CN109701531A - A kind of method of preparing isobutene through dehydrogenation of iso-butane - Google Patents
A kind of method of preparing isobutene through dehydrogenation of iso-butane Download PDFInfo
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Abstract
The invention discloses a kind of methods of preparing isobutene through dehydrogenation of iso-butane.It include: that iso-butane and catalyst carry out haptoreaction, the haptoreaction carries out in fixed bed reactors, fluidized-bed reactor or moving-burden bed reactor, and reactor inlet temperature is 400-650 DEG C, and the volume space velocity of the iso-butane is 300-2000h‑1, the catalytic pressure not more than 0.05MPa；The catalyst includes carrier and the active component being supported on carrier and auxiliary agent；The active component is platinum group metal, and it is in terms of 100% by overall catalyst weight, the content of the auxiliary agent is 0.001-30% that the auxiliary agent, which includes lanthanide series, alkali metal, tin and carbon,.Method of the invention can significantly improve iso-butane conversion ratio, selective isobutene river anti-carbon performance, have preferable prospects for commercial application.
Description
Technical field
The present invention relates to four technical fields of carbon, further say, are to be related to a kind of method of preparing isobutene through dehydrogenation of iso-butane.
Background technique
Isobutene is a kind of important Organic Chemicals, is widely used in polyisobutene, butyl rubber and methyl- tert fourth
The chemical products such as base ether.Wherein methyl tertiary butyl ether(MTBE), which can be used as, mentions high-octane additive, and the market demand is huge, causes different
Supply falls short of demand in butylene market.Isobutene is mainly derived from the catalytic cracking work of naphtha steam cracking ethylene and petroleum refining
Skill.In order to improve the conversion ratio of dehydrogenation of isobutane, higher reaction temperature is needed, and higher reaction temperature easily causes it
His side reaction causes reaction selectivity to reduce the inactivation for accelerating catalyst.
Dehydrogenation of isobutane has been realized in industrialization at present, existing technique mainly have Uop Inc. Oleflex technique,
Catofin technique and the Star technique of UHDE company of LUMMUS company etc..Currently, industrialized catalytic dehydrogenation of isobutane catalysis
Agent mainly has platinum group catalyst and chromium-based catalysts two major classes.Wherein, chromium-based catalysts inactivation is very fast, and to human health and ring
Border protection is unfavorable；And platinum group catalyst is because it is with high activity, low pollution, low wear rate, the spy that can be operated under severe conditions
It puts and becomes research hotspot.But platinum group catalyst tends to the surface carbon deposit because of catalytic active center in reaction atmosphere
And quickly reduce reactivity.Therefore, people generally require to add a series of help when using platinum as main active component
Agent, to improve iso-butane conversion ratio and selective isobutene.
Zhang et al. finds that (DOI:10.1016/S0167-2991 (08) 62627-0) tin is anti-in dehydrating alkanes compared with early
It is able to suppress the generation of platinum area carbon in answering, can preferably improve the stability of catalyst.
Wan et al. has found (DOI:10.1021/ie1023518), and the addition of lanthanum, which has platinum catalyst, to be promoted to make well
With.Suitable lanthanum can reduce the carbon deposition quantity of catalyst surface, improve the dispersion degree of platinum, but more lanthanum is also possible to cause
The reunion of platinum inactivates.
Zhang et al. discovery (DOI:10.1016/j.fuproc.2011.12.040) is added a small amount of zinc and can not only be mentioned
The dispersion degree of high platinum, and the generation of carbon distribution can also be reduced.The addition of zinc can effectively enhance tin auxiliary agent and between body
Interaction, therefore enhance the anti-reducing power of surface oxidation tin.
In conclusion during existing preparing isobutene through dehydrogenation of iso-butane, using platinum as the different of main active component
Butane dehydrogenation catalysts are main in the prior art or technological improvement is carried out using assistant types as breach, but simultaneously
Without fundamentally solving platinum group catalyst system inactivation, conversion ratio and the lower technical problem of selective isobutene.
Summary of the invention
During solving existing preparing isobutene through dehydrogenation of iso-butane, iso-butane conversion ratio and selective isobutene are lower
The technical issues of, the present invention provides a kind of methods of preparing isobutene through dehydrogenation of iso-butane.Higher iso-butane conversion can be obtained
Rate and selective isobutene.
The object of the present invention is to provide a kind of methods of preparing isobutene through dehydrogenation of iso-butane.
The described method includes:
Iso-butane and catalyst carry out haptoreaction, the haptoreaction fixed bed reactors, fluidized-bed reactor or
It is carried out in moving-burden bed reactor, reactor inlet temperature is 400-650 DEG C, and the volume space velocity of the iso-butane is 300-2000h-1, the catalytic pressure not more than 0.05MPa；
The catalyst includes carrier and the active component being supported on carrier and auxiliary agent；
The active component is platinum group metal, and the auxiliary agent includes lanthanide series, alkali metal, tin and carbon,
It is in terms of 100% by overall catalyst weight, the content of the auxiliary agent is 0.001-30%.
It is preferred that:
The haptoreaction carries out in fixed bed reactors, and reactor inlet temperature is 540-620 DEG C, the iso-butane
Volume space velocity be 500-1600h-1。
Wherein,
By overall catalyst weight be 100% in terms of,
The content of carrier is 69-99.9%；Preferably 82.5-99.6%；More preferably 89.2-98.4%；
The content of active component is 0.001-5%；Preferably 0.1-1%；More preferably 0.3-0.5%；
The content of lanthanide series metal is 0.001-15%；Preferably 0.01-10%；More preferably 0.1-5%；；
Alkali metal element content is 0.001-5%；Preferably 0.01-4%；More preferably 0.1-3%；
The content of tin is 0.001-5%；Preferably 0.1-4%；More preferably 1.0-2.0%；
The content of carbon is 0.001-1%；Preferably 0.01-0.5%；More preferably 0.1-0.3%.
The carrier is aluminium oxide, silica, zirconium dioxide, titanium dioxide, magnesia or zinc oxide；
The active component is at least one of ruthenium, rhodium, palladium, osmium, iridium and platinum；
The alkali metal is one of lithium, sodium, potassium, rubidium, caesium；
The lanthanide series is one of lanthanum, cerium, praseodymium, neodymium.
The catalyst is prepared by method comprising the following steps:
(1) it is obtained using infusion process in supported on carriers active component, lanthanide metal component, alkaline components and tin component
To catalyst precarsor I；
(2) the catalyst precarsor I is roasted in the mixed atmosphere of hydrocarbon and hydrogen, obtains catalyst precarsor II；
(3) the catalyst precarsor II is restored under hydrogen atmosphere, obtains catalyst.
It is preferred that:
Step (2), the hydrocarbon are methane or ethylene.
The ratio of step (2), hydrogen and hydrocarbon is 1:1-30；
Maturing temperature is 300-500 DEG C, calcining time 1-30min.
Following technical scheme specifically can be used in the present invention:
The present invention provides a kind of method of preparing isobutene through dehydrogenation of iso-butane, and this method includes by iso-butane and dehydrogenation
Carry out haptoreaction, wherein the catalyst includes carrier and the active component being supported on carrier and auxiliary agent, wherein institute
Stating carrier is aluminium oxide, and the active component is platinum group metal, and the auxiliary agent includes lanthanide series metal, alkali metal, tin and carbon, with institute
On the basis of the gross mass for stating catalyst, the mass content of the auxiliary agent is 0.001-30%.
According to the present invention, in order to further increase iso-butane conversion ratio and selective isobutene, with the total of the catalyst
On the basis of quality, the mass content of the carrier is 69-99.9%, preferably 82.5.5-99.7%, more preferably 89.2-
98.5%；The mass content of the active component is 0.001-5%, preferably 0.1-1%, more preferably 0.3-0.5%；It is described
The mass content of lanthanide series metal is 0.001-15%, preferably 0.01-10%, more preferably 0.1-5%；The alkali metal element
Content is 0.001-5%, preferably 0.01-4%, more preferably 0.1-3%；The mass content of the tin is 0.001-5%, excellent
It is selected as 0.1-4%, more preferably 1.0-2.0%；The mass content of the carbon be 0.001-1%, preferably 0.01-0.5%, more
Preferably 0.1-0.3%.
According to the present invention, the carrier is not particularly limited, the carrier that can be well known to those skilled in the art,
It such as can be aluminium oxide, silica, zirconium dioxide, titanium dioxide, magnesia, zinc oxide etc..Preferably, the carrier is
Aluminium oxide, more preferably gama-alumina.
In catalyst provided by the invention, the active constituent is not particularly limited, as long as having catalysis dehydrogenation
Activity, the active constituent that can be well known to those skilled in the art, such as can be platinum group metal, the platinum group metal
It can be selected from least one of ruthenium, rhodium, palladium, osmium, iridium and platinum, preferably platinum.
In catalyst provided by the invention, the lanthanide series metal is selected from least one of lanthanum and cerium, preferably lanthanum.
In catalyst provided by the invention, the alkali metal be selected from one of lithium, sodium, potassium, rubidium, caesium, preferably lithium,
Sodium, potassium.
There is no particular limitation for preparation method of the present invention to the catalyst, can use side commonly used in the art
Method, for example, can be infusion process, coprecipitation etc., preferably infusion process, in a kind of specific embodiment, the catalysis
The preparation method of agent may comprise steps of:
(1) it is obtained using infusion process in supported on carriers active component, lanthanide metal component, alkaline components and tin component
To catalyst precarsor I；
(2) the catalyst precarsor I is roasted in hydrocarbonaceous mixed atmosphere, obtains catalyst precarsor II；
(3) the catalyst precarsor II is restored under hydrogen atmosphere, obtains catalyst.
Wherein, use infusion process described in step (1) is in supported on carriers active component, lanthanide metal component and tin component
Process include:
(a) using the presoma of the infusion process presoma of load active component and lanthanide series metal on the carrier, then
It is dried and roasts；
(b) presoma of tin is loaded on the catalyst precarsor that step (a) obtains using infusion process, is then dried
And roasting, to obtain the catalyst precarsor I.
According to the present invention, in step (1), to the condition of dipping, there is no particular limitation, can be the routine of this field
Condition, such as 0.5-1h can be impregnated at room temperature.Wherein, the presoma of the active component is the acid containing active component
Or salt, preferably at least one of chloroplatinic acid, ammonium chloroplatinate and Tetrachloroplatinate ammonium, more preferably chloroplatinic acid；The group of the lanthanides
The presoma of metal is at least one of nitrate, chloride, carbonate and the acetate of the lanthanide series metal, preferably nitre
At least one of sour lanthanum, lanthanum chloride and lanthanum acetate, more preferably lanthanum nitrate；The precursor of the alkali metal is the alkali metal
One of nitrate, nitrite, chloride and acetate, preferably potassium nitrate, sodium nitrate, sodium carbonate, more preferably
Potassium nitrate；The presoma of the tin is stannous chloride or stannous sulfate, preferably stannous chloride, so that in the forerunner containing tin
In liquid solution, tin can be such that the dispersion degree of active component increases with the presence of its oxidation state, the tin of oxidation state, and it is de- to be conducive to catalyst
The improvement of hydrogen performance.
According to the present invention, in step (a) and step (b), the drying can adopt to be implemented with the conventional methods in the field,
Such as rotary evaporation seasoning；The roasting can also conventionally be implemented, and implementation condition may include: roasting temperature
Degree is 450-650 DEG C, and the time is 2-6 hours.
According to the present invention, in step (2), the catalyst precarsor I obtained by step (1) is needed in hydrocarbonaceous mixed atmosphere
In roasted, to load carbon on catalyst precarsor I, obtain catalyst precarsor II.The present invention is to the hydrocarbonaceous mixing
Atmosphere is not particularly limited, such as can be in H2And C2H4Mixed atmosphere under roasted；In addition, the present invention is to the roasting
The condition of burning is not particularly limited, such as can be H2And C2H4Volume ratio be 1:1-30, maturing temperature be 300-500 DEG C,
Calcining time is 1-30min.
According to the present invention, the haptoreaction that iso-butane and catalyst carry out can in reactor commonly used in the art into
It goes, such as can be carried out in fixed bed reactors, fluidized-bed reactor or moving-burden bed reactor, preferably fixed bed reaction
Device.In addition, since catalytic dehydrogenation of isobutane reaction is thermodynamically heat absorption and the increased reversible reaction of molecular number, conversion ratio
Depending on thermodynamical equilibrium, improves reaction temperature and reduction reaction pressure is conducive to reaction and carries out to dehydrogenation direction.But it is excessively high
Temperature can aggravate the deep dehydrogenation of iso-butane, cause reaction selectivity to reduce, while high temperature causes cracking reaction to be aggravated, accelerate
Catalyst surface carbon deposit, to accelerate the inactivation of catalyst.Therefore, the catalytic operating condition can be according to routine
Condition implement.In one embodiment, the haptoreaction carries out in fixed bed reactors, and reactor inlet temperature is
400-650 DEG C, preferably 540-620 DEG C；The volume space velocity of iso-butane is 300-3000h-1, preferably 500-2000h-1, described
Catalytic pressure not more than 0.05MPa.
In the present invention, the pressure is gauge pressure.
Dehydrogenation of isobutane catalyst is used in method of the invention, using platinum group metal as active component, with lanthanide series,
Tin, alkali metal and carbon are auxiliary agent.Iso-butane conversion ratio, selective isobutene river anti-carbon performance, therefore this can be significantly improved
The method of invention has preferable prospects for commercial application.
Specific embodiment
Below with reference to embodiment, the present invention is further illustrated.
Embodiment
The present embodiment is used to illustrate to prepare the catalyst of preparing isobutene through dehydrogenation of iso-butane provided by the invention.
Preparation: in the lanthanum nitrate hexahydrate that 60g gama-alumina (Shandong Aluminum Co., Ltd.) is impregnated in 0.15mol/L at 75 DEG C,
At 75 DEG C after the dry 0.5h of rotary evaporation.Put into chloroplatinic acid (Sinopharm Chemical Reagent Co., Ltd.), potassium nitrate and
It is dry through rotary evaporation at 75 DEG C in stannous chloride (fine chemistry industry research institute is recovered in Tianjin) aqueous solution of 0.3mol/L
After 0.5h, material is placed into Muffle furnace, roasts 3h in 450 DEG C of air atmosphere, obtains catalyst precarsor I.It is wherein molten
Liquid product measures the catalyst precarsor I that will be obtained according to the mass content of catalytic component.Catalyst precarsor I is taken out, is set
In tube furnace, in H2And C2H415min is roasted in the mixed atmosphere that volume ratio is 1:1, maturing temperature is 500 DEG C, is catalyzed
Agent precursor II.Finally, by catalyst precarsor II, hydrogen reducing 1h obtains catalyst 1 at 580 DEG C, consisting of Pt-Sn-La-
C/Al2O3。
The preparation method of catalyst 2-5 is similar with catalyst 1, and the ratio of added catalyst activity component is different,
Based on the gross mass of catalyst, the mass content of each component is as shown in table 1 in catalyst.
Comparative example
Preparation: in the lanthanum nitrate hexahydrate that 60g gama-alumina (Shandong Aluminum Co., Ltd.) is impregnated in 0.15mol/L at 75 DEG C,
At 75 DEG C after the dry 0.5h of rotary evaporation.Put into chloroplatinic acid (Sinopharm Chemical Reagent Co., Ltd.), potassium nitrate and
It is dry through rotary evaporation at 75 DEG C in stannous chloride (fine chemistry industry research institute is recovered in Tianjin) aqueous solution of 0.3mol/L
After 0.5h, material is placed into Muffle furnace, roasts 3h in 450 DEG C of air atmosphere, obtains catalyst precarsor I.It is wherein molten
Liquid product measures the catalyst precarsor I that will be obtained according to the mass content of catalytic component.By catalyst precarsor I at 580 DEG C
Hydrogen reducing 1h obtains catalyst 6, consisting of Pt-Sn-La/Al2O3。
The added catalyst activity component of catalyst 6-10 is based on the gross mass of catalyst, each component in catalyst
Mass content it is identical as catalyst 1-5 respectively.
Dehydrogenation of isobutane experiment is completed on a fixed bed, wherein catalyst filling volume 30ml, iso-butane volume space velocity 500
~2000h-1, reaction pressure is normal pressure, and reactor inlet temperature is 540~620 DEG C, and dehydrogenation of isobutane product uses HP7890 gas
Phase chromatography is analyzed, and experimental period reaches the experimental results of 3 hours, and see Table 1 for details.
Table 1
Table 2
Above-described embodiment 1-5 is compared with comparative example 1-5 as can be seen that in the mistake for preparing isobutene by dehydrogenation of isobutane
It is different to can be improved dehydrogenation of isobutane system by introducing auxiliary agent lanthanide series metal, alkali metal, tin and carbon in dehydrogenation by Cheng Zhong
Iso-butane conversion ratio and selective isobutene during butylene.
Claims (9)
1. a kind of method of preparing isobutene through dehydrogenation of iso-butane, it is characterised in that the described method includes:
Iso-butane and catalyst carry out haptoreaction, and the haptoreaction is in fixed bed reactors, fluidized-bed reactor or movement
It is carried out in bed reactor, reactor inlet temperature is 400-650 DEG C, and the volume space velocity of the iso-butane is 300-2000h-1, institute
State catalytic pressure not more than 0.05MPa；
The catalyst includes carrier and the active component being supported on carrier and auxiliary agent；
The active component is platinum group metal, and the auxiliary agent includes lanthanide series, alkali metal, tin and carbon,
It is in terms of 100% by overall catalyst weight, the content of the auxiliary agent is 0.001-30%.
2. the method for preparing isobutene through dehydrogenation of iso-butane as described in claim 1, it is characterised in that:
The haptoreaction carries out in fixed bed reactors, and reactor inlet temperature is 540-620 DEG C, the body of the iso-butane
Product air speed is 500-1600h-1。
3. the method for preparing isobutene through dehydrogenation of iso-butane as described in claim 1, it is characterised in that:
By overall catalyst weight be 100% in terms of,
The content of carrier is 69-99.9%；
The content of active component is 0.001-5%；
The content of lanthanide series metal is 0.001-15%；
Alkali metal element content is 0.001-5%；
The content of tin is 0.001-5%；
The content of carbon is 0.001-1%.
4. the method for preparing isobutene through dehydrogenation of iso-butane as claimed in claim 3, it is characterised in that:
By overall catalyst weight be 100% in terms of,
The content of the carrier is 82.5-99.6%；
The content of active component is 0.1-1%；
The content of lanthanide series metal is 0.01-10%；
Alkali metal element content is 0.01-4%；
The content of tin is 0.1-4%；
The content of carbon is 0.01-0.5%.
5. the method for preparing isobutene through dehydrogenation of iso-butane as claimed in claim 4, it is characterised in that:
By overall catalyst weight be 100% in terms of,
The content of carrier is 89.2-98.4%；
The content of active component is 0.3-0.5%；
The content of lanthanide series metal is 0.1-5%；
Alkali metal element content is 0.1-3%；
The content of tin is 1.0-2.0%；
The content of carbon is 0.1-0.3%.
6. the method for preparing isobutene through dehydrogenation of iso-butane as described in claim 1, it is characterised in that:
The carrier is aluminium oxide, silica, zirconium dioxide, titanium dioxide, magnesia or zinc oxide；
The active component is at least one of ruthenium, rhodium, palladium, osmium, iridium and platinum；
The alkali metal is one of lithium, sodium, potassium, rubidium, caesium；
The lanthanide series is one of lanthanum, cerium, praseodymium, neodymium.
7. the method for preparing isobutene through dehydrogenation of iso-butane as described in claim 1, it is characterised in that:
The catalyst is prepared by method comprising the following steps:
(1) it is urged using infusion process in supported on carriers active component, lanthanide metal component, alkaline components and tin component
Agent precursor I；
(2) the catalyst precarsor I is roasted in the mixed atmosphere of hydrocarbon and hydrogen, obtains catalyst precarsor II；
(3) the catalyst precarsor II is restored under hydrogen atmosphere, obtains catalyst.
8. the method for preparing isobutene through dehydrogenation of iso-butane as claimed in claim 7, it is characterised in that:
Step (2), the hydrocarbon are methane or ethylene.
9. the method for preparing isobutene through dehydrogenation of iso-butane as claimed in claim 8, it is characterised in that:
The ratio of step (2), hydrogen and hydrocarbon is 1:1-30；
Maturing temperature is 300-500 DEG C, calcining time 1-30min.
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Cited By (1)
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| CN110841726A (en) * | 2019-12-02 | 2020-02-28 | 西安凯立新材料股份有限公司 | Regeneration method of catalyst for isobutane dehydrogenation |
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