523/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals combined with metals, oxides or hydroxides provided for in groups C07C2523/02 - C07C2523/36
- C07C2523/56—Platinum group metals
- C07C2523/62—Platinum group metals with gallium, indium, thallium, germanium, tin or lead
-
- 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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- Chemical & Material Sciences (AREA)
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- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
- Catalysts (AREA)
Abstract
The present invention relates to catalyst fields, disclose the method for a kind of propane dehydrogenation catalyst and preparation method thereof and preparing propylene by dehydrogenating propane, the propane dehydrogenation catalyst includes the main active component Pt of carrier and load on the carrier, metal promoter Sn and metal promoter Na, wherein, the carrier is the spherical mesoporous composite material of diplopore, the average particle diameter of the spherical mesoporous composite material of diplopore is 30-60 microns, specific surface area is 200-650 meters squared per gram, pore volume is 0.5-1.5 mls/g, pore-size distribution is bimodal distribution, and the bimodal corresponding most probable pore size is respectively 1.5-15 nanometers and 16-50 nanometers.The propane dehydrogenation catalyst shows good catalytic performance when reacting for preparing propylene by dehydrogenating propane, conversion of propane is high, and Propylene Selectivity is high, and catalyst stability is good.
Description
Technical field
The present invention relates to catalyst fields, and in particular, to a kind of propane dehydrogenation catalyst and preparation method thereof and propane
The method of dehydrogenation producing propylene.
Background technique
Propylene is the base stock of petrochemical industry, mainly for the production of polypropylene, acrylonitrile, acetone, propylene oxide, propylene
Acid and octyl alconyl etc..The supply half of propylene comes from refinery's by-product, separately has about 45% to come from steam cracking, a small amount of other substitution skills
Art.In recent years, the demand of propylene increases year by year, and traditional production of propylene has been unable to meet demand of the chemical industry to propylene,
Therefore propylene enhancing become research a big hot spot, wherein preparing propylene by dehydrogenating propane be propylene volume increase a major technique, ten
For many years, preparing propylene by dehydrogenating propane has become the important process process of industrialization production of propylene.The major catalytic of dehydrogenating propane
Agent has in chromium oxide/aluminum oxide catalyst and Uop Inc.'s Oleflex technique in ABB Lummus company Catofin technique
Platinum tin/aluminium oxide catalyst.Requirement of the chromium-based catalysts to raw material impurity is relatively low, on the low side compared with noble metal, but
It is that such catalyst is easy carbon distribution inactivation, will be regenerated every 15-30 minutes once, and since the chromium in catalyst is weight
Metal, environmental pollution is serious.The activity of platinum-tin catalyst is high, and selectivity is good, can reach reaction time several days, can bear compared with
For harsh process conditions, and to more environment-friendly, still, since noble metal platinum is expensive, lead to catalyst cost
It is higher.Preparing propylene by dehydrogenating propane technique realizes that industrialized production alreadys exceed 20 years, also many to the research of dehydrogenation,
But current catalyst is not still high there is conversion of propane and is easy to the defects of inactivating, and requires further improvement and perfect.Cause
This, the propane dehydrogenation catalyst for developing function admirable has realistic meaning.
In order to improve the reactivity worth of propane dehydrogenation catalyst, researcher has done many work.Such as: use molecular sieve
Class carrier substitutes traditional γ-Al2O3Carrier, effect preferably include MFI type micro porous molecular sieve (CN104307555A,
CN101066532A, CN101380587A, CN101513613A), mesostructured material (CN102389831A) and mesoporous
Molecular sieve SBA-15 (CN101972664A, CN101972664B) etc..However, currently used carrier specific surface area is smaller, such as
Fruit carries out bulky molecular catalysis reaction, macromolecular duct more difficult to get access, so that influencing catalytic effect.Therefore, it selects a kind of excellent
Carrier is one, dehydrogenating propane field urgent problem to be solved.
Summary of the invention
The purpose of the present invention is overcome existing propane dehydrogenation catalyst preparation process complexity, preparation process to easily cause ring
Border pollution, conversion of propane and the lower defect of Propylene Selectivity, provide a kind of propane dehydrogenation catalyst and preparation method thereof and
The method of preparing propylene by dehydrogenating propane.
To achieve the goals above, the present invention provides a kind of propane dehydrogenation catalysts, wherein the dehydrogenating propane catalysis
Agent includes main active component Pt, metal promoter Sn and the metal promoter Na of carrier and load on the carrier, wherein institute
Stating carrier is the spherical mesoporous composite material of diplopore, and the average particle diameter of the spherical mesoporous composite material of diplopore is that 30-60 is micro-
Rice, specific surface area are 200-650 meters squared per gram, and pore volume is 0.5-1.5 mls/g, and pore-size distribution is bimodal distribution, and institute
Stating bimodal corresponding most probable pore size is respectively 1.5-15 nanometers and 16-50 nanometers.
The present invention also provides a kind of preparation methods of propane dehydrogenation catalyst, wherein the preparation method includes: that will carry
Body is immersed in the mixed solution containing Pt salt, Sn salt and Na salt, is dried after the solution after dipping is then removed solvent
And roasting, wherein the carrier is the spherical mesoporous composite material of diplopore, the average particle of the spherical mesoporous composite material of diplopore
Diameter is 30-60 microns, and specific surface area is 200-650 meters squared per gram, and pore volume is 0.5-1.5 mls/g, and pore-size distribution is
Bimodal distribution, and the bimodal corresponding most probable pore size is respectively 1.5-15 nanometers and 16-50 nanometers.
The present invention also provides the propane dehydrogenation catalysts of preparation method of the present invention preparation.
The present invention also provides a kind of methods of preparing propylene by dehydrogenating propane, which comprises in catalyst and hydrogen
In the presence of, propane is subjected to dehydrogenation reaction, wherein the catalyst is propane dehydrogenation catalyst of the present invention.
Propane dehydrogenation catalyst of the invention has the advantage that
(1), pore volume biggish diplopore spherical mesoporous composite material larger using specific surface area of the invention is de- as propane
The carrier of hydrogen catalyst, above structure feature are conducive to metal component in carrier surface fine dispersion, and then can guarantee to prepare
Propane dehydrogenation catalyst function admirable；
(2) good catalytic performance is shown when catalyst provided by the invention is reacted for preparing propylene by dehydrogenating propane,
Conversion of propane is high, and Propylene Selectivity is high, and catalyst stability is good.
Also, the preparation method of the propane dehydrogenation catalyst of the invention step impregnation conventional using co-impregnation method substitution
Method, preparation process is simple, and condition is easily controllable, good repetitiveness.
Other features and advantages of the present invention will the following detailed description will be given in the detailed implementation section.
Detailed description of the invention
The drawings are intended to provide a further understanding of the invention, and constitutes part of specification, with following tool
Body embodiment is used to explain the present invention together, but is not construed as limiting the invention.In the accompanying drawings:
Fig. 1 is the X-ray diffracting spectrum of the spherical mesoporous composite material of diplopore of embodiment 1；
Fig. 2 is the SEM scanning electron microscope (SEM) photograph of the spherical mesoporous composite material of diplopore of embodiment 1；
Fig. 3 is the graph of pore diameter distribution of the spherical mesoporous composite material of diplopore of embodiment 1；
Fig. 4 is the grain size distribution of the spherical mesoporous composite material of diplopore of embodiment 1.
Specific embodiment
Detailed description of the preferred embodiments below.It should be understood that described herein specific
Embodiment is merely to illustrate and explain the present invention, and is not intended to restrict the invention.
The endpoint of disclosed range and any value are not limited to the accurate range or value herein, these ranges or
Value should be understood as comprising the value close to these ranges or value.For numberical range, between the endpoint value of each range, respectively
It can be combined with each other between the endpoint value of a range and individual point value, and individually between point value and obtain one or more
New numberical range, these numberical ranges should be considered as specific open herein.
The present invention provides a kind of propane dehydrogenation catalysts, wherein the propane dehydrogenation catalyst includes carrier and bears
Carry main active component Pt, metal promoter Sn and metal promoter Na on the carrier, wherein the carrier is that diplopore is spherical
Mesoporous composite material, the average particle diameter of the spherical mesoporous composite material of diplopore are 30-60 microns, specific surface area 200-
650 meters squared per grams, pore volume are 0.5-1.5 mls/g, and pore-size distribution is bimodal distribution, and the bimodal corresponding most probable
Aperture is respectively 1.5-15 nanometers and 16-50 nanometers.
In the present invention, relative to the propane dehydrogenation catalyst of 100 parts by weight, the content of the carrier is 97.5-
The content of 99.3 weight %, the main active component Pt is 0.2-0.5 weight %, and the content of metal promoter Sn is 0.2-1.2
The content of weight %, metal promoter Na are 0.3-0.8 weight %.
The present invention also provides a kind of preparation methods of propane dehydrogenation catalyst, wherein the preparation method includes: that will carry
Body is immersed in the mixed solution containing Pt salt, Sn salt and Na salt, is dried after the solution after dipping is then removed solvent
And roasting, wherein the carrier is the spherical mesoporous composite material of diplopore, the average particle of the spherical mesoporous composite material of diplopore
Diameter is 30-60 microns, and specific surface area is 200-650 meters squared per gram, and pore volume is 0.5-1.5 mls/g, and pore-size distribution is
Bimodal distribution, and the bimodal corresponding most probable pore size is respectively 1.5-15 nanometers and 16-50 nanometers.
In the present invention, the carrier, Pt salt, Sn salt and Na salt dosage make the propane dehydrogenation catalyst being prepared
In, on the basis of the total weight of the propane dehydrogenation catalyst, the content of the carrier be 97.5-99.3 weight %, Pt salt with
The content of Pt element meter is that content of 0.2-0.5 weight %, the Sn salt in terms of Sn element is 0.2-1.2 weight %, Na salt with Na member
The content of element meter is 0.3-0.8 weight %.
There is no particular limitation for selection of the present invention to the Pt salt, Sn salt and Na salt, can be with as long as water solubility
For the conventional selection of this field, for example, the Pt salt can be H2PtCl6, the Sn salt can be SnCl4, the Na salt can be with
For NaNO3。
Concentration no spy of the present invention to Pt salt, Sn salt and Na salt in the mixed solution containing Pt salt, Sn salt and Na salt
Other restriction can be the conventional selection of this field, for example, the concentration of the Pt salt is 0.10-0.30mol/l, the Sn salt
Concentration be 0.15-1.00mol/l, the concentration of the Na salt is 1.00-3.50mol/l.
In the present invention, propane dehydrogenation catalyst is prepared using the conventional step impregnation method of co-impregnation method substitution, is prepared
Simple process, condition is easily controllable, good repetitiveness.There is no particular limitation for condition of the present invention to the dipping, can be with
It is still, described under preferable case in order to improve the performance of prepared propane dehydrogenation catalyst for the conventional method of this field
The condition of dipping includes: that temperature is 25-50 DEG C, and the time is 2-6 hours.
In the present invention, the process of the removal solvent can be adopted with the conventional methods in the field, such as can be using rotation
Solvent in evaporimeter removal system.
In the present invention, the drying can carry out in drying box, and the roasting can carry out in Muffle furnace.The present invention
To the condition of the drying and roasting, also there is no particular limitation, can be the conventional selection of this field, for example, the drying
Condition may include: that temperature is 110-150 DEG C, and the time is 3-6 hours；The condition of the roasting may include: that temperature is 600-
650 DEG C, the time is 5-8 hours.
In the present invention, the preparation method of the spherical mesoporous composite material of diplopore includes:
(1) cetyl trimethylammonium bromide, ethyl orthosilicate are contacted with ammonium hydroxide, and by the product mistake after contact
Filter, obtains mesoporous material filter cake；
(2) waterglass is contacted with inorganic acid, and the product obtained after contact is filtered, obtain silica gel filter cake；
(3) the mesoporous material filter cake is uniformly mixed to simultaneously ball milling, and the solid powder that will be obtained after ball milling with silica gel filter cake
It is spray-dried and is calcined after the water slurrying of end.
It is main to pass through control mesoporous material filter cake and silica gel in the preparation process of the spherical mesoporous composite material of above-mentioned diplopore
The composition of filter cake controls pore-size distribution for bimodal distribution, and the spherical mesoporous composite material of the diplopore is made to have diplopore distribution knot
Structure；And it (that is, mesoporous material filter cake to be first uniformly mixed to simultaneously ball milling with silica gel filter cake, is then incited somebody to action by control forming method
To solid powder water slurrying after be spray-dried) microscopic appearance of the spherical mesoporous composite material of the diplopore is controlled as ball
Shape.
In the present invention, during preparing mesoporous material filter cake, the dosage of each substance can in a wider scope into
Row selects and adjustment, under preferable case, in step (1), and the ethyl orthosilicate, cetyl trimethylammonium bromide, ammonium hydroxide
In ammonia and water molar ratio be 1:0.1-1:0.1-5:100-200, preferably 1:0.1-0.5:2-4:120-160.
The present invention does not limit the condition that cetyl trimethylammonium bromide, ethyl orthosilicate are contacted with ammonium hydroxide particularly
It is fixed, such as may include: the temperature of contact be 25-100 DEG C, preferably 50-100 DEG C；Time is 1-10 hours, preferably 2-6
Hour.
The condition that the present invention contacts the waterglass with inorganic acid is not particularly limited, for example, in step (2),
The condition that the waterglass is contacted with inorganic acid generally includes: temperature can be 10-60 DEG C, preferably 20-40 DEG C；Time can be with
It is 1-5 hours, preferably 1.5-3 hours, pH value 2-4.In order to be more advantageous to the uniform mixing between each substance, the waterglass
It contacts with inorganic acid and preferably carries out under agitation.
In the present invention, the waterglass is the aqueous solution of sodium metasilicate, and concentration is preferably 3-20 weight %.
In the present invention, the type of the inorganic acid can be the conventional selection of this field, for example, can be sulfuric acid, nitric acid
With one of hydrochloric acid or a variety of.The inorganic acid can use in pure form, can also be made in the form of its aqueous solution
With when inorganic acid is aqueous solution, preferably the concentration of inorganic acid aqueous solution is 3-20 weight %.The dosage of the inorganic acid is preferred
So that the pH value of the contact conditions reaction system of waterglass and inorganic acid is 2-4.
In addition, it is above-mentioned prepare mesoporous material filter cake and silica gel filter cake during, the mistake of filter cake is obtained by filtering
Journey may include: after filtration, washs (washing times can be 2-10) repeatedly with distilled water, is then filtered.It is described
The process of washing can for washing or it is pure wash it is one or more.Preferably, the washing during mesoporous material filter cake is prepared
So that filter cake PH is 7, the washing during silica gel filter cake is prepared so that sodium ions content is lower than 0.02 weight %.
In the present invention, in step (3), the dosage of the mesoporous material filter cake and silica gel filter cake can be obtained according to expection
The component of the spherical mesoporous composite material of the equally distributed diplopore of diplopore selected, under preferable case, in step (3), be situated between
The weight ratio of the dosage of the dosage and silica gel filter cake of Porous materials filter cake is 1:0.1-2.
In the present invention, there is no particular limitation for concrete operation method and condition to the ball milling, not destroy or substantially
The structure of carrier is not destroyed and enters silica gel subject to carrier duct.Those skilled in the art can select each according to mentioned above principle
Suitable condition is planted to implement the present invention.Specifically, the ball milling carries out in the ball mill, wherein abrading-ball is straight in ball mill
Diameter can be 2-3mm；The quantity of abrading-ball can reasonably be selected according to the size of ball grinder, be 50-150mL for size
Ball grinder, 1 abrading-ball usually can be used；The material of the abrading-ball can be agate, polytetrafluoroethylene (PTFE) etc., preferably Ma
Nao.The condition of the ball milling includes: that the revolving speed of abrading-ball can be 300-500r/min, and the temperature in ball grinder can be 15-100
DEG C, the time of ball milling can be 0.1-100 hours.
In the present invention, the concrete operation method and condition of the spray drying are known to the skilled person.Specifically,
The slurry being made by the solid powder and water is added in atomizer high speed rotation to realize spray drying.Wherein, described
The condition of spray drying includes: that temperature can be 150-600 DEG C, and the revolving speed of rotation can be 10000-15000r/min；It is preferred that
In the case of, the condition of the spray drying includes: that temperature is 150-250 DEG C, and the revolving speed of rotation is 11000-13000r/min；Most
Under preferable case, the condition of the spray drying includes: that temperature is 200 DEG C, and the revolving speed of rotation is 12000r/min.
In the present invention, the condition of the calcining may include: that temperature is 90-600 DEG C, preferably 200-500 DEG C；Time is
10-80 hours, preferably 20-30 hours.
The present invention also provides the propane dehydrogenation catalysts that preparation method of the present invention is prepared.The dehydrogenating propane
Catalyst is using specific surface area is larger, the spherical mesoporous composite material of the biggish diplopore of pore volume is as carrier, above structure feature
Be conducive to metal component in carrier surface fine dispersion, and then can guarantee the propane dehydrogenation catalyst function admirable of preparation.
The present invention also provides a kind of methods of preparing propylene by dehydrogenating propane, which comprises in catalyst and hydrogen
In the presence of, propane is subjected to dehydrogenation reaction, wherein the catalyst is propane dehydrogenation catalyst of the present invention.
In the present invention, in order to improve conversion of propane and prevent catalyst coking, under preferable case, the dosage and hydrogen of propane
The molar ratio of the dosage of gas is 0.5-1.5:1.
There is no particular limitation for condition of the present invention to the dehydrogenation reaction, can be the conventional selection of this field, such as
The condition of the dehydrogenation reaction may include: that reaction temperature is 600-650 DEG C, reaction pressure 0.05-0.2MPa, the reaction time
For 40-60h, propane mass space velocity is 2-5h-1。
It below will the present invention will be described in detail by embodiment and comparative example.
In following embodiment and comparative example, X-ray diffraction analysis is in the model for being purchased from Bruker AXS company, Germany
It is carried out on the X-ray diffractometer of D8Advance；Scanning of the scanning electron microscope analysis in the model XL-30 purchased from FEI Co., the U.S.
It is carried out on electron microscope；Pore structure parameter analysis is in the ASAP2020-M+C purchased from the production of U.S. Micromeritics company
It is carried out on type adsorption instrument, the specific surface area and pore volume of sample, which calculate, uses BET method；The particle diameter distribution of sample swashs in Malvern
It is carried out on light particle size analyzer；Rotary Evaporators are the production of IKA company, Germany, model RV10digital；Propane dehydrogenation catalyst
Activity component load quantity is in the Wavelength Dispersive-X-Ray fluorescence spectrum for being Axios-Advanced purchased from Dutch Panaco company model
It is measured on instrument；The analysis of reaction product ingredient carries out on the gas chromatograph purchased from agilent company model 7890A；
In following EXPERIMENTAL EXAMPLE and Experimental comparison's example, the conversion ratio (%) of propane=(in dosage-reaction product of propane
The content of propane) ÷ propane dosage × 100%；
Theoretical yield × 100% of selectivity (%)=propylene actual production ÷ propylene of propylene；
Embodiment 1
The embodiment is for illustrating propane dehydrogenation catalyst and preparation method thereof.
(1) preparation of the spherical mesoporous composite material of diplopore
At 80 DEG C, cetyl trimethylammonium bromide and ethyl orthosilicate are added to the ammonium hydroxide that concentration is 25 weight %
In solution, deionized water is added, wherein the additional amount of ethyl orthosilicate is 1g, ethyl orthosilicate, cetyl trimethyl bromine
The molar ratio for changing ammonium, the ammonia in ammonium hydroxide and water is 1:0.37:2.8:142, and is stirred 4 hours at a temperature of 80 DEG C, then will be molten
It is 7 that liquid, which filters and is washed with distilled water to pH, obtains mesoporous material filter cake.
By the waterglass that concentration is 15 weight % and the sulfuric acid solution that concentration is 12 weight %, and press waterglass: sulfuric acid
Weight ratio is uniformly mixed for 5:1, is then stirred to react at 20 DEG C 1.5 hours, and is 98 by obtained reaction product concentration
The sulfuric acid adjustment pH of weight % is 3, and reaction mass is then lower than 0.02 weight by filtering, distilling water washing to sodium ions content
% is measured, silica gel filter cake is obtained.
10 grams of dielectric material filter cakes of above-mentioned preparation and 10 grams of silica gel filter cakes are put into togerther (wherein, ball in 100mL ball grinder
Grinding jar material is polytetrafluoroethylene (PTFE), and Material quality of grinding balls is agate, and the diameter of abrading-ball is 3mm, and quantity is 1, revolving speed 400r/
Min), ball grinder is closed, temperature is to obtain 20 grams of solid powders ball milling 1 hour at 60 DEG C in ball grinder；By the solid powder
It is dissolved in 50 grams of deionized waters, and is spray-dried at 200 DEG C in the case where revolving speed is 12000r/min；Then after being spray-dried
Obtained product is calcined 24 hours for 500 DEG C in Muffle furnace, obtains 19 grams of the spherical mesoporous composite material C1 of target product diplopore；
(2) preparation of propane dehydrogenation catalyst
By 0.080g H2PtCl6·6H2O、0.207g SnCl4·5H2O and 0.185g NaNO3It is dissolved in 100ml deionization
In water, mixture solution is obtained, the spherical mesoporous composite material C1 of diplopore that step (1) obtains is immersed in the mixture solution
In, after being impregnated 5 hours at 25 DEG C, the aqueous solvent in system is boiled off with Rotary Evaporators, obtains solid product, by solid product
It is placed in the drying box that temperature is 120 DEG C, 3 hours dry, being subsequently placed in temperature is to roast 6 hours, obtain in 600 DEG C of Muffle furnaces
To propane dehydrogenation catalyst A, (on the basis of the total weight of propane dehydrogenation catalyst A, the content of Pt is containing for 0.3 weight %, Sn
The content that amount is 0.7 weight %, Na is 0.5 weight %, remaining is carrier).
With XRD, scanning electron microscope, ASAP2020-M+C type adsorption instrument and Malvern laser particle analyzer come to diplopore ball
Shape mesoporous composite material C1 is characterized；
Fig. 1 is the XRD spectra of the spherical mesoporous composite material C1 of diplopore, and abscissa is 2 θ, and ordinate is intensity, is composed by XRD
The low-angle spectral peak occurred is schemed it is found that the XRD spectra of the spherical mesoporous composite material C1 of diplopore has 2D specific to mesoporous material
Hexagonal hole road structure；
Fig. 2 is the stereoscan photograph (SEM) of the spherical mesoporous composite material C1 of diplopore, and as seen from the figure, sample is point
The good sphere material of property is dissipated, average grain diameter is at 30-60 μm；
Fig. 3 is the graph of pore diameter distribution of the spherical mesoporous composite material C1 of diplopore, wherein abscissa is aperture, unit nm, by
Fig. 3 can be seen that the spherical mesoporous composite material C1 of diplopore and be distributed with double-pore structure, and duct is highly uniform；
Fig. 4 is the grain size distribution of the spherical mesoporous composite material C1 of diplopore, and unit is micron, as seen from Figure 4, diplopore
The particle diameter distribution of spherical mesoporous composite material C1 is highly uniform.
Table 1 is the pore structure parameter of the spherical mesoporous composite material C1 of diplopore
Embodiment 2
The embodiment is for illustrating propane dehydrogenation catalyst and preparation method thereof.
(1) preparation of the spherical mesoporous composite material of diplopore
At 100 DEG C, cetyl trimethylammonium bromide and ethyl orthosilicate are added to the ammonia that concentration is 25 weight %
In aqueous solution, deionized water is added, wherein the additional amount of ethyl orthosilicate is 1g, ethyl orthosilicate, cetyl trimethyl
The molar ratio of ammonia and water in ammonium bromide, ammonium hydroxide is 1:0.1:2:120, and is stirred 2 hours at a temperature of 100 DEG C, then will be molten
Liquid is filtered and is washed with distilled water four times, obtains mesoporous material filter cake；
By the waterglass that concentration is 15 weight % and the sulfuric acid solution that concentration is 12 weight %, and by waterglass and sulfuric acid
Weight ratio is uniformly mixed for 5:1, is then stirred to react at 40 DEG C 1.5 hours, and is 98 by obtained reaction product concentration
The sulfuric acid adjustment pH of weight % is 2, and reaction mass is then washed till sodium ions content lower than 0.02 by filtering, distilling water washing
Weight % obtains silica gel filter cake；
(wherein, 20 grams of mesoporous material filter cakes of above-mentioned preparation, 10 grams of silica gel filter cakes are put into togerther in 100mL ball grinder
Ball grinder material is polytetrafluoroethylene (PTFE), and Material quality of grinding balls is agate, and the diameter of abrading-ball is 3mm, and quantity is 1, revolving speed 400r/
Min), ball grinder is closed, temperature is to obtain 30 grams of solid powders ball milling 1 hour at 60 DEG C in ball grinder；By the solid powder
It is dissolved in 51 grams of deionized waters, and at 150 DEG C, is spray-dried in the case where revolving speed is 11000r/min；It then will spray drying
The product obtained afterwards is calcined 24 hours in 500 DEG C of Muffle furnace, obtains 29 grams of the spherical mesoporous composite wood of target product diplopore
Expect C2；
(2) preparation of propane dehydrogenation catalyst
By 0.133g H2PtCl6·6H2O、0.089g SnCl4·5H2O and 0.259g NaNO3It is dissolved in 100ml deionization
In water, mixture solution is obtained, the spherical mesoporous composite material C2 of diplopore that step (1) obtains is immersed in the mixture solution
In, after being impregnated 3 hours at 50 DEG C, the aqueous solvent in system is boiled off with Rotary Evaporators, obtains solid product, by solid product
It is placed in the drying box that temperature is 110 DEG C, 6 hours dry, being subsequently placed in temperature is to roast 7 hours, obtain in 620 DEG C of Muffle furnaces
To propane dehydrogenation catalyst B, (on the basis of the total weight of propane dehydrogenation catalyst B, the content of Pt is containing for 0.5 weight %, Sn
The content that amount is 0.3 weight %, Na is 0.7 weight %, remaining is carrier).
Table 2 is the pore structure parameter of the spherical mesoporous composite material C2 of diplopore
Embodiment 3
(1) preparation of the spherical mesoporous composite material of diplopore
At 50 DEG C, cetyl trimethylammonium bromide and ethyl orthosilicate are added to the ammonium hydroxide that concentration is 25 weight %
In solution, deionized water is added, wherein the additional amount of ethyl orthosilicate is 1g, ethyl orthosilicate, cetyl trimethyl bromine
The molar ratio for changing ammonium, the ammonia in ammonium hydroxide and water is 1:0.5:4:160, and stirring is to dissolving at 50 °C, then by solution
It filters and is washed with distilled water four times, obtain mesoporous material filter cake；
By the waterglass that concentration is 15 weight % and the sulfuric acid solution that concentration is 12 weight %, and by waterglass and sulfuric acid
Weight ratio is uniformly mixed for 4:1, is then stirred to react at 30 DEG C 2 hours, and is 98 weights by obtained reaction product concentration
The sulfuric acid adjustment pH for measuring % is 4, and reaction mass is then washed till sodium ions content lower than 0.02 weight by suction filtration, distillation water washing
% is measured, silica gel filter cake is obtained；
(wherein, 20 grams of mesoporous material filter cakes of above-mentioned preparation, 30 grams of silica gel filter cakes are put into togerther in 100mL ball grinder
Ball grinder material is polytetrafluoroethylene (PTFE), and Material quality of grinding balls is agate, and the diameter of abrading-ball is 3mm, and quantity is 1, revolving speed 400r/
Min), ball grinder is closed, temperature is to obtain 50 grams of solid powders ball milling 1 hour at 60 DEG C in ball grinder；By the solid powder
It is dissolved in 100 grams of deionized waters, and at 250 DEG C, is spray-dried in the case where revolving speed is 13000r/min；It then will spray drying
The product obtained afterwards is calcined 24 hours in 500 DEG C of Muffle furnace, obtains 49 grams of the spherical mesoporous composite wood of target product diplopore
Expect C3；
(2) preparation of propane dehydrogenation catalyst
By 0.107g H2PtCl6·6H2O、0.325g SnCl4·5H2O and 0.111g NaNO3It is dissolved in 100ml deionization
In water, mixture solution is obtained, the spherical mesoporous composite material of diplopore that step (1) obtains is immersed in the mixture solution
In, after being impregnated 5 hours at 30 DEG C, the aqueous solvent in system is boiled off with Rotary Evaporators, obtains solid product, by solid product
It is placed in the drying box that temperature is 150 DEG C, 3 hours dry, being subsequently placed in temperature is to roast 5 hours, obtain in 650 DEG C of Muffle furnaces
To propane dehydrogenation catalyst C, (on the basis of the total weight of propane dehydrogenation catalyst C, the content of Pt is containing for 0.4 weight %, Sn
The content that amount is 1.1 weight %, Na is 0.3 weight %, remaining is carrier).
Table 3 is the pore structure parameter of the spherical mesoporous composite material C3 of diplopore
Comparative example 1
Propane dehydrogenation catalyst is prepared according to the method for embodiment 1, unlike, using what is prepared in CN102389831A
Mesostructured material replaces the spherical mesoporous composite material C1 of diplopore, obtains propane dehydrogenation catalyst D1.
Comparative example 2
Propane dehydrogenation catalyst is prepared according to the method for embodiment 1, unlike, third is prepared according to the method for embodiment 1
Alkane dehydrogenation, unlike, H2PtCl6·6H2O、SnCl4·5H2O and NaNO3Dosage make the propane being prepared
In dehydrogenation D2, on the basis of the total weight of the propane dehydrogenation catalyst, the content of Pt is containing for 0.1 weight %, Sn
The content that amount is 1.5 weight %, Na is 0.2 weight %, remaining is carrier.
Comparative example 3
Propane dehydrogenation catalyst is prepared according to the method for embodiment 1, unlike, in the step for preparing propane dehydrogenation catalyst
In rapid, co-impregnation is replaced using step impregnation, specifically: first by the spherical mesoporous composite material C1 of diplopore first in H2PtCl6In solution
Dipping, then dry and roasting；Again in SnCl4It is impregnated in solution, then dry and roasting；Finally in NaNO3It is impregnated in solution,
Then dry and roasting, obtains propane dehydrogenation catalyst D3.
EXPERIMENTAL EXAMPLE 1
The present embodiment is used for the method for illustrating to prepare propylene using propane dehydrogenation catalyst of the invention
0.5g propane dehydrogenation catalyst A is fitted into fixed-bed quartz reactor, control reaction temperature is 610 DEG C, reaction
Pressure is 0.1MPa, and propane: the molar ratio of hydrogen is 1:1, and reaction time 50h, propane mass space velocity is 3h-1.Propane conversion
Rate and Propylene Selectivity are as shown in table 4.
EXPERIMENTAL EXAMPLE 2-3
Preparing propylene by dehydrogenating propane is carried out according to the method for EXPERIMENTAL EXAMPLE 1, unlike, dehydrogenating propane catalysis is respectively adopted
Agent B and propane dehydrogenation catalyst C replaces propane dehydrogenation catalyst A.Conversion of propane and Propylene Selectivity are as shown in table 4.
Experimental comparison's example 1-3
Preparing propylene by dehydrogenating propane is carried out according to the method for EXPERIMENTAL EXAMPLE 1, unlike, dehydrogenating propane catalysis is respectively adopted
Agent D1, propane dehydrogenation catalyst D2 and propane dehydrogenation catalyst D3 replace propane dehydrogenation catalyst A.Conversion of propane and propylene choosing
Selecting property is as shown in table 4.
Table 4
| Dehydrogenation | Conversion of propane | Propylene Selectivity | |
| EXPERIMENTAL EXAMPLE 1 | A | 32% | 99.4% |
| EXPERIMENTAL EXAMPLE 2 | B | 31.7% | 99.3% |
| EXPERIMENTAL EXAMPLE 3 | C | 32.4% | 99.6% |
| Experimental comparison's example 1 | D1 | 10% | 82% |
| Experimental comparison's example 2 | D2 | 13% | 77% |
| Experimental comparison's example 3 | D3 | 16% | 85% |
From table 4, it can be seen that using the propane of the invention prepared using the spherical mesoporous composite material of diplopore as carrier de-
Hydrogen catalyst for preparing propylene by dehydrogenating propane react when, reaction 50 hours after, still available higher conversion of propane and
Propylene Selectivity, illustrating propane dehydrogenation catalyst of the invention not only has preferable catalytic performance, but also stability is good.
The preferred embodiment of the present invention has been described above in detail, still, during present invention is not limited to the embodiments described above
Detail within the scope of the technical concept of the present invention can be with various simple variants of the technical solution of the present invention are made, this
A little simple variants all belong to the scope of protection of the present invention.
It is further to note that specific technical features described in the above specific embodiments, in not lance
In the case where shield, can be combined in any appropriate way, in order to avoid unnecessary repetition, the present invention to it is various can
No further explanation will be given for the combination of energy.
In addition, various embodiments of the present invention can be combined randomly, as long as it is without prejudice to originally
The thought of invention, it should also be regarded as the disclosure of the present invention.
Claims (15)
1. a kind of propane dehydrogenation catalyst, which is characterized in that the propane dehydrogenation catalyst includes carrier and is supported on described
Main active component Pt, metal promoter Sn and metal promoter Na on carrier, wherein the carrier is that diplopore is spherical mesoporous compound
Material, the average particle diameter of the spherical mesoporous composite material of diplopore are 30-60 microns, and specific surface area is 200-650 squares
Rice/gram, pore volume is 0.5-1.5 mls/g, and pore-size distribution is bimodal distribution, and the bimodal corresponding most probable pore size divides
It Wei not be 1.5-15 nanometers and 16-50 nanometers.
2. propane dehydrogenation catalyst according to claim 1, wherein the dehydrogenating propane relative to 100 parts by weight is urged
Agent, the content of the carrier are 97.5-99.3 weight %, and the content of the main active component Pt is 0.2-0.5 weight %,
The content of metal promoter Sn is 0.2-1.2 weight %, and the content of metal promoter Na is 0.3-0.8 weight %.
3. a kind of preparation method of propane dehydrogenation catalyst, which is characterized in that the preparation method includes: to contain carrier impregnation
In the mixed solution for having Pt salt, Sn salt and Na salt, it is dried and roasts after the solution after dipping is then removed solvent,
In, the carrier is the spherical mesoporous composite material of diplopore, and the average particle diameter of the spherical mesoporous composite material of diplopore is 30-
60 microns, specific surface area is 200-650 meters squared per gram, and pore volume is 0.5-1.5 mls/g, and pore-size distribution is bimodal distribution,
And the bimodal corresponding most probable pore size is respectively 1.5-15 nanometers and 16-50 nanometers.
4. preparation method according to claim 3, wherein the carrier, Pt salt, Sn salt and Na salt dosage to prepare
In obtained propane dehydrogenation catalyst, on the basis of the total weight of the propane dehydrogenation catalyst, the content of the carrier is
Content of 97.5-99.3 weight %, the Pt salt in terms of Pt element is that content of 0.2-0.5 weight %, the Sn salt in terms of Sn element is
Content of 0.2-1.2 weight %, the Na salt in terms of Na element is 0.3-0.8 weight %.
5. the preparation method according to claim 4, wherein the condition of the dipping includes: that temperature is 25-50 DEG C, the time
It is 2-6 hours.
6. preparation method according to claim 3, wherein the preparation method packet of the spherical mesoporous composite material of diplopore
It includes:
(1) cetyl trimethylammonium bromide, ethyl orthosilicate are contacted with ammonium hydroxide, and the product after contact are filtered,
Obtain mesoporous material filter cake；
(2) waterglass is contacted with inorganic acid, and the product obtained after contact is filtered, obtain silica gel filter cake；
(3) the mesoporous material filter cake is uniformly mixed to simultaneously ball milling with silica gel filter cake, and the solid powder obtained after ball milling is used
It is spray-dried and is calcined after water slurrying.
7. preparation method according to claim 6, wherein in step (1), the ethyl orthosilicate, cetyl three
The molar ratio of ammonia and water in methyl bromide ammonium, ammonium hydroxide is 1:0.1-1:0.1-5:100-200.
8. preparation method according to claim 6, wherein in step (1), cetyl trimethylammonium bromide, positive silicon
The condition that acetoacetic ester is contacted with ammonium hydroxide includes: that temperature is 25-100 DEG C, and the time is 1-10 hours.
9. preparation method according to claim 6, wherein in step (2), item that the waterglass is contacted with inorganic acid
Part includes: that temperature is 10-60 DEG C, and the time is 1-5 hours, pH value 2-4.
10. preparation method according to claim 9, wherein the inorganic acid be one of sulfuric acid, nitric acid and hydrochloric acid or
It is a variety of.
11. preparation method according to claim 6, wherein in step (3), the dosage and silica gel of mesoporous material filter cake
The weight ratio of the dosage of filter cake is 1:0.1-2.
12. the propane dehydrogenation catalyst that preparation method described in any one of claim 3-11 is prepared.
13. a kind of method of preparing propylene by dehydrogenating propane, which comprises in the presence of catalyst and hydrogen, by propane into
Row dehydrogenation reaction, which is characterized in that the catalyst is dehydrogenating propane catalysis described in any one of claim 1,2 and 12
Agent.
14. according to the method for claim 13, wherein the molar ratio of the dosage of the dosage and hydrogen of propane is 0.5-1.5:
1。
15. according to the method for claim 13, wherein the condition of the dehydrogenation reaction includes: that reaction temperature is 600-650
DEG C, reaction pressure 0.05-0.2MPa, reaction time 40-60h, propane mass space velocity are 2-5h-1。
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| CN109622023A (en) * | 2018-12-05 | 2019-04-16 | 大连理工大学 | A kind of preparation method and application for dehydrogenating propane aromatization catalyst |
| CN112221533A (en) * | 2019-06-30 | 2021-01-15 | 中国石油化工股份有限公司 | Mg and/or Ti component modified hexagonal mesoporous material and propane dehydrogenation catalyst, and preparation methods and applications thereof |
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| US3396205A (en) * | 1964-05-20 | 1968-08-06 | Polymer Corp | Dehydrogenation catalysts containing bismuth compounds and calcium nickel phosphate |
| CN1013361B (en) * | 1987-03-13 | 1991-07-31 | 中国科学院大连化学物理研究所 | Catalyst containing pt, sn, li, s for dehydrogenation of saturated hydrocarbon |
| CN1032678C (en) * | 1992-12-21 | 1996-09-04 | 中国石油化工总公司 | Catalyst for dehydrogen of saturated hydrocarbon |
| DE19937107A1 (en) * | 1999-08-06 | 2001-02-08 | Basf Ag | Catalyst with bimodal pore radius distribution |
| US6417135B1 (en) * | 1999-08-27 | 2002-07-09 | Huntsman Petrochemical Corporation | Advances in dehydrogenation catalysis |
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