CN106478351B - The method of iso-butane and/or dehydrogenating propane - Google Patents
The method of iso-butane and/or dehydrogenating propane Download PDFInfo
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- CN106478351B CN106478351B CN201510541835.2A CN201510541835A CN106478351B CN 106478351 B CN106478351 B CN 106478351B CN 201510541835 A CN201510541835 A CN 201510541835A CN 106478351 B CN106478351 B CN 106478351B
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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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Abstract
The present invention relates to a kind of methods of iso-butane and/or dehydrogenating propane, mainly solve existing iso-butane and/or dehydrogenating propane preparing isobutene and/or production of propylene is difficult to the technical problem for operating, steadily producing.The present invention uses fixed bed reactors, by using reactor include reaction raw materials feed inlet (1), catalyst regeneration gas feed inlet (2), reactor blow valve port (3), reduction/evacuation entrance (4), reacting product outlet (5), catalyst regeneration waste gas outlet (6), purge gass/evacuation waste gas outlet (7) technical solution, by the way that timing switching valve A~G is respectively set and switches in each feed inlet or outlet, complete raw material reaction, inside reactor purging, catalyst regeneration, reactor restores/evacuate process, the production of iso-butane and/or dehydrogenating propane preparing isobutene and/or propylene is completed using the switching of at least four reactor.
Description
Technical field
The present invention relates to a kind of methods of iso-butane and/or dehydrogenating propane, steadily carry out using at least four reactors
The production of iso-butane and/or dehydrogenating propane preparing isobutene and/or propylene.
Background technique
Reaction refers in petrochemical production process, converts industry for the raw material such as petroleum, natural gas, coal
And target product needed for human lives, main production equipments are reactor.The equipment that reactor realizes reaction process, extensively
Applied to industrial departments such as chemical industry, oil refining, metallurgy, light industrys.Solid for realizing single liquid phase reaction process and liquid liquid, gas-liquid, liquid,
The heterogeneous reaction process such as gas-liquid-solid.Reactor occupies an important position in process industrial production.With regard to full-range construction investment and
For operating cost, ratio shared by reactor may not be very big.But its performance and the superiority and inferiority of operation affect front and back processing and
The yield and quality of product also has an important influence on consumption of raw materials, energy consumption and product cost.For specifically reacting
Journey, the type selecting of reactor need to comprehensively consider the factor of the aspects such as technology, economy and safety.
The essential characteristic of reaction process determines suitable reactor types.Such as gas-solid phase reaction process is generally with solid
Fixed bed reactor, fluidized-bed reactor or moving-burden bed reactor.But suitable type selecting then needs the fuel factor of consideration reaction, to anti-
It answers many factors such as requirement, catalyst physical chemistry condition and the inactivation of conversion ratio and selection rate, or even needs to different anti-
It answers device to make conceptual design respectively, just can determine that after technology and economic analysis.
Nowadays the worker of academia and industry is directed to different objects by various methods, successfully develops a variety of tools
The reactor of characteristic reaction process.Such as the synthesis of fluidized catalytic cracking commercial plant, fluidized bed acrylonitrile, fixed bed radial direction
And the catalytic reactor of the diversified forms such as the ammonia synthesis of axis radial direction, ethyl benzene dehydrogenation preparation of styrene, methanol-fueled CLC, butylene oxidation-dehydrogenation,
In fact the design of reactor must and specific raw material route, production method, flow setting, production scale and raw material composition,
The operating conditions such as conversion ratio, selectivity are closely related, and the structure model selection and operating condition of reactor must be based on chemical technologies.
After reactor type selecting determines, there is corresponding suitable production method.
Isobutene/propylene is important Organic Chemicals.Isobutene is mainly for the preparation of methyl tertiary butyl ether(MTBE), butyl rubber
Glue, isoprene rubber, polyisobutene.In addition, it can also be used to synthesizing methylmethacrylate, isoprene etc..In traditional handicraft,
The main source of isobutene is the by-product C 4 fraction of naphtha steam cracking ethylene unit, refinery's fluidized catalytic cracker
The by-product tert-butyl alcohol in by-product C 4 fraction and the synthesis of Halcon method propylene oxide.With the exploitation benefit of isobutene downstream product
With the contradiction of global isobutene inadequate resource becomes increasingly conspicuous.Propylene is equally used as important Organic Chemicals, in addition to production
Outside polypropylene, the important source material of the products such as also a large amount of production acrylonitrile, butanol, ethylene oxide, isopropylbenzene.Dehydrogenation of isobutane system
Isobutene has similar reaction principle with preparing propylene by dehydrogenating propane, and used catalyst is also similar, is nowadays faced with alkene
Cracking leads to the problem of the production capacity deficiency of propylene and isobutene, and the De-hydrogen Technology by dehydrating alkanes production isobutene is more important.
Propylene is the base stock of three big synthetic materials, mainly for the production of polypropylene, acrylonitrile, isopropyl alkene, acetone and
Propylene oxide etc..To produce a variety of important Organic Chemicals, generate synthetic resin, synthetic rubber and a variety of fine chemicals
Deng.Its representative production technology mainly has three kinds of steam cracking method, catalytic cracking method and propane (butane) dehydriding etc.
Type.Data is shown according to the relevent statistics, and there are about 60% propylene to come from ethylene vapor cracker at present in the whole world, and 35% or so comes
From oil plant (mainly catalytic cracking unit), account for about 5% from other techniques such as dehydrogenating propanes.Wherein, catalytic cracking method
The propylene of production accounts for about 90% or more of the produced propylene in oil refining enterprise.
The largest source of propylene is 15% propylene of ethylene plant by-product, provides about 70% petrochemical material propylene.Third
The second largest source of alkene is fluidized catalytic cracker (FCCU), provides about 28% propylene demand in addition, there are also a small amount of
Propylene comes from dehydrogenating propane, this is only limitted to the resourceful area of lighter hydrocarbons, is difficult to realize in gas price weakness and third in China
Under the situation of alkene demand growth, for oil plant, increase effective way that crude propylene yield is raising refinery's benefit
Diameter
Most during the nearly last ten years, dehydrogenating propane becomes the important process process of industrialization production of propylene, however, it is promoted and applied
It is somewhat prohibitive because propane is worth due to higher, technical process investment is larger.But propylene demand growth and propylene value improve
And process is improved, and dehydrogenating propane is caused to become effective propylene enhancing technique, which produces propane and short propylene to rich
Area is especially useful.The speedup of propylene demand be higher than gasoline and ethylene demand speedup, for this purpose, conventional propylene supply and demand it
Between difference will be made up by dehydrogenating propane.Nexant chemical system company points out, over first 20 years, propylene demand speedup is higher than second
Alkene, in the U.S., the ratio between propylene demand/ethylene requirements were increased to 2003 0.6 by 1980 0.48, and some other area is as in
East, West Europe and East Asia are also similarly.
The by-product of oil plant is mainly made of C3-C6 alkane, these by-products are used as always the fuel of low value to make
With chemical utilization rate is low.Propane/dehydrogenation of isobutane can produce more propylene and isobutene than hydrocarbon vapours cracking technique.Example
Such as when steam cracking technology produces propylene, propene yield at most only has 33%, and produces propylene with dehydrogenating propane technology, total to receive
Rate is up to 74%-86%.Single raw material produces single product, and the equipment investment of dehydrogenating propane technology is than hydrocarbon vapours cracking technique
Low 33%, and liquefied petroleum gas resource can be efficiently used and be allowed to be converted into useful alkene.
The technology of advanced and mature propane catalytic dehydrogenation production propylene has the Oleflex of Uop Inc. of the U.S. in the world at present
The Catofin technique of technique and Lummus company of the U.S. both have passed through technological development and the engineer application of many years, have height
The reliability of degree.The general process of two kinds of techniques is similar, and the main distinction is what the Catofin technique of propane catalytic dehydrogenation used
It is chromium-based catalysts, stability is poor, and has toxicity.And Oleflex technique is using platinum group catalyst, it is more stable to heat,
There is no toxicity.Compared with other production technologies, Oleflex technique has less reactor, less loaded catalyst
And occupied area, and more importantly Oleflex uses chromium-free catalyst, avoids the pollution problem of failure chrome catalysts.
But platinum series catalyst regeneration cycle is long, but its selectivity is low with yield；Chrome catalysts series of regeneration cycles is short, but selects
Property and yield it is all relatively high, and platinum series Catalytic processes generally use moving-burden bed reactor, and chrome catalysts series is using fixing
Bed reactor.But for relatively primary investment, platinum series catalyst investment is big, and reaction pressure is higher.It is circulating fixed bed anti-
Reactor uses chromium class non-precious metal catalyst, low to the requirement of raw material impurity, cheap, without to agent in use process
Loss.High conversion per pass and high catalyst reduce operating pressure and temperature, hydrogen-free circulation, no steaming in reaction
Vapour dilution, can effectively reduce energy consumption and operating cost.
Summary of the invention
To be solved by this invention is the problem of implementation of iso-butane and/or dehydrogenating propane preparing isobutene and/or propylene reaction
And the technical issues of existing operating difficulties, steady production, by using the side of a kind of new iso-butane and/or dehydrogenating propane
Method can solve above-mentioned technical problem, and with industrial production operation, simple, device runs smoothly, reduces operation pressure,
The advantages that improving the conversion ratio and target product yield of reaction.
In order to solve the above-mentioned technical problem, The technical solution adopted by the invention is as follows: a kind of iso-butane and/or dehydrogenating propane
Method, blown using fixed bed reactors, including reaction raw materials feed inlet (1), catalyst regeneration gas feed inlet (2), reactor
It is useless to sweep mouth (3), reduction/evacuation entrance (4), reacting product outlet (5), catalyst regeneration waste gas outlet (6), purge gass/evacuation
Gas exports (7)；By the way that timing switching valve A~G is respectively set and switches in each feed inlet or outlet, the reaction of completion raw material,
Inside reactor purging, catalyst regeneration, reactor restore/process is evacuated, utilize the switching of at least four reactor to complete life
It produces.
In above-mentioned technical proposal, it is preferable that fixed bed reactors are horizontal type structure；
In above-mentioned technical proposal, it is preferable that reactor also includes feed distributor (9)；It is highly preferred that feed distributor
(9) upper wall in reactor is hung on；
Preferably, reactor also includes catalyst support plate (10)；
Preferably, reaction raw materials feed inlet (1), catalyst regeneration gas feed inlet (2), reactor blow valve port (3), reduction/
Entrance (4) are evacuated to be connected by the combined feed mouth (11) of reactor head with reactor；
Preferably, the first outlet that reacting product outlet (5), catalyst regeneration waste gas outlet (6) pass through reactor bottom
(12) it is connected with reactor；
Preferably, second outlet (13) and reactor phase that purge gass/evacuation waste gas outlet (7) passes through reactor bottom
Even；
Preferably, reaction raw materials feed inlet (1), catalyst regeneration gas feed inlet (2), reactor blow valve port (3), reduction/
Evacuate entrance (4), reacting product outlet (5), catalyst regeneration waste gas outlet (6), purge gass/evacuation waste gas outlet (7) respectively
Timing switching valve A, B, C, D, E, F and G are set；
Preferably, raw material reaction, inside reactor purging, catalyst regeneration, reactor restore/evacuate process successively into
Row；
In above-mentioned technical proposal, it is preferable that complete production using the switching of at least six reactor；It is highly preferred that using extremely
Production is completed in the switching of few 8 reactors.
In above-mentioned technical proposal, horizontal reactor is thinner its object is to make catalytic bed, and reaction pressure drop is small.It is logical
It crosses welding manner and distributor is hung on into upper wall in reactor, so that raw material, purge gass, regeneration gas etc. are equal by feed distributor
It is even catalyst bed occur dehydrogenation reaction, purging catalyst bed impurity and regeneration gas cmpletely to catalyst again
It is raw.In present invention design, only one mouth (11) of top feed mouth, relevant material charging, the interior purging of reactor, reduction/pumping
The feed steps such as sky all pass through this mouthful progress, the advantage is that the risk for effectively reducing and being open elsewhere in reactor.?
In design, outlet at bottom is arranged two discharge ports (12) and (13) and carries out the switching of production process by timing control, several
Orderly switching between reactor ensure that the continuity of production.It is related simultaneously in this design for the same reactor
Catalyst regeneration, purging, reduction/evacuation processing step all pass through timing control valve in the same inside reactor in reactor
It completes.With this condition, using chromium-based catalysts, it ensure that whole system has high conversion ratio and low recirculation rate, thus
Reduce energy consumption and operating cost.In above-mentioned reaction process, reaction pressure is preferably negative pressure 40-100KPa；Reaction temperature is preferred
It is 300-600 DEG C, more preferably 400-600 DEG C；Catalyst is preferably chromium system or platinum group catalyst.
In above-mentioned technical proposal, it is preferable that catalyst based on parts by weight, including following components:
A) 0.1~5 part of Pt or its oxide；
B) 0.2~4 part of Sn or its oxide；
C) 0.1~5 part of alkali metal or its oxide；
D) 0.2~3 part Ga, In, Tl, Cr, Mn or its oxide；
E) 0.1~10 part of Ce-La-O solid solution；
F) 80~99 parts of Al2O3。
A kind of method of iso-butane and/or dehydrogenating propane preparing isobutene and/or propylene proposed by the present invention, outstanding advantages
It is: according to iso-butane and/or the reality of dehydrogenating propane reaction process, has carried out uniqueness in the material entrance setting of reactor
Design, import only one, export two, effectively reduce production risk.Production process controls reactor list using time control valve
One entrance carries out dehydrogenation reaction, catalyst regeneration, purging, reduction/evacuation technique ring in reactor in same reactor
Section, by preferred catalyst, while at least four parallel reactor designed carry out timing switching complete entire iso-butane and/or
The undisturbed of dehydrogenating propane preparing isobutene and/or propylene steadily produces, and has high conversion and low recycling when specific operation
Rate effectively reduces system energy consumption and operating cost without Steam dilution during system carries out.
Detailed description of the invention
Fig. 1 is the structure of reactor schematic diagram of the present invention produced for iso-butane and/or dehydrogenating propane.
Fig. 2 is the time control valve connection schematic diagram connecting in Fig. 1 with 8 reactors of the invention.
Fig. 3 is the timing control schematic diagram based on the present invention when 8 parallel reactors work.
Fig. 4 is the time control valve connection schematic diagram connecting in Fig. 1 with 6 reactors of the invention.
Fig. 5 is the timing control schematic diagram based on the present invention when 6 parallel reactors work.
In Fig. 1: 1 be reaction raw materials feed inlet, 2 be catalyst regeneration gas feed inlet, 3 for reactor purge, 4 for reduction/
Entrance is evacuated, 5 be reacting product outlet, and 6 be catalyst regeneration waste gas outlet, and 7 be purge gass/evacuation waste gas outlet, and 8 be catalysis
Agent bed, 9 be feed distributor, and 10 be catalyst support plate, and 11 be reactor head combined feed mouth, and 12,13 be reactor bottom
The first outlet and second outlet in portion.
In Fig. 2: 1-8 is respectively eight iso-butanes and/or dehydrogenating propane reactor in parallel for illustrating of the invention, respectively
First reactor, second reactor, third reactor, the 4th reactor, the 5th reactor, the 6th reactor, the 7th reactor
With the 8th reactor, A~G be respectively with 1~7 time control valve that is correspondingly connected with of feed inlet or outlet in Fig. 1, and respectively with it is low
Pressure purge vapor, reduction/evacuation, regeneration, feedstock are connected.
Go into operation, regenerate in Fig. 3, evacuating, the time of purging it is given according to specific catalyst, in timing diagram different colours and
Mark respectively indicates that meaning is as follows, and 1-8 respectively indicates the timing position of corresponding reactor.
Fig. 4 has similar definition with Fig. 2.
Fig. 5 has similar definition with Fig. 3.
Specific embodiment
[embodiment 1]
Reaction is that preparing isobutene through dehydrogenation of iso-butane reacts, and completes dehydrogenation of isobutane production process using 8 reactors.
The unstripped gas iso-butane that temperature is 400 degree or so is heated to 600 degree or so by feed heater, by unstripped gas
Timing control valve A and reaction raw materials feed inlet (1) enter first reactor, and feed distributor (9) enters isobutyl in reacted device
Alkane dehydrogenation bed (8) carries out dehydrogenation reaction and generates isobutene, and it is negative pressure 40Kpa that pressure is kept in reactor；It has reacted
Cheng Hou, under the conditions of system vacuum, chronologically control figure 3 enters reactor blow valve port (3) through control valve C with steam and thoroughly purges
Reactor sweeps off the remaining hydrocarbon in reactor；Catalyst in reactor is carried out again according to timing control timing shown in Fig. 3
Raw, regeneration air enters reactor through catalyst regeneration gas feed inlet (2) by timing control valve B, and the purpose is to remove catalysis
Coking in agent and the operation temperature that bed body is returned to；After the completion of regeneration, using reduction/evacuation entrance (4) and
Control valve D is switched to evacuated state, into next operation cycle.Other 7 reactors are successively complete according to timing control valve
At the operation circulation of first reactor is pressed, produced to form some reactors, and other reactor catalysts regenerate, other
Some reactors evacuated, the processes such as steam blowing, production efficiency so can be improved, complete the steady of entire isobutene
Production.
[embodiment 2]
Reaction is that preparing propylene by dehydrogenating propane reacts, and completes dehydrogenating propane production process using 6 reactors.
The unstripped gas propane that temperature is 450 degree or so is heated to 580 degree or so by feed heater, when by unstripped gas
Sequence control valve A and reaction raw materials feed inlet (1) enter first reactor, and feed distributor (9) is de- into propane in reacted device
Hydrogen catalyst bed (8) carries out dehydrogenation reaction and generates propylene, and it is negative pressure 60Kpa that pressure is kept in reactor；After the reaction was completed, exist
Under the conditions of system vacuum, chronologically control figure 5 enters reactor blow valve port (3) thorough purge through control valve C with steam,
Sweep off the remaining hydrocarbon in reactor；The regeneration of catalyst in reactor, regeneration are carried out according to timing control timing shown in fig. 5
Air enters reactor through catalyst regeneration gas feed inlet (2) by timing control valve B, and the purpose is to remove the knot in catalyst
Operation temperature burnt and that bed body is returned to；After the completion of regeneration, cut using reduction/evacuation entrance (4) and control valve D
Evacuated state is changed to, into next operation cycle.Other 5 reactors are successively completed according to timing control valve anti-by first
The operation circulation of device is answered, so that some reactor productions are formed, and other reactor catalysts regenerate, other some reactions
The processes such as device evacuated, steam blowing, so can be improved production efficiency, complete the steady production of entire propylene.
[embodiment 3]
Reaction is that preparing isobutene through dehydrogenation of iso-butane reacts, and completes dehydrogenation of isobutane production process using 8 reactors.By reality
The process flow of example 1 is applied, wherein the catalyst selected is 0.6%Pt1.0%Sn1.0%K0.4%Ga0.5%
Ce0.8La0.2O2-δ/Al2O3, complete the steady production of entire isobutene.
[embodiment 4]
Reaction is that preparing propylene by dehydrogenating propane reacts, and completes dehydrogenating propane production process using 10 reactors.By embodiment 1
Process flow, wherein the catalyst selected be 4%Pt0.3%Sn3%Na2%In8%Ce0.8La0.2O2-δ/Al2O3, complete whole
The steady production of a isobutene.
[comparative example 1]
Reaction is that preparing isobutene through dehydrogenation of iso-butane reacts, and completes dehydrogenation of isobutane production process using 4 reactors.
The unstripped gas iso-butane that temperature is 400 degree or so is heated to 600 degree or so by feed heater, by unstripped gas
Timing control valve A and reaction raw materials feed inlet (1) enter first reactor, and feed distributor (9) enters isobutyl in reacted device
Alkane dehydrogenation bed (8) carries out dehydrogenation reaction and generates isobutene, and it is negative pressure 40Kpa that pressure is kept in reactor；It has reacted
Cheng Hou, under the conditions of system vacuum, chronologically control figure 3 enters reactor blow valve port (3) through control valve C with steam and thoroughly purges
Reactor sweeps off the remaining hydrocarbon in reactor；Catalyst in reactor is carried out again according to timing control timing shown in Fig. 3
Raw, regeneration air enters reactor through catalyst regeneration gas feed inlet (2) by timing control valve B, and the purpose is to remove catalysis
Coking in agent and the operation temperature that bed body is returned to；After the completion of regeneration, using reduction/evacuation entrance (4) and
Control valve D is switched to evacuated state, into next operation cycle.Other 3 reactors are successively complete according to timing control valve
At the operation circulation of first reactor is pressed, produced to form some reactors, and other reactor catalysts regenerate, other
Some reactors evacuated, the processes such as steam blowing, entire isobutene production is unstable.
Claims (10)
1. a kind of method of iso-butane and/or dehydrogenating propane, using fixed bed reactors, including reaction raw materials feed inlet (1), urge
Agent regeneration gas feed inlet (2), reactor blow valve port (3), reduction/evacuation entrance (4), reacting product outlet (5), catalyst are again
Raw waste gas outlet (6), purge gass/evacuation waste gas outlet (7)；By the way that timing switching valve is respectively set in each feed inlet or outlet
A~G is switched over, and completes raw material reaction, inside reactor purging, catalyst regeneration, reactor restore/evacuate process, utilization
Production is completed in the switching of at least four reactor, wherein dehydrogenation reaction, catalyst regeneration, reactor are carried out in same reactor
Interior purging, reduction/evacuation process procedure, dehydrogenation reaction pressure are negative pressure 40-100KPa, and reaction temperature is 300-600 DEG C, catalysis
Agent is chromium system or platinum group catalyst.
2. the method for iso-butane according to claim 1 and/or dehydrogenating propane, it is characterised in that fixed bed reactors are sleeping
Formula structure.
3. the method for iso-butane according to claim 1 and/or dehydrogenating propane, it is characterised in that reactor also includes charging
Distributor (9).
4. the method for iso-butane according to claim 1 and/or dehydrogenating propane, it is characterised in that reactor also includes catalysis
Agent support plate (10).
5. the method for iso-butane according to claim 1 and/or dehydrogenating propane, it is characterised in that reaction raw materials feed inlet
(1), catalyst regeneration gas feed inlet (2), reactor blow valve port (3), reduction/evacuation entrance (4) are total by reactor head
Feed inlet (11) is connected with reactor.
6. the method for iso-butane according to claim 1 and/or dehydrogenating propane, it is characterised in that reacting product outlet (5),
Catalyst regeneration waste gas outlet (6) is connected by the first outlet (12) of reactor bottom with reactor.
7. the method for iso-butane according to claim 1 and/or dehydrogenating propane, it is characterised in that purge gass/evacuation exhaust gas
Outlet (7) is connected by the second outlet (13) of reactor bottom with reactor.
8. the method for iso-butane according to claim 1 and/or dehydrogenating propane, it is characterised in that in reaction raw materials feed inlet
(1), catalyst regeneration gas feed inlet (2), reactor blow valve port (3), reduction/evacuation entrance (4), reacting product outlet (5), urge
Timing switching valve A, B, C, D, E, F and G is respectively set in agent regeneration off gases outlet (6), purge gass/evacuation waste gas outlet (7).
9. the method for iso-butane and/or dehydrogenating propane according to claim 1 or 8, it is characterised in that raw material reaction, reaction
Device internal sweep, catalyst regeneration, reactor restore/evacuate process and successively carry out.
10. the method for iso-butane according to claim 1 and/or dehydrogenating propane, it is characterised in that catalyst is with parts by weight
Number meter, including following components:
A) 0.1~5 part of Pt or its oxide；
B) 0.2~4 part of Sn or its oxide；
C) 0.1~5 part of alkali metal or its oxide；
D) 0.2~3 part Ga, In, Tl, Cr, Mn or its oxide；
E) 0.1~10 part of Ce-La-O solid solution；
F) 80~99 parts of Al2O3。
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