CN103539614B - The reaction method of dehydrogenating low-carbon alkane producing light olefins - Google Patents

The reaction method of dehydrogenating low-carbon alkane producing light olefins Download PDF

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CN103539614B
CN103539614B CN201210240059.9A CN201210240059A CN103539614B CN 103539614 B CN103539614 B CN 103539614B CN 201210240059 A CN201210240059 A CN 201210240059A CN 103539614 B CN103539614 B CN 103539614B
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catalyst
low
carbon
reaction
alkane
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CN103539614A (en
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吴文海
吴省
樊志贵
马春景
张新玉
缪长喜
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Abstract

The present invention relates to a kind of method preparing low-carbon alkene for dehydrogenating low-carbon alkane, mainly solve that existing catalyst noble metal consumption is high, selectivity is low under the high temperature conditions, cause catalyst carbon deposit serious, the problem of one way poor stability.The present invention passes through to adopt with propane/Trimethylmethane for raw material, in temperature of reaction 520 ~ 620 oc, reaction pressure 0 ~ 0.4MPa, alkane mass space velocity 0.1 ~ 8.0h -1, H 2/ C nh 2n+2volume ratio is under 0.2 ~ 1.6 condition, raw material and catalyst exposure, and reaction generates the technical scheme of propylene/iso-butylene, solves this problem preferably, can be used for the industrial production of dehydrogenating low-carbon alkane producing light olefins catalyzer.

Description

The reaction method of dehydrogenating low-carbon alkane producing light olefins
Technical field
The present invention relates to a kind of reaction method of dehydrogenating low-carbon alkane producing light olefins.
Background technology
Propylene/iso-butylene mainly from coproduction or the by-product of steam cracking and refinery factory fluid catalytic cracking process, can be widely used in synthetic polymer, gasoline dope, rubber and various chemical intermediate.Growing with low-carbon alkene demand, what traditional production process was difficult to meet the need of market increases rapidly.The a large amount of low-carbon alkanes obtained by refinery are main components of liquefied petroleum gas (LPG), are mainly used as domestic fuel.Develop and opened up new alkene by low-carbon alkanes preparing low-carbon olefins process originate significant for making full use of low-carbon alkanes.At present, propane catalytic dehydrogenation technology with the Catofin technique of the Oleflex technique of Uop Inc. and Lummus company for representative.The domestic production equipment still not having dehydrogenating low-carbon alkane producing light olefins.
Dehydrogenating low-carbon alkane catalyzed reaction is carried out under high temperature, lower pressure, and catalyst carbon deposit inactivation is serious, and the catalyzer of exploitation high reactivity, highly selective and high stability becomes the key of this technology.The disclosed catalyzer of Chinese patent (CN200710025372.X), be the preparation method of platinum-impregnated tin component on carrier at alumina modified mesoporous molecular sieve, conversion of propane is only 17%, Propylene Selectivity 93%; Chinese patent (CN200710023431.X) adopts the method for Hydrothermal Synthesis that tin is introduced ZSM-5 molecular sieve carrier, and by pickling process Supported Pt Nanoparticles component, after this catalyzer runs 100 hours, conversion of propane is higher than 30%, Propylene Selectivity 99%, but this patent does not provide the stability data of coke-burning regeneration process.Chinese patent (CN200710020064.8) and (CN200710133324.2) disclose a kind of platinum-tin catalyst and react for dehydrogenating propane, have employed the preparation method of tin component and platinum component total immersion stain, carrier is that Y type, ZSM-5 etc. are containing Na molecular sieve, after catalyzer runs 720 hours continuously, conversion of propane 30.5%, Propylene Selectivity 96.4%, but activity decrease half after twice coke-burning regeneration.
Above-mentioned catalyzer all have employed the active ingredient tin that aluminum oxide carrys out supported catalyst, the easy coking deactivation of catalyzer in applied at elevated temperature process, the poor stability of catalyzer.The thin shell type Pt system's dehydrogenation catalyst adopting the method for doped element periodictable II B compound and rare earth element to obtain also has no report for the document that low-carbon alkanes prepares low-carbon alkene.
In addition, adopt precious metal as the active ingredient of catalyzer, due to expensive, therefore its content is often lower.Research finds that the non-uniform Distribution of active ingredient in carrier can reduce the consumption of precious metal, improves the utilization ratio of precious metal; Meanwhile, in many reactions, the catalyzer of non-uniform Distribution showed than equally distributed catalyzer better activity, selectivity and the life-span.Wherein, on carrier, in eggshell type, the catalyzer of distribution may be used for the selectivity or the raising quick response selectivity that improve cascade reaction intermediate product to active ingredient, namely when internal diffusion speed is much smaller than intrinsic reaction rate, if speed of reaction is very fast, reactant molecule has just diffused in duct a bit apart from just having reacted away, and rate of diffusion is too slow, make the internal surface of catalyst center part do not utilized like this, thus active ingredient is prepared into thin shell type distribution.In addition, Active components distribution also helps the transfer of energy in outside surface.Therefore this technology is industrially widely used and achieves good effect.
Summary of the invention
Technical problem to be solved by this invention there is catalyzer easy coking deactivation in applied at elevated temperature process in existing technology of preparing, the problem of poor stability, a kind of method for dehydrogenating low-carbon alkane producing light olefins is newly provided, the method has when using under the high temperature conditions, catalyst selectivity, transformation efficiency are high, catalyst carbon deposit deactivation rate is slow, the advantage that stability is high.
In order to solve the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of reaction method for dehydrogenating low-carbon alkane producing light olefins, with propane or/and Trimethylmethane is for raw material, in temperature of reaction 520 ~ 620 oc, reaction pressure 0 ~ 0.4MPa, alkane mass space velocity 0.1 ~ 8.0h -1, H 2/ C nh 2n+2volume ratio is under 0.2 ~ 1.6 condition, raw material and catalyst exposure, reaction generation third rare/iso-butylene, wherein catalyst comprises following component:
A) α-Al will be selected from 2o 3, γ-Al 2o 3, δ-l 2o 3, θ-Al 2o 3, spinel, zeolite, titanium oxide or zirconic at least one coated porous material slurries be coated in and be selected from α-Al 2o 3, γ-Al 2o 3, δ-l 2o 3, metal, SiC, trichroite, quartz, at least one inert support in mullite or titanium oxide kernel on as complex carrier, complex carrier is 90 ~ 99.5% of catalyst weight;
B) be selected from least one in ruthenium in platinum metals, rhodium, palladium, osmium, iridium or platinum, count 0.01 ~ 1.2% of catalyst weight with simple substance;
C) be selected from least one in the periodic table of elements II B compound, count 0.01 ~ 4.0% of catalyst weight with simple substance;
D) be selected from the catalyst aid (M) of rare earth element, at least one in La, Nd, Lu, Eu, Ce, Yb, Tb or Ho, counts 0.01 ~ 4.0% of catalyst weight with simple substance;
E) be selected from least one in the periodic table of elements I A or II A compound, count 0.01 ~ 1.0% of catalyst weight with simple substance.
In technique scheme, temperature of reaction preferable range is 540 ~ 600 oc; Reaction pressure preferable range is 0.05 ~ 0.35MPa; Starting alkane air speed preferable range is 0.5 ~ 5.6h -1; H 2/ C nh 2n+2the preferable range of volume ratio is 0.4 ~ 1.0; Reaction raw materials is propane, Trimethylmethane or the mixture of the two; The adsorptive power checking catalyst activity component presoma in support of the catalyst is more weak, and preferred version is selected from trichroite, quartz, mullite, γ-Al 2o 3in at least one, consumption is 80 ~ 95% of complex layered carrier; The coating of lamellar composite carrier is heat-resisting porous adsorbing material, comparatively strong to the adsorptive power of active ingredient presoma, and has high specific surface area, and its preferred version is selected from γ-Al 2o 3, δ-l 2o 3, θ-Al 2o 3or at least one of spinel, consumption is 5 ~ 20% of lamellar composite carrier weight, and coat-thickness is 5 ~ 200 microns, specific surface area 50 ~ 200m2/g.Platinum metals is selected from Pt or Pd, and preferable range counts 0.1 ~ 1.0% of catalyst weight with simple substance.The periodic table of elements I A or II element A are selected from least one in Li, Na, K, Ca, Mg or Ba, and preferable range counts 0.05 ~ 0.6% of catalyst weight with simple substance.Composition metal auxiliary agent comprises at least one in the periodic table of elements II B compound, and preferable range is to count 1.0 ~ 2.0% of catalyst weight with simple substance; Be selected from the catalyst aid (M) of rare earth element, at least one in La, Nd, Lu, Eu, Ce, Yb, Tb or Ho, preferable range is to count 0.1 ~ 2.0% of catalyst weight with simple substance.
In the inventive method, the preparation method of used catalyst comprises the following steps:
A) α-Al will be selected from 2o 3, γ-Al 2o 3, δ-l 2o 3, θ-Al 2o 3, zeolite, spinel, titanium oxide or zirconic at least one coated porous material slurries be coated in and be selected from α-Al 2o 3, γ-Al 2o 3, δ-l 2o 3, metal, SiC, trichroite, quartz, at least one inert support in mullite or titanium oxide kernel on; Prior to 50 ~ 250 odrying 1 ~ 15 hour under C, then 700 ~ 1000 oc roasting makes coating and carrier effectively combine for 1 ~ 9 hour, obtains lamellar composite carrier;
B) mixing solutions I is prepared, comprise the soluble salt aqueous solution of II B compound Zn of aequum, Cd, Hg, rare earth element auxiliary agent M and I A or II element A, its rare earth elements auxiliary agent M is selected from least one in La, Ce, Pr, Eu or Tm, and I A/ II element A is selected from least one in Li, Na, K, Ca, Mg or Ba; The platinichloride aqueous solution II of preparation aequum;
C) with pickling process by soluble salt load contained in solution I and II in composite catalyst carrier, flood after 12 ~ 48 hours, after drying, obtain catalyst precursor;
D) catalyst precursor is 450 ~ 650 oc roasting 0.5 ~ 12 hour, and obtain dehydrogenating low-carbon alkane producing light olefins catalyzer with hydrogen reducing with steam dechlorination after 0.5 ~ 10 hour.
Dehydrogenating low-carbon alkane reaction is carried out on the miniature catalyst reaction device of continuous flow quartz tube reactor.Reaction conditions: temperature 520 ~ 650 oc, pressure 0 ~ 0.4MPa, alkane mass space velocity 0.1 ~ 8.0h -1, H 2/ C nh 2n+2be 0.1 ~ 1.6; Product analysis adopts HP-5890 gas chromatograph (HP-AL/S capillary column, 50m × 0.53mm × 15 μm; Fid detector) alkane in on-line analysis dehydrogenation product, olefin(e) centent calculate the transformation efficiency of reaction, selectivity and yield.
On carrier, in eggshell type, the catalyzer of distribution may be used for the selectivity or the raising quick response selectivity that improve cascade reaction intermediate product to active ingredient, namely when internal diffusion speed is much smaller than intrinsic reaction rate, if speed of reaction is very fast, reactant molecule has just diffused in duct a bit apart from just having reacted away, and rate of diffusion is too slow, make the internal surface of catalyst center part do not utilized like this, thus active ingredient is prepared into thin shell type distribution.And Active components distribution also helps the transfer of energy in outside surface.In addition, the dehydrogenation reaction of the low-carbon (LC) hydro carbons occurred in metallic surface, generate the alkene of electron rich, and if even can not just be easy to be polymerized further at catalyst surface from metallic surface desorption in time, dehydrogenation, cyclisation generation catalyst surface further carbon distribution affect the stability of catalyzer.The introducing of metal promoter plays critical effect for platinum group dehydrogenation catalyst, find after a large amount of experiments, the composite assistant that II B race elementary composition and rare earth element component form can play good promoter action for the activity of catalyzer, this is likely can interact with metal platinum component well after metal promoter introduces catalyzer, change the characteristic electron of metal platinum, add the cloud density of metal platinum, thus make the easier desorption of the alkene of electron rich, thus decrease carbon distribution, enhance the stability of catalyzer.
Dehydrogenating low-carbon alkane reaction is carried out on the miniature catalyst reaction device of continuous flow quartz tube reactor.Reaction conditions: temperature 520 ~ 650 oc, pressure 0 ~ 0.4MPa, alkane mass space velocity 0.1 ~ 8.0h -1, H 2/ C nh 2n+2be 0.1 ~ 1.6; Product analysis adopts HP-5890 gas chromatograph (HP-AL/S capillary column, 50m × 0.53mm × 15 μm; Fid detector) alkane in on-line analysis dehydrogenation product, olefin(e) centent calculate the transformation efficiency of reaction, selectivity and yield.The catalyzer using method provided by the invention to prepare reacts for dehydrogenating low-carbon alkane, and propane/Trimethylmethane transformation efficiency reaches 37%/45%, olefine selective is higher than 91%; Through 24 coke-burning regenerations, Trimethylmethane transformation efficiency remains on 43.2%, and olefine selective is higher than 92%, and catalyst performance stabilised, achieves good technique effect.
Below by embodiment, the present invention is further elaborated.
Embodiment
[embodiment 1]
By 280 grams of Alumina gel (aluminum oxide containing 16% mass ratio), 30.0 grams of barium oxide, 7.0 grams of zirconyl chlorides, 68 grams of mordenite powder (less than <5 μm, specific surface area 270m 2/ g), 12.8g6% polyvinyl alcohol and the mixing of 120 grams of distilled water, stir 1 hour obtained coating paste, the trichroite bead of diameter 4mm is impregnated into join mixed coating slurry in, placement is spent the night, in 80 odry 2 hours of C, is then warming up to 150 oc dry 2 hours again, finally in 900 oc roasting 3 hours, obtains lamellar composite carrier.Analysis shows coat-thickness about 120 μm, and coating specific surface area is 186m 2/ g.
The mixing solutions of 130ml containing catalyst activity component is added, comprising NaNO in above-mentioned obtained 280.8g carrier 3, 2.2g; La (NO 3) 36H 2o, 2.5g; Zn (NO 3) 26H 2o, 1.91g; H 2ptCl 66H 2o, 2.23g flood 24 hours, and then 60 oc is dried, and in the air stream 530 oc roasting 3 hours, then uses water vapour 530 o4 hours are processed, finally logical dry air 530 under C oc process obtains catalyst sample in 1 hour, is designated as A.Sample uses hydrogen before dehydrogenation reaction, and 500 oc reduction activation 90 minutes, for propane/dehydrogenation of isobutane reaction.Reaction result is in table 2.
[embodiment 2]
By 300 grams of Alumina gel (aluminum oxide containing 16% mass ratio), 380g3% polyacrylamide solution makes slurries.Then in this mixed solution, add 3g Calucium Silicate powder, 300g θ-Al 2o 3powder, stirs and adds about 20g magnesium chloride brine after 20 minutes, and the slurries obtained at room temperature ball milling make Particle size control for 4 hours below 20 μm.Obtained coating paste sprays to the α-Al of diameter 4mm 2o 3on bead, in 80 odry 2 hours of C, is then warming up to 150 oc dry 2 hours again, finally in 800 oc roasting 10 hours, obtains lamellar composite carrier.Analysis shows coat-thickness about 80 μm, and coating specific surface area is 121m 2/ g.
By the method Kaolinite Preparation of Catalyst of embodiment 1, difference is; H 2ptCl 66H 2o, 5.3g; Zn (NO 3) 26H 2o, 13.6g; Ce (NO 3) 36H 2o, 7.0g; Mg (NO 3) 26H 2o, 10.7g.Gained catalyst weight composition is in table 1, and be designated as B, reaction result is in table 2.
[embodiment 3]
By 350 grams of Alumina gel (aluminum oxide containing 25% mass ratio), the cyclodextrin soln of 50g40% silicon sol, 600g4%, 20g lanthanum trioxide, 10g cetyl trimethylammonium bromide make slurries.Then in this mixed solution, 4g Calucium Silicate powder, 3g salt of wormwood and 400g is added through the δ-Al of pretreated size below 10 μm 2o 3powder, the slurries obtained at room temperature ball milling make Particle size control for 4 hours below 10 μm.Obtained coating paste sprays on the mullite bead of diameter 4mm, in 80 odry 2 hours of C, is then warming up to 150 oc dry 2 hours again, finally in 900 oc roasting 8 hours, obtains lamellar composite carrier.Analysis shows coat-thickness about 100 μm, and coating specific surface area is 135m 2/ g.
By the method Kaolinite Preparation of Catalyst of embodiment 1, difference is; (NH 4) 2pdCl 4, 3.4g; Zn (NO 3) 26H 2o, 7.3g; La (NO 3) 36H 2o, 14.0g; KNO 3, 4.5g.Gained catalyst weight composition is in table 1, and be designated as C, reaction result is in table 2.
[embodiment 4]
By 380 grams of Alumina gel (aluminum oxide containing 20% mass ratio), the cyclodextrin soln of 600g4%, 40g lanthanum nitrate, 10g cetyl trimethylammonium bromide make slurries.Then in this mixed solution, 2g Calucium Silicate powder and 400g is added through the δ-Al of pretreated size below 5 μm 2o 3powder, the slurries obtained at room temperature ball milling make Particle size control for 4 hours below 10 μm.Obtained coating paste sprays on the mullite bead of diameter 4mm, in 80 odry 2 hours of C, is then warming up to 150 oc dry 2 hours again, finally in 950 oc roasting 6 hours, obtains lamellar composite carrier.Analysis shows coat-thickness about 90 μm, and coating specific surface area is 112m 2/ g.
By the method Kaolinite Preparation of Catalyst of embodiment 1, difference is; H 2ptCl 66H 2o, 0.7g; Cd (NO 3) 24H 2o, 4.1g; Nd (NO 3) 36H 2o, 3.0g; Ca (NO 3) 24H 2o, 0.1g.Gained catalyst weight composition is in table 1, and be designated as D, reaction result is in table 2.
[embodiment 5]
By 400 grams of Alumina gel (aluminum oxide containing 15% mass ratio), the glycerine solution of 600g2% makes slurries.Then in this mixed solution, 5g potassium felspar sand and 400g is added through the γ-Al of pretreated size below 10 μm 2o 3powder (specific surface area 200m 2/ g), the slurries obtained at room temperature ball milling make Particle size control for 4 hours below 10 μm.Obtained coating paste sprays on the SiC bead of diameter 4mm, in 80 odry 2 hours of C, is then warming up to 150 oc dry 2 hours again, finally in 1000 oc roasting 6 hours, obtains lamellar composite carrier.Analysis shows coat-thickness about 120 μm, and coating specific surface area is 174m 2/ g.
By the method Kaolinite Preparation of Catalyst of embodiment 1, difference is; Rh (NO 3) 32H 2o, 3.2g; Zn (NO 3) 26H 2o, 5.2g; Ce (NO 3) 36H 2o, 0.6g; NaNO 3, 4.6g.Gained catalyst weight composition is in table 1, and be designated as E, reaction result is in table 2.
[comparative example 1]
By the method Kaolinite Preparation of Catalyst of embodiment 1, difference adopts the pure γ of 4mm-Al 2o 3bead is as carrier impregnation SnCl 45H 2o, 5.9g; NaNO 3, 2.5g; H 2ptCl 66H 2o, 2.9g.Gained catalyst weight composition is in table 1, and be designated as F, reaction result is in table 2, and reaction conditions is with embodiment 1.
[comparative example 2]
By the method Kaolinite Preparation of Catalyst of comparative example 1, difference does not add Zn (NO 3) 26H 2o and La (NO 3) 36H 2o active ingredient presoma is SnCl 45H 2o, 4.5g; NaNO 3, 2.8g; H 2ptCl 66H 2o, 2.3g.Gained catalyzer composition is in table 1, and be designated as G, reaction result is in table 2, and reaction conditions is with embodiment 1.
Table 1
Embodiment 1 ~ 5, comparative example 1 ~ 2 at normal pressure, temperature 550 oc; C nh 2n+2/ H 2=5/2 (vol/vol); Alkane air speed (WHSV) is 4.6h -1carry out activity rating under condition, test result lists in table 2.
Table 2*
* the data in bracket are for adopting same catalyst, and raw material changes the dehydrogenation data of propane into.
[comparative example 3]
The comparative example 1 gained catalyzer F (adopting traditional Sn auxiliary agent) and comparative example 2 catalyzer G that do not contain composition metal auxiliary agent are carried out the experiment of stability, and contrast with embodiment 1, experimental result is in A, F, the G in table 2.Reaction conditions is with embodiment 1.The catalyzer F transformation efficiency of containing metal auxiliary agent does not drop to 22.7% from 41.3% after 100 hours, and lowering speed is far above catalyst A (only dropping to 33.7% from 45.6%), and selectivity is far below A.Comparative example 2 gained catalyzer G, also has similar result.
[comparative example 4]
Embodiment 1 gained catalyzer is carried out coke-burning regeneration performance evaluation, and reaction conditions is with embodiment 1, and the reaction result of catalyzer after 6 hours is in table 3, and raw material is Trimethylmethane.
Table 3
[embodiment 6 ~ 12]
Embodiment 1 is carried out performance evaluation under differential responses processing condition, the results are shown in Table 4.
Table 4

Claims (6)

1. a method for low-carbon alkene is prepared for dehydrogenating low-carbon alkane, with propane or/and Trimethylmethane is raw material, temperature of reaction 520 ~ 650 DEG C, reaction pressure 0 ~ 0.4MPa, alkane mass space velocity 0.1 ~ 8.0h -1, H 2/ C nh 2n+2volume ratio is under 0.2 ~ 1.6 condition, raw material and catalyst exposure, reaction generation third rare/iso-butylene; Wherein catalyst comprises following component:
A) α-Al will be selected from 2o 3, γ-Al 2o 3, δ-l 2o 3, θ-Al 2o 3, spinel, zeolite, titanium oxide or zirconic at least one coated porous material slurries be coated in and be selected from α-Al 2o 3, γ-Al 2o 3, δ-l 2o 3, metal, SiC, trichroite, quartz, at least one inert support in mullite or titanium oxide kernel on as complex carrier, complex carrier is 90 ~ 99.5% of catalyst weight;
B) be selected from least one in ruthenium in platinum metals, rhodium, palladium, osmium, iridium or platinum, count 0.01 ~ 1.2% of catalyst weight with simple substance;
C) be selected from least one in the periodic table of elements II B compound, count 0.01 ~ 4.0% of catalyst weight with simple substance;
D) be selected from catalyst aid M, catalyst aid M is at least one in La, Nd, Lu, Eu, Ce, Yb, Tb or Ho, counts 0.01 ~ 4.0% of catalyst weight with simple substance;
E) be selected from least one in the periodic table of elements I A or II A compound, count 0.01 ~ 1.0% of catalyst weight with simple substance;
The preparation method of used catalyst comprises the following steps:
A) α-Al will be selected from 2o 3, γ-Al 2o 3, δ-l 2o 3, θ-Al 2o 3, zeolite, spinel, titanium oxide or zirconic at least one coated porous material slurries be coated in and be selected from α-Al 2o 3, γ-Al 2o 3, δ-l 2o 3, metal, SiC, trichroite, quartz, at least one inert support in mullite or titanium oxide kernel on; At prior to 50 ~ 250 DEG C, drying 1 ~ 15 hour, then makes coating and carrier effectively combine for 1 ~ 9 hour 700 ~ 1000 DEG C of roastings, obtains lamellar composite carrier;
B) prepare mixing solutions I, comprise the soluble salt aqueous solution of II B compound of aequum, catalyst aid M and I A or II element A, wherein catalyst aid M is at least one in La, Nd, Lu, Eu, Ce, Yb, Tb or Ho; The platinichloride aqueous solution II of preparation aequum;
C) with pickling process by soluble salt load contained in solution I and II in composite catalyst carrier, flood after 12 ~ 48 hours, after drying, obtain catalyst precursor;
D) catalyst precursor was 450 ~ 650 DEG C of roastings 0.5 ~ 12 hour, and obtained dehydrogenating low-carbon alkane producing light olefins catalyzer with hydrogen reducing with steam dechlorination after 0.5 ~ 10 hour.
2. prepare the method for low-carbon alkene according to claim 1 for dehydrogenating low-carbon alkane, it is characterized in that temperature of reaction is 540 ~ 600 DEG C.
3. prepare the method for low-carbon alkene according to claim 1 for dehydrogenating low-carbon alkane, it is characterized in that reaction pressure is 0.05 ~ 0.35MPa.
4. prepare the method for low-carbon alkene according to claim 1 for dehydrogenating low-carbon alkane, it is characterized in that alkane mass space velocity is 0.5 ~ 5.6h -1.
5. prepare the method for low-carbon alkene according to claim 1 for dehydrogenating low-carbon alkane, it is characterized in that H 2/ C nh 2n+2volume ratio is 0.2 ~ 1.6.
6. prepare the method for low-carbon alkene according to claim 1 for dehydrogenating low-carbon alkane, it is characterized in that reaction raw materials is at least one in propane or Trimethylmethane.
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CN106607100B (en) * 2015-10-22 2019-04-12 中国石油化工股份有限公司 Dehydrogenating low-carbon alkane producing light olefins catalyst carrier and application thereof
CN110743611A (en) * 2019-10-31 2020-02-04 厦门大学 Nano composite catalyst, preparation method and application thereof
CN110743611B (en) * 2019-10-31 2021-01-01 厦门大学 Nano composite catalyst, preparation method and application thereof

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