CN110180537A - One kind is for dehydrogenating low-carbon alkane metal alloy catalyst and its preparation method and application - Google Patents
One kind is for dehydrogenating low-carbon alkane metal alloy catalyst and its preparation method and application Download PDFInfo
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- CN110180537A CN110180537A CN201910507250.7A CN201910507250A CN110180537A CN 110180537 A CN110180537 A CN 110180537A CN 201910507250 A CN201910507250 A CN 201910507250A CN 110180537 A CN110180537 A CN 110180537A
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- 239000003054 catalyst Substances 0.000 title claims abstract description 72
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 36
- 238000002360 preparation method Methods 0.000 title claims abstract description 10
- 229910001092 metal group alloy Inorganic materials 0.000 title claims description 16
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Substances [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims abstract description 16
- 150000001335 aliphatic alkanes Chemical class 0.000 claims abstract description 15
- 229910052733 gallium Inorganic materials 0.000 claims abstract description 4
- 229910052732 germanium Inorganic materials 0.000 claims abstract description 4
- 229910052718 tin Inorganic materials 0.000 claims abstract description 4
- 229910052741 iridium Inorganic materials 0.000 claims abstract description 3
- 229910052763 palladium Inorganic materials 0.000 claims abstract description 3
- 229910052697 platinum Inorganic materials 0.000 claims abstract description 3
- 239000010970 precious metal Substances 0.000 claims abstract description 3
- 229910052703 rhodium Inorganic materials 0.000 claims abstract description 3
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 68
- 238000006243 chemical reaction Methods 0.000 claims description 39
- 239000001294 propane Substances 0.000 claims description 34
- 238000001035 drying Methods 0.000 claims description 32
- 239000004215 Carbon black (E152) Substances 0.000 claims description 14
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 9
- YRAJNWYBUCUFBD-UHFFFAOYSA-N 2,2,6,6-tetramethylheptane-3,5-dione Chemical compound CC(C)(C)C(=O)CC(=O)C(C)(C)C YRAJNWYBUCUFBD-UHFFFAOYSA-N 0.000 claims description 8
- 238000006356 dehydrogenation reaction Methods 0.000 claims description 7
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N titanium dioxide Inorganic materials O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 6
- 238000000034 method Methods 0.000 claims description 5
- 229910026161 MgAl2O4 Inorganic materials 0.000 claims description 4
- 229910052681 coesite Inorganic materials 0.000 claims description 4
- 229910052906 cristobalite Inorganic materials 0.000 claims description 4
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 claims description 4
- 239000000377 silicon dioxide Substances 0.000 claims description 4
- 229910052596 spinel Inorganic materials 0.000 claims description 4
- 229910052682 stishovite Inorganic materials 0.000 claims description 4
- KSBAEPSJVUENNK-UHFFFAOYSA-L tin(ii) 2-ethylhexanoate Chemical compound [Sn+2].CCCCC(CC)C([O-])=O.CCCCC(CC)C([O-])=O KSBAEPSJVUENNK-UHFFFAOYSA-L 0.000 claims description 4
- 229910052905 tridymite Inorganic materials 0.000 claims description 4
- 229910003609 H2PtCl4 Inorganic materials 0.000 claims description 3
- 229910020427 K2PtCl4 Inorganic materials 0.000 claims description 3
- YRKCREAYFQTBPV-UHFFFAOYSA-N acetylacetone Chemical compound CC(=O)CC(C)=O YRKCREAYFQTBPV-UHFFFAOYSA-N 0.000 claims description 3
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 3
- 229910052593 corundum Inorganic materials 0.000 claims description 3
- JGFBRKRYDCGYKD-UHFFFAOYSA-N dibutyl(oxo)tin Chemical compound CCCC[Sn](=O)CCCC JGFBRKRYDCGYKD-UHFFFAOYSA-N 0.000 claims description 3
- WNVQCJNZEDLILP-UHFFFAOYSA-N dimethyl(oxo)tin Chemical compound C[Sn](C)=O WNVQCJNZEDLILP-UHFFFAOYSA-N 0.000 claims description 3
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 claims description 3
- 239000003863 metallic catalyst Substances 0.000 claims description 3
- 229910001845 yogo sapphire Inorganic materials 0.000 claims description 3
- 229910021638 Iridium(III) chloride Inorganic materials 0.000 claims description 2
- 229910002666 PdCl2 Inorganic materials 0.000 claims description 2
- 229910019029 PtCl4 Inorganic materials 0.000 claims description 2
- 229910021604 Rhodium(III) chloride Inorganic materials 0.000 claims description 2
- 150000001721 carbon Chemical group 0.000 claims description 2
- LQRUPWUPINJLMU-UHFFFAOYSA-N dioctyl(oxo)tin Chemical compound CCCCCCCC[Sn](=O)CCCCCCCC LQRUPWUPINJLMU-UHFFFAOYSA-N 0.000 claims description 2
- 229930195733 hydrocarbon Natural products 0.000 claims description 2
- 150000002430 hydrocarbons Chemical class 0.000 claims description 2
- 239000001282 iso-butane Substances 0.000 claims description 2
- 235000013847 iso-butane Nutrition 0.000 claims description 2
- PIBWKRNGBLPSSY-UHFFFAOYSA-L palladium(II) chloride Chemical compound Cl[Pd]Cl PIBWKRNGBLPSSY-UHFFFAOYSA-L 0.000 claims description 2
- 229910002093 potassium tetrachloropalladate(II) Inorganic materials 0.000 claims description 2
- SONJTKJMTWTJCT-UHFFFAOYSA-K rhodium(iii) chloride Chemical compound [Cl-].[Cl-].[Cl-].[Rh+3] SONJTKJMTWTJCT-UHFFFAOYSA-K 0.000 claims description 2
- AFCAKJKUYFLYFK-UHFFFAOYSA-N tetrabutyltin Chemical compound CCCC[Sn](CCCC)(CCCC)CCCC AFCAKJKUYFLYFK-UHFFFAOYSA-N 0.000 claims description 2
- FBEIPJNQGITEBL-UHFFFAOYSA-J tetrachloroplatinum Chemical compound Cl[Pt](Cl)(Cl)Cl FBEIPJNQGITEBL-UHFFFAOYSA-J 0.000 claims description 2
- CRHIAMBJMSSNNM-UHFFFAOYSA-N tetraphenylstannane Chemical compound C1=CC=CC=C1[Sn](C=1C=CC=CC=1)(C=1C=CC=CC=1)C1=CC=CC=C1 CRHIAMBJMSSNNM-UHFFFAOYSA-N 0.000 claims description 2
- DANYXEHCMQHDNX-UHFFFAOYSA-K trichloroiridium Chemical compound Cl[Ir](Cl)Cl DANYXEHCMQHDNX-UHFFFAOYSA-K 0.000 claims description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims 1
- 239000001257 hydrogen Substances 0.000 claims 1
- 229910052739 hydrogen Inorganic materials 0.000 claims 1
- 239000006185 dispersion Substances 0.000 abstract description 5
- 229910045601 alloy Inorganic materials 0.000 abstract description 3
- 239000000956 alloy Substances 0.000 abstract description 3
- 230000003197 catalytic effect Effects 0.000 abstract description 3
- 238000005245 sintering Methods 0.000 abstract 1
- 238000007598 dipping method Methods 0.000 description 24
- 150000001875 compounds Chemical class 0.000 description 22
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 13
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 13
- 239000000376 reactant Substances 0.000 description 11
- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 8
- 229910052751 metal Inorganic materials 0.000 description 7
- 239000002184 metal Substances 0.000 description 7
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 7
- 150000001336 alkenes Chemical class 0.000 description 6
- 239000007789 gas Substances 0.000 description 5
- 239000003795 chemical substances by application Substances 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000011651 chromium Substances 0.000 description 3
- 239000000395 magnesium oxide Substances 0.000 description 3
- WWZKQHOCKIZLMA-UHFFFAOYSA-N octanoic acid Chemical compound CCCCCCCC(O)=O WWZKQHOCKIZLMA-UHFFFAOYSA-N 0.000 description 3
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 229910052804 chromium Inorganic materials 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 239000004575 stone Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- TXUICONDJPYNPY-UHFFFAOYSA-N (1,10,13-trimethyl-3-oxo-4,5,6,7,8,9,11,12,14,15,16,17-dodecahydrocyclopenta[a]phenanthren-17-yl) heptanoate Chemical compound C1CC2CC(=O)C=C(C)C2(C)C2C1C1CCC(OC(=O)CCCCCC)C1(C)CC2 TXUICONDJPYNPY-UHFFFAOYSA-N 0.000 description 1
- ZVYYAYJIGYODSD-LNTINUHCSA-K (z)-4-bis[[(z)-4-oxopent-2-en-2-yl]oxy]gallanyloxypent-3-en-2-one Chemical compound [Ga+3].C\C([O-])=C\C(C)=O.C\C([O-])=C\C(C)=O.C\C([O-])=C\C(C)=O ZVYYAYJIGYODSD-LNTINUHCSA-K 0.000 description 1
- -1 Carbon alkane Chemical class 0.000 description 1
- 240000007594 Oryza sativa Species 0.000 description 1
- 235000007164 Oryza sativa Nutrition 0.000 description 1
- 101150003085 Pdcl gene Proteins 0.000 description 1
- 229910002846 Pt–Sn Inorganic materials 0.000 description 1
- 229910008195 SnAl2O4 Inorganic materials 0.000 description 1
- ATJFFYVFTNAWJD-UHFFFAOYSA-N Tin Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 0.000 description 1
- 229910021626 Tin(II) chloride Inorganic materials 0.000 description 1
- 239000002671 adjuvant Substances 0.000 description 1
- OBETXYAYXDNJHR-UHFFFAOYSA-N alpha-ethylcaproic acid Natural products CCCCC(CC)C(O)=O OBETXYAYXDNJHR-UHFFFAOYSA-N 0.000 description 1
- 239000012752 auxiliary agent Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 238000001802 infusion Methods 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 150000002484 inorganic compounds Chemical class 0.000 description 1
- 229910010272 inorganic material Inorganic materials 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 235000009566 rice Nutrition 0.000 description 1
- 239000001119 stannous chloride Substances 0.000 description 1
- 235000011150 stannous chloride Nutrition 0.000 description 1
- 239000000126 substance 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
- B01J23/38—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
-
- 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
- B01J23/624—Platinum group metals with gallium, indium, thallium, germanium, tin or lead with germanium, tin or lead with germanium
-
- 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
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/0201—Impregnation
-
- 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
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/08—Heat treatment
- B01J37/082—Decomposition and pyrolysis
-
- 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
- C07C5/3335—Catalytic processes with metals
- C07C5/3337—Catalytic processes with metals of the platinum group
-
- 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
Abstract
The invention discloses one kind for dehydrating alkanes alloy catalyst and its preparation method and application.The catalyst includes one of tri- kinds of components of A, B and C, component A Pt, Pd, Rh and Ir precious metal element predecessor, accounts for 0.1~5 wt% of total catalyst weight；B component is one of Sn, Ge, Ga element predecessor, accounts for 0.1~5 wt% of total catalyst weight；Component C is carrier, accounts for 90~99.8 wt% of total catalyst weight.The present invention uses predecessor of the metallo-organic compound as B component, this predecessor is very easy to evenly dispersed in carrier surface.Hereafter active component A, finally prepd alloy catalyst are re-introduced into.The catalyst that must be prepared have partial size is small, dispersion degree is high, anti-sintering property is strong, catalytic activity is high, have good dehydrogenating low-carbon alkane performance.
Description
Technical field
The present invention relates to industrial catalyst preparation fields, and in particular to one kind for dehydrogenating low-carbon alkane metallic catalyst and
Preparation method and application.
Background technique
Low-carbon alkanes (C3-C4) catalytic dehydrogenation be converted into low-carbon alkene be not only realize natural gas, refinery gas, oil field association
One important channel of the optimizing network resource utilizations such as gas and shale gas, but also can be relieved low-carbon alkene especially propylene supply falls short of demand
Contradiction.Low-carbon alkanes are used as fuel mostly in Natural Gas In China, casing-head gas and refinery gas, and are underutilized, and in
State's low-carbon alkene especially propylene feedstocks wretched insufficiency.If low-carbon alkene effectively can be directly translated into low-carbon alkanes, not only
It solves the problems, such as the source deficiency of low-carbon alkene raw material, and also improves the utility value of low-carbon alkanes.Therefore, exploitation is by low
Carbon alkane preparing low-carbon olefins process utilizes C to reasonable3-C4It alkane and opens up low-carbon alkene new sources and is of great significance.
The catalyst of dehydrogenating low-carbon alkane reaction for preparing light olefins is mainly platinum group catalyst and chromium-based catalysts.Although
Chromium-based catalysts it is cheap and not high to ingredient requirement, but since Cr is heavy metal, pollute the environment, thus its
Using being restricted.Platinum group catalyst is the mainstream catalyst of current dehydrogenating propane, although its dehydrogenation activity is relatively good, selection
Property is higher, but its metal component dispersibility is poor, and partial size is larger, and the easy high temperature coking deactivation of catalyst, so steady to its
Qualitative and active improve is still the hot spot studied at present.
The preparation of Pt base catalyst is generally synthesized using tradition dipping, and it is metal promoter that inorganic compound is used in synthesis
The predecessor of component, such as stannous chloride introduce Ga, Sn and Ge auxiliary agent with this to help divided active component Pt.But inorganic chemical
Object and carrier binding ability are limited, and active component is caused to be unevenly distributed on carrier, and active phase partial size is larger.And organic compound
Object, such as stannous octoate, it is stronger with carrier binding force, it is distributed on carrier more uniformly, and have strong phase interaction with Pt metal
Firmly promote the dispersion of Pt metal.
In consideration of it, the present invention provides a kind of preparation method of metal alloy catalyst, which has been firstly introduced into machine aided
Agent component after being evenly distributed on carrier, is re-introduced into active component, and the high dispersion metal so as to form composition, uniform particle sizes is received
Rice cluster catalyst is broken through the disadvantages of conventional metallic alloys catalyst the Nomenclature Composition and Structure of Complexes is inhomogenous, partial size is big, bad dispersibility, is realized
Metal alloy catalyst synthesis-structure-performance Effective Regulation.
Summary of the invention
The purpose of the present invention is in view of the shortcomings of the prior art, providing a kind of for dehydrogenating low-carbon alkane metal alloy catalyst
And its preparation method and application.The made catalyst of the present invention is alloy catalyst, and partial size is small, dispersion degree is high, anti-agglutinatting property
Energy is strong, catalytic activity is good.When for dehydrogenating low-carbon alkane reaction, it is active it is high, stability is good, low-carbon alkanes high conversion rate,
The advantages that olefine selective is high, inactivation rate is low and renewable.
To achieve the above object, the present invention adopts the following technical scheme:
One kind being used for dehydrogenating low-carbon alkane metal alloy catalyst, and the catalyst includes tri- kinds of components of A, B and C, and component A is
Any one in Pt, Pd, Rh and Ir precious metal element predecessor, accounts for 0.1~5wt% of total catalyst weight；B component be Sn,
Any one in Ge and Ga element predecessor, accounts for 0.1~5 wt% of total catalyst weight；Component C is carrier, accounts for catalyst
90~99.8 wt% of total weight.
In the component A, the predecessor of Pt includes PtCl4·5H2O、H2PtCl4、K2PtCl4、(NH4)2PtCl6Or Pt
(COD)Cl2Middle one kind；
The predecessor of Pd includes PdCl2·2H2O、K2PdCl4、Pd(NH3)4Cl2Or Pd (COD) Cl2One of；
The predecessor of Rh includes RhCl3·3H2O、K3RhCl6、(NH4)3RhCl6、 [Rh(COD)Cl]2、[(COD)RhOMe)]2Or
[(COD)RhOSi(OtBu)3]2One of；
The predecessor of Ir includes IrCl3·3H2O、K2IrCl6、(NH4)2IrCl6、[Ir(COD)Cl]2、[(COD)IrOMe]2Or
[(COD)IrOSi(OtBu)3]2One of.
In the B component, the predecessor of Sn includes Dibutyltin oxide, stannous octoate, dimethyl tin oxide, oxidation two
One of tin octylate, tetraphenyltin, tetrabutyltin；
The predecessor of Ge includes Ge (Ph)4、Ge(Me)4Or Ge (ETH)4One of；
The predecessor of Ga includes Ga (TMHD)3Or Ga (ACAC)3One of.
The carrier is oxide, including SiO2、Al2O3、MgO、TiO2Or MgAl2O4In any one.
A method of it prepares for dehydrogenating low-carbon alkane metallic catalyst, specifically includes the following steps:
(1) oxide is weighed, as carrier, impregnates B component, then through drying, roasting；
(2) component A is impregnated in step (1) above the carrier containing B component, then the lower alkanes are made in drying, roasting
Hydrocarbon dehydrogenation metal alloy catalyst.
The dip time is the h of 1 h~24；The drying is in 60 DEG C~150 DEG C drying h of 1 h~12, roasting
Burning is that the h of 2 h~8 is roasted at 400 DEG C~650 DEG C.The catalyst is used for the dehydrogenation reaction of low-carbon alkanes, the low-carbon
Alkane includes the alkane of 2-4 carbon atom, and 400 DEG C~600 DEG C of reaction temperature, mass space velocity is 0.5~20 h-1。
The low-carbon alkanes are propane or iso-butane, and dehydrogenation reaction carries out in fixed bed reactors.
In entire reaction process, dehydrating alkanes mainly generate corresponding alkene, and crack, the pair of isomerization and polymerization
Product is all considerably less.Thus, the selectivity that dehydrating alkanes generate corresponding alkene is very high, the highest in the case where condition is suitable for
It can reach 99%, or even generate corresponding alkene almost close to 100%.
The beneficial effects of the present invention are: catalyst prepared by the present invention is firstly introduced into organic metal adjuvant component, with this
Replace traditional inorganic assistant component, after being evenly distributed on carrier, be re-introduced into active component, so as to form composition, uniform particle sizes
High dispersion metal nanocluster catalyst, it is uneven to break through traditional infusion process preparation legal person's metal alloy catalyst the Nomenclature Composition and Structure of Complexes
One, the disadvantages of partial size is big, bad dispersibility, realizes metal alloy catalyst synthesis-structure-performance Effective Regulation；Exploitation is provided
There is the catalyst of high combination property, the selectivity that dehydrating alkanes generate corresponding alkene is high, conversion per pass is high, and catalyst loses
Living, slow, regenerability is good.
Detailed description of the invention
Fig. 1 is the Rh-Sn/Al of synthesis2O3The STEM of catalyst schemes.
Specific embodiment
For a better understanding of the technical solution of the present invention, combined with specific embodiments below and attached drawing is further details of
Than statement, but it is not intended to limit protection scope of the present invention.
Embodiment 1
Weigh 5.00 g aluminum oxide (Al2O3) load 0.037 g Sn compound (stannous octoate).Normal temperature dipping octanoic acid
In 120 DEG C of drying 8 h, 500 DEG C of 4 h of roasting after 6 h of stannous solution.By carrier loaded 0.061 g of load active component Sn
Compound (the PtCl of Pt4·5H2O), Pt-Sn/ is made in 120 DEG C of drying 12 h, 550 DEG C of 4 h of roasting after 6 h of normal temperature dipping
Al2O3Catalyst.In the fixed-bed tube reactor of the catalyst prepared in being filled with 1 g embodiment 1, reactant is propane,
Reaction temperature is 550 DEG C, and reaction pressure is normal pressure, 8 h of propane weight (hourly) space velocity (WHSV)-1, under conditions of hydrogen-hydrocarbon ratio is 1, conversion of propane
38%, Propylene Selectivity 99.3%.
Embodiment 2
Weigh 5.00 g silica (SiO2) load 0.042 g Ge compound (Ge (Ph)4).Normal temperature dipping Ge (Ph)4It is molten
In 120 DEG C of drying 8 h, 500 DEG C of 4 h of roasting after 6 h of liquid.By the change of the carrier loaded 0.061 g Pt of load active component Ge
Close object (H2PtCl4), in 120 DEG C of drying 12 h, 520 DEG C of 4 h of roasting after 6 h of normal temperature dipping, Pt-Ge/SiO is made2Catalysis
Agent.In the fixed-bed tube reactor of the catalyst prepared in being filled with 1 g embodiment 2, reactant is propane, reaction temperature
It is 550 DEG C, reaction pressure is normal pressure, 5 h of propane weight (hourly) space velocity (WHSV)-1, under conditions of hydrogen-hydrocarbon ratio is 1, conversion of propane 37.5%,
Propylene Selectivity 98%.
Embodiment 3
Weigh the compound (Ga (TMHD) that 3.00 g magnesia (MgO) load 0.022 g Ga3).Normal temperature dipping Ga (TMHD)3
In 120 DEG C of drying 8 h, 500 DEG C of 4 h of roasting after 6 h of solution.By the carrier loaded 0.061 g Pt's of load active component Ga
Compound (K2PtCl4), in 120 DEG C of drying 12 h, 540 DEG C of 4 h of roasting after 6 h of normal temperature dipping, Pt-Ga/MgO catalysis is made
Agent.In the fixed-bed tube reactor of the catalyst prepared in being filled with 1 g embodiment 3, reactant is propane, reaction temperature
It is 550 DEG C, reaction pressure is normal pressure, 6 h of propane weight (hourly) space velocity (WHSV)-1, under conditions of hydrogen-hydrocarbon ratio is 1, conversion of propane 37%, third
Alkene selectivity 99%.
Embodiment 4
Weigh 6.00 g titanium dioxide (TiO2) load 0.037 g Sn compound (Dibutyltin oxide).Normal temperature dipping
HSnBu3In 120 DEG C of drying 8 h, 500 DEG C of 4 h of roasting after 6 h of solution.By carrier loaded the 0.048 of load active component Sn
Compound (the PdCl of g Pd2·2H2O), Pd- is made in 120 DEG C of drying 12 h, 550 DEG C of 4 h of roasting after 6 h of normal temperature dipping
Sn/TiO2Catalyst.In the fixed-bed tube reactor of the catalyst prepared in being filled with 1 g embodiment 4, reactant third
Alkane, reaction temperature are 550 DEG C, and reaction pressure is normal pressure, 5 h of propane weight (hourly) space velocity (WHSV)-1, under conditions of hydrogen-hydrocarbon ratio is 1, propane turns
Rate 35%, Propylene Selectivity 97.5%.
Embodiment 5
Weigh 5.00 g magnaliums crystallization stone (MgAl2O4) load 0.042 g Ge compound (Ge (Me)4).Normal temperature dipping Ge
(Me)4In 120 DEG C of drying 8 h, 500 DEG C of 4 h of roasting after 6 h of solution.By carrier loaded 0.048 g of load active component Ge
Compound (the K of Pd2PdCl4), in 120 DEG C of drying 12 h, 550 DEG C of 4 h of roasting after 6 h of normal temperature dipping, Pd-Ge/ is made
MgAl2O4Catalyst.In the fixed-bed tube reactor of the catalyst prepared in being filled with 1 g embodiment 6, reactant third
Alkane, reaction temperature are 550 DEG C, and reaction pressure is normal pressure, 3 h of propane weight (hourly) space velocity (WHSV)-1, under conditions of hydrogen-hydrocarbon ratio is 1, propane turns
Rate 36.5%, Propylene Selectivity 93%.
Embodiment 6
Weigh 5.00 g aluminum oxide (Al2O3) load 0.022 g Ga compound (Ga (ACAC)3).Normal temperature dipping Ga
(ACAC)3In 120 DEG C of drying 8 h, 500 DEG C of 4 h of roasting after 6 h of solution.By carrier loaded the 0.048 of load active component Ga
Compound (Pd (the NH of g Pd3)4Cl2), in 120 DEG C of drying 12 h, 500 DEG C of 4 h of roasting after 6 h of normal temperature dipping, Pd- is made
Ga/Al2O3Catalyst.In the fixed-bed tube reactor of the catalyst prepared in being filled with 1 g embodiment 5, reactant third
Alkane, reaction temperature are 550 DEG C, and reaction pressure is normal pressure, 4 h of propane weight (hourly) space velocity (WHSV)-1, under conditions of hydrogen-hydrocarbon ratio is 1, propane turns
Rate 37%, Propylene Selectivity 96.5%.
Embodiment 7
Weigh 5.00 g silica (SiO2) load 0.037 g Sn compound (dimethyl tin oxide).Normal temperature dipping Sn
(HAC)2In 120 DEG C of drying 8 h, 500 DEG C of 4 h of roasting after 6 h of solution.By carrier loaded the 0.058 of load active component Sn
Compound (the RhCl of g Rh3·3H2O), Rh- is made in 120 DEG C of drying 12 h, 520 DEG C of 4 h of roasting after 6 h of normal temperature dipping
Sn/SiO2Catalyst.In the fixed-bed tube reactor of the catalyst prepared in being filled with 1 g embodiment 7, reactant third
Alkane, reaction temperature are 550 DEG C, and reaction pressure is normal pressure, 3 h of propane weight (hourly) space velocity (WHSV)-1, under conditions of hydrogen-hydrocarbon ratio is 1, propane turns
Rate 39%, Propylene Selectivity 95.8%.
Embodiment 8
Weigh the compound (Ge (ETH) that 3.00 g magnesia (MgO) load 0.042 g Ge4).Normal temperature dipping Ge (ETH)4It is molten
In 120 DEG C of drying 8 h, 500 DEG C of 4 h of roasting after 6 h of liquid.By the change of the carrier loaded 0.058 g Rh of load active component Ge
Close object (K3RhCl6), in 120 DEG C of drying 12 h, 540 DEG C of 4 h of roasting after 6 h of normal temperature dipping, Rh-Ge/MgO catalyst is made.
In the fixed-bed tube reactor of the catalyst prepared in being filled with 1 g embodiment 8, reactant is propane, and reaction temperature is
550 DEG C, reaction pressure is normal pressure, 6 h of propane weight (hourly) space velocity (WHSV)-1, under conditions of hydrogen-hydrocarbon ratio is 1, conversion of propane 33%, propylene
Selectivity 96.5%.
Embodiment 9
Weigh 10.00 g titanium dioxide (TiO2) load 0.022 g Ga compound (Ga (TMHD)3).Normal temperature dipping Ga
(TMHD)3In 120 DEG C of drying 8 h, 500 DEG C of 4 h of roasting after 6 h of solution.By carrier loaded the 0.058 of load active component Ga
Compound (the NH of g Rh4)3RhCl6, in 120 DEG C of drying 12 h, 550 DEG C of 4 h of roasting after 6 h of normal temperature dipping, Rh-Ga/ is made
TiO2Catalyst.In the fixed-bed tube reactor of the catalyst prepared in being filled with 1 g embodiment 9, reactant is propane,
Reaction temperature is 550 DEG C, and reaction pressure is normal pressure, 4 h of propane weight (hourly) space velocity (WHSV)-1, under conditions of hydrogen-hydrocarbon ratio is 1, conversion of propane
31.5%, Propylene Selectivity 96.5%.
Embodiment 10
Weigh 5.00 g magnaliums crystallization stone (MgAl2O4) load 0.037 g Sn compound (di-n-octyltin oxide).Room temperature leaching
Stain HSnPh3In 120 DEG C of drying 8 h, 500 DEG C of 4 h of roasting after 6 h of solution.By the carrier loaded of load active component Sn
Compound (the IrCl of 0.048 g Ir3·3H2O), in 120 DEG C of drying 12 h, 550 DEG C of 4 h of roasting, system after 6 h of normal temperature dipping
Obtain Ir-Sn/MgAl2O4Catalyst.In the fixed-bed tube reactor of the catalyst prepared in being filled with 1 g embodiment 10, instead
Answering object is propane, and reaction temperature is 550 DEG C, and reaction pressure is normal pressure, 4 h of propane weight (hourly) space velocity (WHSV)-1, hydrogen-hydrocarbon ratio be 1 condition
Under, conversion of propane 39%, Propylene Selectivity 97.8%.
Embodiment 11
Weigh 5.00 g aluminum oxide (Al2O3) load 0.042 g Ge compound (Ge (Ph)4).Normal temperature dipping Ge (Ph)4
In 120 DEG C of drying 8 h, 500 DEG C of 4 h of roasting after 6 h of solution.By the carrier loaded 0.048 g Ir's of load active component Ge
Compound (K2IrCl6), in 120 DEG C of drying 12 h, 500 DEG C of 4 h of roasting after 6 h of normal temperature dipping, Ir-Ge/Al is made2O3It urges
Agent.In the fixed-bed tube reactor of the catalyst prepared in being filled with 1 g embodiment 11, reactant is propane, reaction
Temperature is 550 DEG C, and reaction pressure is normal pressure, 4 h of propane weight (hourly) space velocity (WHSV)-1, under conditions of hydrogen-hydrocarbon ratio is 1, conversion of propane
33.5%, Propylene Selectivity 96.5%.
Embodiment 12
Weigh 5.00 g silica (SiO2) load 0.022 g Ga compound (Ga (TMHD)3).Normal temperature dipping Ga
(TMHD)3In 120 DEG C of drying 8 h, 500 DEG C of 4 h of roasting after 6 h of solution.By carrier loaded the 0.048 of load active component Ga
Compound (the NH of g Ir4)2IrCl6, in 120 DEG C of drying 12 h, 520 DEG C of 4 h of roasting after 6 h of normal temperature dipping, Ir-Ga/ is made
SiO2Catalyst.In the fixed-bed tube reactor of the catalyst prepared in being filled with 1 g embodiment 12, reactant third
Alkane, reaction temperature are 550 DEG C, and reaction pressure is normal pressure, 4 h of propane weight (hourly) space velocity (WHSV)-1, under conditions of hydrogen-hydrocarbon ratio is 1, propane turns
Rate 31.5%, Propylene Selectivity 96.5%.
The foregoing is merely presently preferred embodiments of the present invention, all equivalent changes done according to scope of the present invention patent with
Modification, is all covered by the present invention.
Claims (8)
1. one kind is used for dehydrogenating low-carbon alkane metal alloy catalyst, it is characterised in that: the catalyst includes tri- kinds of A, B and C
Component, any one in component A Pt, Pd, Rh and Ir precious metal element predecessor, account for total catalyst weight 0.1~
5wt%；B component is any one in Sn, Ge and Ga element predecessor, accounts for 0.1~5 wt% of total catalyst weight；Component C
For carrier, 90~99.8 wt% of total catalyst weight are accounted for.
2. according to claim 1 be used for dehydrogenating low-carbon alkane metal alloy catalyst, it is characterised in that: the A group
In point, the predecessor of Pt includes PtCl4·5H2O、H2PtCl4、K2PtCl4、(NH4)2PtCl6Or Pt (COD) Cl2Middle one kind；
The predecessor of Pd includes PdCl2·2H2O、K2PdCl4、Pd(NH3)4Cl2Or Pd (COD) Cl2One of；
The predecessor of Rh includes RhCl3·3H2O、K3RhCl6、(NH4)3RhCl6、 [Rh(COD)Cl]2、[(COD)RhOMe)]2Or
[(COD)RhOSi(OtBu)3]2One of；
The predecessor of Ir includes IrCl3·3H2O、K2IrCl6、(NH4)2IrCl6、[Ir(COD)Cl]2、[(COD)IrOMe]2Or
[(COD)IrOSi(OtBu)3]2One of.
3. according to claim 1 be used for dehydrogenating low-carbon alkane metal alloy catalyst, it is characterised in that: the B group
Point in, the predecessor of Sn include Dibutyltin oxide, stannous octoate, dimethyl tin oxide, di-n-octyltin oxide, tetraphenyltin,
One of tetrabutyltin；
The predecessor of Ge includes Ge (Ph)4、Ge(Me)4Or Ge (ETH)4One of；
The predecessor of Ga includes Ga (TMHD)3Or Ga (ACAC)3One of.
4. according to claim 1 be used for dehydrogenating low-carbon alkane metal alloy catalyst, it is characterised in that: the carrier is
Oxide, including SiO2、Al2O3、MgO、TiO2Or MgAl2O4In any one.
5. a kind of method for dehydrogenating low-carbon alkane metallic catalyst prepared as described in claim 1 ~ 4 is any, feature
It is: specifically includes the following steps:
(1) oxide is weighed, as carrier, impregnates B component, then through drying, roasting；
(2) component A is impregnated in step (1) above the carrier containing B component, then the lower alkanes are made in drying, roasting
Hydrocarbon dehydrogenation metal alloy catalyst.
6. the preparation method according to claim 5 for dehydrogenating low-carbon alkane metal alloy catalyst, it is characterised in that:
The dip time is the h of 1 h~24；The drying be in 60 DEG C~150 DEG C drying h of 1 h~12, roasting be
The h of 2 h~8 is roasted at 400 DEG C~650 DEG C.
7. a kind of application of catalyst as described in claim 1, it is characterised in that: the catalyst is for the de- of low-carbon alkanes
Hydrogen reaction, the low-carbon alkanes include the alkane of 2-4 carbon atom, and 400 DEG C~600 DEG C of reaction temperature, mass space velocity 0.5
~20 h-1。
8. application according to claim 7, it is characterised in that: the low-carbon alkanes are propane or iso-butane, dehydrogenation reaction
It is carried out in fixed bed reactors.
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