CN109465020A - It is a kind of using FAU type structure molecular screen as the isomerization catalyst preparation method of carrier - Google Patents
It is a kind of using FAU type structure molecular screen as the isomerization catalyst preparation method of carrier Download PDFInfo
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- 239000003054 catalyst Substances 0.000 title claims abstract description 81
- 238000006317 isomerization reaction Methods 0.000 title claims abstract description 29
- 238000002360 preparation method Methods 0.000 title claims abstract description 18
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims abstract description 100
- 239000002808 molecular sieve Substances 0.000 claims abstract description 99
- 238000000034 method Methods 0.000 claims abstract description 46
- 239000012298 atmosphere Substances 0.000 claims abstract description 29
- 229910052751 metal Inorganic materials 0.000 claims abstract description 25
- 239000002184 metal Substances 0.000 claims abstract description 25
- 239000001257 hydrogen Substances 0.000 claims abstract description 19
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 19
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 18
- 239000000843 powder Substances 0.000 claims abstract description 13
- 230000009467 reduction Effects 0.000 claims abstract description 13
- 150000001335 aliphatic alkanes Chemical class 0.000 claims abstract description 11
- 229910000510 noble metal Inorganic materials 0.000 claims abstract description 11
- 238000012545 processing Methods 0.000 claims abstract description 3
- 229910052799 carbon Inorganic materials 0.000 claims description 35
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 31
- 238000009826 distribution Methods 0.000 claims description 29
- 230000008569 process Effects 0.000 claims description 15
- 238000001354 calcination Methods 0.000 claims description 8
- 239000007789 gas Substances 0.000 claims description 7
- 229910052697 platinum Inorganic materials 0.000 claims description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 6
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 claims description 4
- 229930195733 hydrocarbon Natural products 0.000 claims description 3
- 150000002430 hydrocarbons Chemical class 0.000 claims description 3
- 229910052742 iron Inorganic materials 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 239000004215 Carbon black (E152) Substances 0.000 claims description 2
- 150000001336 alkenes Chemical class 0.000 claims description 2
- 229910052786 argon Inorganic materials 0.000 claims description 2
- 229910052793 cadmium Inorganic materials 0.000 claims description 2
- 229910052804 chromium Inorganic materials 0.000 claims description 2
- 229910052802 copper Inorganic materials 0.000 claims description 2
- 239000008246 gaseous mixture Substances 0.000 claims description 2
- 229910052741 iridium Inorganic materials 0.000 claims description 2
- 229910052749 magnesium Inorganic materials 0.000 claims description 2
- 229910052748 manganese Inorganic materials 0.000 claims description 2
- 229910052759 nickel Inorganic materials 0.000 claims description 2
- 229910052763 palladium Inorganic materials 0.000 claims description 2
- 238000011084 recovery Methods 0.000 claims description 2
- 229910052725 zinc Inorganic materials 0.000 claims description 2
- 150000001412 amines Chemical class 0.000 claims 1
- 239000000470 constituent Substances 0.000 claims 1
- 239000001307 helium Substances 0.000 claims 1
- 229910052734 helium Inorganic materials 0.000 claims 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 claims 1
- 239000011261 inert gas Substances 0.000 claims 1
- 229910052754 neon Inorganic materials 0.000 claims 1
- GKAOGPIIYCISHV-UHFFFAOYSA-N neon atom Chemical compound [Ne] GKAOGPIIYCISHV-UHFFFAOYSA-N 0.000 claims 1
- 150000003242 quaternary ammonium salts Chemical class 0.000 claims 1
- 239000011148 porous material Substances 0.000 abstract description 3
- 230000009257 reactivity Effects 0.000 abstract description 3
- 150000002739 metals Chemical class 0.000 abstract 1
- 239000002253 acid Substances 0.000 description 24
- 238000006243 chemical reaction Methods 0.000 description 15
- 239000003795 chemical substances by application Substances 0.000 description 11
- 238000006555 catalytic reaction Methods 0.000 description 8
- 238000012512 characterization method Methods 0.000 description 8
- 230000000052 comparative effect Effects 0.000 description 8
- 238000010792 warming Methods 0.000 description 8
- 238000007598 dipping method Methods 0.000 description 7
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 6
- 239000003708 ampul Substances 0.000 description 6
- 239000010453 quartz Substances 0.000 description 6
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 6
- 150000001722 carbon compounds Chemical class 0.000 description 5
- 238000011946 reduction process Methods 0.000 description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 238000007796 conventional method Methods 0.000 description 4
- SNRUBQQJIBEYMU-UHFFFAOYSA-N dodecane Chemical compound CCCCCCCCCCCC SNRUBQQJIBEYMU-UHFFFAOYSA-N 0.000 description 4
- 238000001035 drying Methods 0.000 description 4
- 238000005984 hydrogenation reaction Methods 0.000 description 4
- 229940094933 n-dodecane Drugs 0.000 description 4
- 239000003921 oil Substances 0.000 description 4
- 239000005416 organic matter Substances 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 229910020514 Co—Y Inorganic materials 0.000 description 3
- 229910020997 Sn-Y Inorganic materials 0.000 description 3
- 229910008859 Sn—Y Inorganic materials 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 230000006378 damage Effects 0.000 description 3
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 3
- 238000005259 measurement Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000001179 sorption measurement Methods 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- 210000003850 cellular structure Anatomy 0.000 description 2
- 238000006356 dehydrogenation reaction Methods 0.000 description 2
- 238000003795 desorption Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- NAQMVNRVTILPCV-UHFFFAOYSA-N hexane-1,6-diamine Chemical compound NCCCCCCN NAQMVNRVTILPCV-UHFFFAOYSA-N 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 238000005985 Hofmann elimination reaction Methods 0.000 description 1
- 239000002841 Lewis acid Substances 0.000 description 1
- 241000428199 Mustelinae Species 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 238000004026 adhesive bonding Methods 0.000 description 1
- 230000001588 bifunctional effect Effects 0.000 description 1
- 125000002915 carbonyl group Chemical group [*:2]C([*:1])=O 0.000 description 1
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 1
- 210000004027 cell Anatomy 0.000 description 1
- 238000004587 chromatography analysis Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 238000012937 correction Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 229910001882 dioxygen Inorganic materials 0.000 description 1
- WEHWNAOGRSTTBQ-UHFFFAOYSA-N dipropylamine Chemical compound CCCNCCC WEHWNAOGRSTTBQ-UHFFFAOYSA-N 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000004108 freeze drying Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- 150000007517 lewis acids Chemical class 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- CSJDCSCTVDEHRN-UHFFFAOYSA-N methane;molecular oxygen Chemical compound C.O=O CSJDCSCTVDEHRN-UHFFFAOYSA-N 0.000 description 1
- 239000012299 nitrogen atmosphere Substances 0.000 description 1
- 238000011017 operating method Methods 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000002411 thermogravimetry Methods 0.000 description 1
- 229910052718 tin Inorganic materials 0.000 description 1
- 230000004580 weight loss Effects 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
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
- B01J29/10—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing iron group metals, noble metals or copper
- B01J29/12—Noble metals
- B01J29/126—Y-type faujasite
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
- B01J29/10—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing iron group metals, noble metals or copper
- B01J29/14—Iron group metals or copper
- B01J29/146—Y-type faujasite
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
- C10G49/02—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 characterised by the catalyst used
- C10G49/08—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
-
- 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
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/10—After treatment, characterised by the effect to be obtained
- B01J2229/18—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1022—Fischer-Tropsch products
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Crystallography & Structural Chemistry (AREA)
- Materials Engineering (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a kind of using FAU type structure molecular screen as the preparation method of the isomerization catalyst of carrier.Specific step is as follows for catalyst preparation: carrying out part demoulding processing to the molecular screen primary powder with FAU type structure first at 100-400 DEG C；It again will be on the group VIII noble metals active component molecular sieve that is carried on that treated；Then reduction obtains final catalyst in hydrogen atmosphere.By the removing mode of template in control molecular sieve carrier, the Effective Regulation of catalyst metals property, Acidity and pore properties is realized.Compared with the catalyst made from the prior art, high reactivity and isomers yield are shown in normal alkane isomerization reaction using catalyst made from the method for the present invention.
Description
Technical field
The invention belongs to petrochemical industry, fine chemistry industry and molecular sieve catalyst fields, and in particular to one kind is with FAU type structure
Molecular sieve is the isomerization catalyst preparation method and application of carrier.
Technical background
Alkane isomerization reaction has a very important role during the quality-improving of oil product.Light paraffins add hydrogen
Isomerization can produce high-octane gasoline blend component, and long chain alkane hydroisomerization is mainly used for improving boat coal, bavin
The low temperature fluidity of oil and lubricating oil.Currently, it is negative by carrier of molecular sieve for being applied to the state-of-the-art catalyst of the reaction
Carrier has plus the bifunctional catalyst of the metal component of (de-) hydrogen performance.US4710485,5135638,5282598,
The patent documents such as CN1792451,1788844,101245260 all report the alkane isomerization catalyst using molecular sieve as carrier
Preparation.
In alkane isomerization reaction process, metal position mainly provides hydrogenation/dehydrogenation performance, the acidic site of molecular sieve carrier
Isomerization/cracking performance is provided, the cellular structure of molecular sieve provides shape-selective function.The isomerization performance of catalyst by its metal,
Acid and duct codetermines.
Generally, using molecular sieve as the acidity and duct template in molecular sieve of the isomerization catalyst of carrier
Removing.The method of template is usually to be roasted in air atmosphere using the temperature not less than 500 DEG C in removing molecular sieve.
For example, template di-n-propylamine (J.Colloid of the Liu et al. in air atmosphere in 600 DEG C of calcination process 6h removing SAPO-11
Interf.Sci.2014,418,193.)；550 DEG C of calcination process in air atmosphere such as Philippaerts remove ZSM-5 for 24 hours
In template 4-propyl bromide (J.Catal.2010,270,172.)；Liu et al. 550 DEG C of calcination process in air atmosphere
8h removes the template hexamethylene diamine (J.Catal.2016,335,11.) in ZSM-22.
In above-mentioned roasting knockout course, it is high that vapor part with caused by that oxidizing fire reaction generates occurs for template
Warm high pressure can destroy the skeleton structure of molecular sieve, influence the pore properties and Acidity of molecular sieve.Corma etc. has found 540 DEG C of roastings
Burning demoulding will lead to molecular sieve and dealuminzation phenomenon occurs, influence the surface acidity (J.Catal.1994,148,569.) of molecular sieve.
The discoveries such as Ward roasting calcining temperature is higher than 500 DEG C of destructions that will cause Y molecular sieve structural hydroxyl, so that molecular sieveAcid (B acid) amount is reduced, and Lewis acid (L acid) amount increases (J.Catal.1968,11,251.).
FAU type molecular sieve has three-dimensional twelve-ring cellular structure, and port size is aboutUsing it as carrier
Loaded catalyst shows excellent performance in long chain alkane hygrogenating isomerization reaction.It is similar with above-mentioned release method,
Molecular sieve is often removed using higher temperature (being not less than 500 DEG C) in preparation using FAU type molecular sieve as the catalyst of carrier
In template.Therefore, the stripping means in the molecular sieve analog are controlled by new tool, realized to FAU type structural molecule
The regulation of the Acidity and pore properties of sieve for preparing there are the hydroisomerisation catalysts of high isomers yield very must
It wants.
Studies have shown that the metallicity (hydrogenation/dehydrogenation performance) of catalyst is related to the load situation of metal.Martens
Etc. shadow of the load situation to Pt/Y-A (mixture that Y-A carrier is molecular sieve and aluminium oxide) isomerization performance for having investigated Pt
It rings, finds compared with the catalyst that Pt is carried in Y molecular sieve duct, Pt is carried on the catalyst on aluminium oxide in alkane isomery
High isomer selective (Nature 2015,528,245.) is shown in change.It thereby it is assumed that, be carried on molecular sieve
The metal component of outer surface is conducive to improve performance of the catalyst in isomerization reaction.And preparation method conventional at present is difficult to
Control the load situation of metal component over a molecular sieve.Therefore, exploitation control metal component is carried on the side of molecular sieve outer surface
Method is particularly significant.
The present invention proposes a kind of using FAU type structure molecular screen as the preparation method of the isomerization catalyst of carrier.Pass through elder generation
Segment template agent in roasting removing molecular sieve, then carried metal active component, is thoroughly taken off using the reduction process of catalyst
Except the template in molecular sieve.Firstly, roasting under 100-400 DEG C of relative low temperature, the template in molecular sieve passes through
The reactions such as Hofmann elimination generate active carbon species, are an endothermic processes.Then, molecular sieve carried hydrogenation metal component,
It is restored in hydrogen or hydrogeneous atmosphere；The active carbon species in molecular sieve are removed by catalytic hydrogenation at hydro carbons in this process.This
Invention makes full use of the reduction process of catalyst to demould, and the carbon species hydrogenation and removing in molecular sieve is compared with the oxygen in customary preparation methods
It is small to change removing heat release, and anhydrous steam generates, framework of molecular sieve structural damage is acted on small.
Meanwhile the load situation of metal component can also be controlled using the method for the present invention.In 50-400 DEG C of relative low temperature
The active carbon species of lower roasting, generation are blocked in the duct of molecular sieve, and the organic matter and impurity of outer surface absorption are then taken off
It removes, the hydroxyl of molecular sieve outer surface is exposed.Thus, in the loading process of metal component, metal component is due to molecular sieve
Duct blocks and cannot be introduced into the duct of molecular sieve, can only interact with the hydroxyl of molecular sieve outer surface, final
The catalyst of molecular sieve supported external surface is distributed only over to metal component.
To sum up, made from the conventional method compared with catalyst, had more using catalyst made from the method for the present invention
High acid amount and Micropore volume, metal component are distributed in the outer surface of molecular sieve, show in isomerization process higher
Reactivity and isomers yield.
Summary of the invention
The purpose of the present invention is to provide a kind of using FAU type structure molecular screen as the preparation side of the isomerization catalyst of carrier
Method.
Specifically, the present invention provides a kind of using FAU type structure molecular screen as the isomerization catalyst preparation method of carrier,
It is characterized by: the segment template agent in first roasting removing molecular sieve, then carried metal active component, utilizes catalyst reduction
Process thoroughly removes the template in molecular sieve, and isomerization catalyst is made, includes the following steps,
(1) template, the calcination process 0.5- at 100-400 DEG C of the molecular screen primary powder with FAU type structure will be contained
18h, carbon distribution and content of organics are the 0.5-20wt.% of molecular sieve in the molecular sieve after roasting；
(2) by the molecular sieve carried group VIII noble metals active component after roasting in (1), group VIII noble metals component
Content be 0.05-10wt.%；
(3) in a reducing atmosphere by the sample after carried metal component in (2), 150-450 DEG C of reduction 0.5-12h is made
Isomerization catalyst.
Treatment temperature described in method and step (1) provided by the present invention is 150-400 DEG C, and the processing time is 1-12h；
Carbon distribution and content of organics are point in molecular sieve after roasting described in method and step (1) provided by the present invention
The 0.5-15wt.% of son sieve weight；
Calcination process process described in method and step (1) provided by the present invention is generally in oxygen-containing atmosphere (such as air, oxygen
Gas, ozone etc.) in carry out, can also be in inert atmosphere (such as nitrogen, argon gas) or reducing atmosphere (such as hydrogen, hydrogen sulfide, an oxygen
Change carbon etc.) in carry out；
Reduction temperature described in method and step (3) provided by the present invention is 200-400 DEG C, recovery time 1-8h；
Reducing atmosphere described in method and step (3) provided by the present invention is that hydrogen or hydrogen and other gases are (such as lazy
Property gas, alkane, alkene etc.) gaseous mixture；
Group VIII noble metals active component described in method and step (2) provided by the present invention or step (3) be Pt,
One or more of elements such as Pd, Ir；
Group VIII noble metals content described in method and step (2) provided by the present invention is 0.05-5.0wt.%；
Described in method provided by the present invention with FAU type structure molecular sieve be Y, Me-Y (Me=Zn, Mg, Mn,
Co, Cr, Cu, Fe, Cd or Ni etc.), one or more of SAPO-37 etc..
The load of metal component described in method and step (2) provided by the present invention uses the operation side of this field routine
Method including but not limited to impregnates, precipitates, deposition, the addition operation such as adhesive bonding or mechanical press, making group VIII noble metals
Presoma is scattered on carrier, realizes the combination of group VIII noble metals and carrier；The metal precursor used includes but unlimited
In metal acid, metal acid-salt, chloride, ammino-complex, carbonyl complex or their mixture；
In the present invention, active carbon species react in the reduction process of catalyst with hydrogen, mainly generate it is hydrocarbon or
Hydronitrogen；And in conventional roasting process, oxidizing fire mainly occurs with oxygen for the template in molecular sieve, main raw
At carbon oxygen or oxynitrides；
It will be needed after on the metal component molecular sieve that is carried on that treated described in method and step (2) provided by the present invention
It is dried, the dry operating method for using this field routine, including but not limited to heat drying, freeze-drying is overcritical
Dry etc., common method is 40-300 DEG C of drying temperature, preferably 60-200 DEG C of drying temperature in air atmosphere；When dry
Between 0.5-24h, preferably drying time 1-8h；
Catalyst provided by the present invention can be widely applied to petroleum distillate, biomass, Fischer-Tropsch synthetic it is processed
Journey, such as isomerization-visbreaking, the processes such as isomerization dewaxing.
It is provided by the invention using FAU type structure molecular screen as the preparation of the catalyst of carrier with conventional preparation method ratio
Method has the advantages that
1. reducing the roasting calcining temperature of molecular sieve carrier, the energy consumption in catalyst preparation process is reduced；
2. making full use of the template in reduction process removing molecular sieve, reduce knockout course to framework of molecular sieve structure
Destruction, the catalyst being prepared has high Micropore volume and acid amount；
3. the isomerization catalyst of preparation is in alkane isomerization reaction with high activity and isomers yield.
Specific embodiment
The present invention is described further for embodiment below, but the invention is not limited to the following embodiments
In.Meanwhile embodiment has been merely given as realizing the partial condition of this purpose, being not meant to must satisfy these conditions just can be with
Reach this purpose.
The test of catalyst acid amount carries out on Micromeritics AutoChem2920 chemical adsorption instrument.Sample first exists
In-situ treatment 60min under the conditions of 350 DEG C of logical He, is then down to 100 DEG C for sample cell temperature, is passed through NH on adsorption instrument3, to be adsorbed
After saturation, lead to He and purge 60min, after waiting TCD detector baseline steady, rises to 700 DEG C with 10 DEG C/min, record NH3Desorption
Curve.The acid amount of sample is according to NH3Concentration correction curve and NH3Calculated by peak area is desorbed and obtains.
The carbon distribution and content of organics of sample are determined according to thermal gravimetric analysis results.Using German NETZSCH company STA
449F3 type instrument carries out thermogravimetric measurement to sample.Determination condition: sample sample-loading amount is the 10mg, (flow in air atmosphere
20ml/min) 900 DEG C are warming up to from 40 DEG C with the heating rate of 10 DEG C/min.The carbon distribution and content of organics of sample are sample heat
It is greater than 200 DEG C of weight loss in weight result.
The hole of catalyst holds measurement and carries out on Micromeritics ASAP2420 physical adsorption appearance.Before test, sample
The vacuumize process 6h at 200 DEG C, then carries out N under liquid nitrogen temperature2The measurement of absorption and desorption isotherm.The micropore of sample
Kong Rong is calculated by t-plot method.
Evaluating catalyst carries out in stainless steel fixed bed reactors, and the catalyst 1.0mL of preparation is taken to be loaded in reactor,
It is warming up to reaction temperature in a hydrogen atmosphere, logical feedstock oil n-dodecane is reacted, and product is by gas chromatographic analysis.React item
Part: 170-270 DEG C of reaction temperature, normal pressure, n-dodecane liquid hourly space velocity (LHSV) 1.0h-1, hydrogen-oil ratio (mol/mol) is 15.
Comparative example
The Y molecular sieve original powder (16.3wt.% that template agent content is molecular sieve) that 20g contains template is placed in stone
Ying Guanzhong, for 24 hours, cooled to room temperature obtains the Y molecular sieve that template removes completely and carries for 600 DEG C of roastings in air atmosphere
Body, carbon distribution and content of organics are 0 in molecular sieve carrier.With the H of 5.0mL 0.001g/mL containing Pt2PtCl6Solution impregnates on 5g
State molecular sieve carrier.Sample after dipping dries 2h at 120 DEG C, and 400 DEG C of reduction 4h, obtain 0.5wt.% in hydrogen atmosphere
Pt/Y catalyst.Carbon distribution and content of organics are 0 in catalyst, and the acid amount having is 0.82mmol/g, and Micropore volume is
0.208cm3/g.Carbon distribution and content of organics, the acid amount of catalyst and Micropore volume characterization result are shown in molecular sieve and catalyst
Table 1, catalysis reaction evaluating the results are shown in Table 2.
Embodiment 1
20g Y molecular sieve original powder identical with comparative example (16.3wt.% that template agent content is molecular sieve) is placed in
In quartz ampoule, in air atmosphere, 5 DEG C/min is warming up to 150 DEG C, roasts 4h at such a temperature, then cooled to room temperature,
The Y molecular sieve carrier that obtains that treated, carbon distribution and content of organics are 14.5wt.% in molecular sieve carrier.Contain Pt with 5.0mL
The H of 0.001g/mL2PtCl6Solution impregnates the above-mentioned molecular sieve carrier of 5g.Sample after dipping dries 2h at 120 DEG C, in hydrogen
300 DEG C of reduction 4h, obtain 0.5wt.%Pt/Y catalyst in atmosphere.Carbon distribution and content of organics are 0 in catalyst, the acid having
Amount is 1.44mmol/g, Micropore volume 0.279cm3/g.Carbon distribution and content of organics in molecular sieve and catalyst, catalyst
Acid amount and Micropore volume characterization result are shown in Table 1, and catalysis reaction evaluating the results are shown in Table 2.
Embodiment 2
By 20g contain template Co-Y molecular screen primary powder (template agent content be molecular sieve 17.3wt.%, Co
Content be 1.3wt.%) be placed in quartz ampoule, in air atmosphere, 5 DEG C/min is warming up to 230 DEG C, roasts at such a temperature
12h, then cooled to room temperature, the Co-Y molecular sieve carrier that obtains that treated, carbon distribution and organic matter contain in molecular sieve carrier
Amount is 13.3wt.%.With the H of 5.0mL 0.001g/mL containing Pt2PtCl6Solution impregnates the above-mentioned molecular sieve carrier of 5g.After dipping
Sample dry 2h at 120 DEG C, 400 DEG C of reduction 6h, obtain 0.5wt.%Pt/Co-Y catalyst in hydrogen atmosphere.Catalyst
Middle carbon distribution and content of organics are 0, and the acid amount having is 1.30mmol/g, Micropore volume 0.265cm3/g.It molecular sieve and urges
Carbon distribution and content of organics, the acid amount of catalyst and Micropore volume characterization result are shown in Table 1 in agent, and catalysis reaction evaluating result is shown in
Table 2.
Embodiment 3
By 20g contain template Sn-Y molecular screen primary powder (template agent content be molecular sieve 16.8wt.%, Sn
Content be 1.1wt.%) be placed in quartz ampoule, in air atmosphere, 5 DEG C/min is warming up to 300 DEG C, roasts at such a temperature
2h, then cooled to room temperature, the Sn-Y molecular sieve carrier that obtains that treated, carbon distribution and content of organics in molecular sieve carrier
For 10.1wt.%.With the H of 5.0mL 0.001g/mL containing Pt2PtCl6Solution impregnates the above-mentioned molecular sieve carrier of 5g.Sample after dipping
Product dry 2h at 120 DEG C, 400 DEG C of reduction 6h, obtain 0.5wt.%Pt/Sn-Y catalyst in hydrogen atmosphere.In catalyst
Carbon distribution and content of organics are 0, and the acid amount having is 1.18mmol/g, Micropore volume 0.249cm3/g.Molecular sieve and catalysis
Carbon distribution and content of organics, the acid amount of catalyst and Micropore volume characterization result are shown in Table 1 in agent, and catalysis reaction evaluating the results are shown in Table
2。
Embodiment 4
By 20g contain template Fe-Y molecular screen primary powder (template agent content be molecular sieve 16.2wt.%, Fe
Content be 0.9wt.%) be placed in quartz ampoule, in air atmosphere, 5 DEG C/min is warming up to 400 DEG C, roasts at such a temperature
1h, then cooled to room temperature, the Fe-Y molecular sieve carrier that obtains that treated, carbon distribution and content of organics in molecular sieve carrier
For 6.3wt.%.H with 5.0mL containing Pt0.001g/mL2PtCl6Solution impregnates the above-mentioned molecular sieve carrier of 5g.Sample after dipping
The dry 2h at 120 DEG C, 200 DEG C of reduction 8h, obtain 0.5wt.%Pt/Fe-Y catalyst in hydrogen atmosphere.Product in catalyst
Carbon and content of organics are 0, and the acid amount having is 1.02mmol/g, Micropore volume 0.225cm3/g.Molecular sieve and catalyst
Middle carbon distribution and content of organics, the acid amount of catalyst and Micropore volume characterization result are shown in Table 1, and catalysis reaction evaluating the results are shown in Table 2.
Embodiment 5
20g Y molecular sieve original powder identical with comparative example (16.3wt.% that template agent content is molecular sieve) is placed in
In quartz ampoule, in nitrogen atmosphere, 5 DEG C/min is warming up to 150 DEG C, roasts 8h at such a temperature, then cooled to room temperature,
The Y molecular sieve carrier that obtains that treated, carbon distribution and content of organics are 14.7wt.% in molecular sieve carrier.Contain Pt with 5.0mL
The H of 0.001g/mL2PtCl6Solution impregnates the above-mentioned molecular sieve carrier of 5g.Sample after dipping dries 2h at 120 DEG C, in hydrogen
400 DEG C of reduction 8h, obtain 0.5wt.%Pt/Y catalyst in atmosphere.Carbon distribution and content of organics are 0 in catalyst, the acid having
Amount is 1.43mmol/g, Micropore volume 0.273cm3/g.Carbon distribution and content of organics in molecular sieve and catalyst, catalyst
Acid amount and Micropore volume characterization result are shown in Table 1, and catalysis reaction evaluating the results are shown in Table 2.
Embodiment 6
20g Y molecular sieve original powder identical with comparative example (16.3wt.% that template agent content is molecular sieve) is placed in
In quartz ampoule, in hydrogen atmosphere, 5 DEG C/min is warming up to 200 DEG C, roasts 6h at such a temperature, then cooled to room temperature,
The Y molecular sieve carrier that obtains that treated, carbon distribution and content of organics are 14.2wt.% in molecular sieve carrier.Contain Pt with 5.0mL
The H of 0.001g/mL2PtCl6Solution impregnates the above-mentioned molecular sieve carrier of 5g.Sample after dipping dries 2h at 120 DEG C, in hydrogen
400 DEG C of reduction 1h, obtain 0.5wt.%Pt/Y catalyst in atmosphere.Carbon distribution and content of organics are 0 in catalyst, the acid having
Amount is 1.40mmol/g, Micropore volume 0.275cm3/g.Carbon distribution and content of organics in molecular sieve and catalyst, catalyst
Acid amount and Micropore volume characterization result are shown in Table 1, and catalysis reaction evaluating the results are shown in Table 2.
The characterization result of molecular sieve, catalyst in 1 comparative example of table and embodiment
The reaction evaluating result of 2 comparative example of table and the catalyst in embodiment
When a reaction temperature is 210 DEG C, n-dodecane conversion ratio on catalyst；
In b n-dodecane isomerization reaction, the maximum isomers yield of catalyst.
As shown in Table 1, carbon distribution and content of organics is 0 in the molecular sieve for using conventional method to demould in comparative example,
Containing a certain amount of in the molecular sieve obtained in embodiment 1-6 using 150-400 DEG C of the present invention roasting molecular screen primary powder
Carbon distribution and organic matter.But after catalyst reduction, contained carbon distribution and organic matter are removed completely.The effect of generation are as follows: with comparison
Catalyst made from conventional method is compared in example, and embodiment 1-6 uses method of the invention, and gained catalyst has high acid amount
With big Micropore volume.
As shown in Table 2, made from the comparative example conventional method compared with catalyst, the method for the present invention is used in embodiment 1-6
The catalyst being prepared shows high reactivity and isomers yield in alkane hygrogenating isomerization reaction.
Claims (9)
1. a kind of using FAU type structure molecular screen as the isomerization catalyst preparation method of carrier, it is characterised in that: in 100-400
DEG C roasting FAU type structure molecular screen original powder, then carried metal active component, then restored and isomerization catalyst is made, including
Following steps,
(1) template, the calcination process 0.5-18h at 100-400 DEG C of the molecular screen primary powder with FAU type structure, control will be contained
Carbon distribution and content of organics are the 0.5-20wt.% of molecular sieve in molecular sieve after system roasting,
(2) by the molecular sieve carried group VIII noble metals active component after roasting in (1), group VIII noble metals component contains
Amount is 0.05-10wt.%,
(3) in a reducing atmosphere by the sample after load group VIII noble metal component in (2), 150-450 DEG C of reduction 0.5-
Isomerization catalyst is made in 12h.
2. according to the method described in claim 1, it is characterized by: treatment temperature in the step (1) is 150-400 DEG C,
The processing time is 1-12h.
3. method according to claim 1, it is characterised in that: in the molecular sieve in the step (1) after control roasting
Carbon distribution and content of organics are the 0.5-15wt.% of molecular sieve.
4. method according to claim 1, it is characterised in that: the reduction temperature in the step (3) is 200-400
DEG C, recovery time 1-8h.
5. method according to claim 1, it is characterised in that: the reducing atmosphere in the step (3) is hydrogen or hydrogen
Gas and other gases (alkane of one of such as inert gas gas such as nitrogen, helium, neon, argon gas or two kinds or more, C1-C4
Hydrocarbon, one of the alkene etc. of C1-C4 or two kinds or more) gaseous mixture, the volume content of hydrogen is 5-100%.
6. method according to claim 1, it is characterised in that: the group VIII in the step (2) or step (3) is expensive
Metal active constituent is one of elements such as Pt, Pd, Ir or two kinds or more.
7. method according to claim 2, it is characterised in that: the group VIII noble metals content in the step (2)
For 0.05-5.0wt.%.
8. method according to claim 1, it is characterised in that: the molecular sieve with FAU type structure is Y, Me-
Y (one of Me=Zn, Mg, Mn, Co, Cr, Cu, Fe, Cd or Ni etc. or two kinds or more, mass content 0.05-
5wt.%), one of SAPO-37 etc. or two kinds or more.
9. according to the method described in claim 1, it is characterized by: template is organic in the step (1) molecular screen primary powder
One of amine, quaternary ammonium salt, metal organic complex etc. or two kinds or more, content are the 0.5-25wt.% of molecular sieve.
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