CN108654526A - A kind of reactor and preparation method of the dehydrating alkanes alkene reducing back-mixing - Google Patents
A kind of reactor and preparation method of the dehydrating alkanes alkene reducing back-mixing Download PDFInfo
- Publication number
- CN108654526A CN108654526A CN201710213552.4A CN201710213552A CN108654526A CN 108654526 A CN108654526 A CN 108654526A CN 201710213552 A CN201710213552 A CN 201710213552A CN 108654526 A CN108654526 A CN 108654526A
- Authority
- CN
- China
- Prior art keywords
- catalyst
- conversion zone
- section
- reactor
- riser
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1809—Controlling processes
-
- 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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
- B01J8/004—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor by means of a nozzle
-
- 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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1845—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised
- B01J8/1863—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised followed by a downward movement outside the reactor and subsequently re-entering it
-
- 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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
-
- 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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/38—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
- B01J8/384—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only
- B01J8/388—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only externally, i.e. the particles leaving the vessel and subsequently re-entering it
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
- C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
- C07C5/333—Catalytic processes
- C07C5/3332—Catalytic processes with metal oxides or metal sulfides
-
- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
-
- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00548—Flow
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
A kind of reaction unit of alkane catalytic dehydrogenation, including conversion zone and reactor settling section, reactor settling section is located at the top of conversion zone, the diameter of the conversion zone tapers into from top to bottom, catalyst regeneration inclined tube stretches into conversion zone, and the outlet end of catalyst regeneration inclined tube is located at the lower part of conversion zone, feed distribution mechanism is located at the lower section of the outlet end of the catalyst regeneration inclined tube in conversion zone.Reactant and catalyst cocurrent flow up in reactor, can effectively improve the uniformity of reactor temperature distribution, localized hyperthermia be avoided, to reduce thermal response；And reactor is along the gradual undergauge of fluid flow direction, the secondary conversion of alkene caused by reducing back-mixing, to improve the yield and selectivity of alkene.High temperature regeneration agent is injected directly into reactor dense bed bottom, high temperature catalyst is not only contributed to mix with the quick of catalyst in reactor, it avoids forming localized hyperthermia in bed, and the catalyst of dense fluidized also helps the transmission for terminating free radical, to reduce thermal response, the selectivity of dehydrating alkanes alkene is improved.
Description
Technical field
The present invention relates to a kind of circulating fluid bed reactors, specifically, being related to a kind of the anti-of recirculating fluidized bed dehydrating alkanes
Device is answered, more particularly to a kind of dehydrating alkanes reaction unit reducing back-mixing.
Background technology
Alkene and alkadienes (ethylene, propylene, butylene, isobutene, isoprene and butadiene etc.) are in synthetic resin, modeling
Material, high-knock rating gasoline blend component (methyl tertiary butyl ether(MTBE), tert amyl methyl ether(TAME) and alkylate oil) and the production of other high added values
It is widely used in terms of product.These alkene except through hydrocarbon steam cracking (such as ethane steam cracking, naphtha steam cracking), alkene
The catalytic pyrolysis (such as Superflex technologies) of hydrocarbon, the catalytic pyrolysis (such as TMP, DCC technology) of heavy oil and heavy-oil catalytic pyrolysis are (such as
CPP technologies) etc. processes production it is outer, alkane catalytic dehydrogenation is also the important technology route of alkene and alkadienes production.
Dehydrating alkanes utilize the important way enriched low-carbon alkanes resource, prepare high added value low-carbon alkene as reasonable
Diameter is increasingly subject to the attention of people.
The dehydrogenation of alkane is the stronger endothermic reaction, such as propane and dehydrogenation of isobutane,
C3H8→C3H6+H2ΔHo=124.3kJ/mol
i-C4H10→i-C4H8+H2ΔHo=117.6kJ/mol
It is up to 124.3 and 117.6kJ/mol respectively in 0.1MPa, 25 DEG C of reaction heat.It either uses what type of
How reactor effectively gives reaction heat supply, is all the problem of must pondering deeply.
The dehydrogenation reaction of alkane is limited by thermodynamical equilibrium.Under identical temperature condition, the molecule of alkane is bigger, balance
Conversion ratio is higher；For same alkane, temperature is higher, and equilibrium conversion is higher.Ethane dehydrogenation to ethene, if using catalysis
The method of dehydrogenation, is limited by thermodynamical equilibrium, and conversion per pass is too low, thus, ethane dehydrogenation is using steam heat at present
The technology of solution, reaction carry out under 800 DEG C or more of hot conditions.The catalytic dehydrogenation of propane, butane etc., in suitable temperature strip
Economically acceptable conversion per pass and olefine selective can be obtained under part, thus, preparing propylene by dehydrogenating propane, butane dehydrogenation system
Butylene or butadiene, generally use be catalytic dehydrogenation method.
Oxidative dehydrogenation, though can break thermodynamical equilibrium limitation, greatly improves alkane and turns as another path of dehydrating alkanes
Rate reduces coking yield, but since the introducing of oxygen species, deep oxidation reaction are difficult to control, generates a large amount of COx and H2O,
Purpose product olefine selective is poor, causes the waste of raw material.Although researchers conduct extensive research this, alkene
Selectivity, which has no, to be significantly improved, this problem is difficult to make a breakthrough in a short time.
Current industrialized De-hydrogen Technology is all made of catalytic dehydrogenation route, and used catalyst is Pt bases and Cr2O3Base is catalyzed
Agent.Pt is expensive, and high investment and catalyst use cost limit the application using Pt catalytic dehydrogenation processes, only
The economy of the resourceful cheap country of alkane, the process is just reasonable.In addition, Pt catalyst is to sulphur, arsenic etc.
Poisonous substance is all very sensitive, therefore, is required impurity content in raw material using the catalyst very high.Using Pt catalyst, Pt is non-
It is often easy sintering, catalyst regeneration needs to regenerate using oxychlorination, and regenerated flue gas could discharge after must being administered.Support type
The dehydrogenation of Cr series catalysts is excellent, but the Cr VI that catalyst regeneration generates has the strong carcinogenesis of cause, the life of catalyst
It produces and may all cause environmental pollution using link, and the processing of dead catalyst is also a problem.
From the point of view of reactor, fixed bed, moving bed and recirculating fluidized bed have application.Alkane dehydrogenating catalyst is easy
Coking and deactivation is easy sintering using Pt catalyst Pts, thus catalyst needs frequent coke burning regeneration or oxychlorination regeneration.Using solid
Fixed bed is obviously not easy to regenerate, and moving bed and fluid bed can be carried out continuously reaction and regeneration.Pt catalyst is expensive, fluid bed
It can only use Cr series catalysts, Cr catalyst that can bring serious pollution to environment.Moving bed uses Pt catalyst, in order to ensure to urge
Agent has several days regeneration periods, reaction to need to carry out under hydro condition, this can reduce conversion per pass, conversion per pass drop
It is low, in addition hydrogen recycles so that the energy consumption of moving bed is very high.
From the point of view of catalyst regeneration, heat transfer efficiency and reaction efficiency, the optimum reactor of dehydrating alkanes is obviously non-
Recirculating fluidized bed does not belong to, and more much simpler than fixed bed, moving bed process flow using circulating fluid bed reactor part, together
Etc. scales plant investment it is relatively low.It is contradictory to focus on exploitation and be used for the nontoxic, relative low price of fluid bed and urge
Agent, and according to the mating circulating fluid bed reactor of performance properties feature of catalyst.
In terms of catalyst and circulating fluid bed reactor, in these years explored We conducted a large amount of.
For example：ZL 201110123675.1 discloses the cycle that a kind of catalyst and the suitable catalyst performance play
Fluidized-bed reactor, the catalyst part in the reactor is extracted out from bottom carries out high temperature afterburning regeneration, then with extraction
It is returned from the top of reactor after the mixing of another part catalyst, so not only coke burning regeneration catalyst, but also utilizes high temperature regeneration
Agent is reactor heat supply, while in turn avoiding the generation for allowing high temperature regeneration agent directly into thermal response caused by reactor.
Chinese patent application CN 201510003377.7 is improved for reactor, is proposed in reactor
Heat-exchanger rig is arranged in settling section, allows raw material to exchange heat with high-temperature oil gas, high-temperature oil gas is cooled down rapidly, reduces high temperature thermal response,
Avoiding device coking.There are reaction-regeneration systems for the scheme that ZL 201110123675.1 is proposed by CN 201510003556.0
Excessively complicated problem, it is proposed that simplified recirculating fluidized bed scheme, and regenerator is improved, ensure that fuel can fill
Divided combustion simultaneously fully exchanges heat with catalyst.
For the circulating fluid bed reaction device of dehydrating alkanes, the conversion per pass and olefine selective of dehydrating alkanes are improved
It is the target of the pursuit of this field forever.And in reaction unit, the air-teturning mixed phenomenon of gas phase also influences the choosing of dehydrating alkanes alkene
One of the factor of selecting property and conversion ratio.
In consideration of it, proposing the application.
Invention content
It is an object of the present invention to provide a kind of reaction unit of alkane catalytic dehydrogenation alkene, the reaction unit along
The gradual undergauge of fluid flow direction reduces the secondary conversion that back-mixing causes alkene.
Another object of the present invention is a kind of reaction unit of alkane catalytic dehydrogenation alkene, the reaction unit reactor
Interior reactant and catalyst cocurrent flow up, and can effectively improve the uniformity of reactor temperature distribution, avoid localized hyperthermia.
It is also another object of the present invention to provide the preparation methods that a kind of alkane catalytic dehydrogenation prepares alkene.
To achieve the above object, it adopts the following technical scheme that：
A kind of reaction unit of alkane catalytic dehydrogenation provided by the invention, including conversion zone and reactor settling section, reaction
Device settling section is located at the top of conversion zone, wherein the cross-sectional diameter of the conversion zone tapers into from top to bottom；
The reaction unit further includes catalyst regeneration inclined tube and feed distributor, and catalyst regeneration inclined tube stretches into instead
It answers in section, feed distributor is located at the lower section of the outlet end of the catalyst regeneration inclined tube in conversion zone.
Reaction unit provided by the invention, the cocurrent in conversion zone flows up catalyst with reactant, flow direction
Conversion zone is undergauge process, reduces secondary conversion caused by product back-mixing, and can make full use of the heat of high temperature catalyst,
The thermal response for avoiding localized hyperthermia's initiation, to improve the selectivity of alkene.
A kind of preparation method of alkane catalytic dehydrogenation alkene using above-mentioned reaction unit, raw material from feed distributor into
Enter conversion zone, raw material is flowed up with catalyst cocurrent, and the two contact carries out catalysis reaction, wherein conversion zone is heavy with reactor
Drop section lower end is at the section of same level, and the average linear velocity of gas is controlled in 0.3~10.0m/s, and reaction temperature is most
Between 500~650 DEG C, when quality sky of reaction is 0.1~15h for good control.
The selectivity of the method for the alkane catalytic dehydrogenation alkene that reaction unit of the present invention carries out, products therefrom alkene is promoted
Significant effect.
Compared with prior art, the advantage of the application is：
Reactant and catalyst cocurrent flow up in reactor, can effectively improve the uniform of reactor temperature distribution
Property, localized hyperthermia is avoided, to reduce thermal response, improves the selectivity of dehydrating alkanes alkene；And reactor is along fluid flowing side
To gradual undergauge, the secondary conversion of alkene caused by reducing back-mixing, to improve the yield and selectivity of alkene.High temperature regeneration agent
It is injected directly into reactor dense bed bottom, high temperature catalyst is not only contributed to and is mixed with the quick of catalyst in reactor, avoided
Localized hyperthermia is formed in bed, and the catalyst of dense fluidized also helps the transmission for terminating free radical, it is hot anti-to reduce
It answers, improves the selectivity of dehydrating alkanes alkene.
Description of the drawings
A kind of embodiment of the reaction unit of the alkane catalytic dehydrogenation alkene of Fig. 1 the application
A kind of embodiment of the reaction unit of Fig. 2 the application alkane catalytic dehydrogenation alkene-regenerating unit combination
Specific implementation mode
Below to the method for the reaction unit and alkane catalytic dehydrogenation alkene of the alkane catalytic dehydrogenation alkene of the present invention
It is described in further detail.The protection domain of the application is not limited, protection domain is defined with claims.It is certain disclosed
Detail provides comprehensive understanding to each disclosed embodiment.However, those skilled in the relevant art know, one is not used
These a or multiple concrete details, and embodiment can also be realized using the situation of other materials etc..
Unless the context otherwise requires, in specification and claims, the terms "include", "comprise" are interpreted as
It is open including meaning, as " include, but are not limited to ".
Mentioned " embodiment ", " embodiment ", " another embodiment " or " certain embodiment party in the description
Case " etc. refer to be included in relevant described feature, the structure or characteristic being specifically related to of the embodiment it is at least one
In embodiment.Therefore, " embodiment ", " embodiment ", " another embodiment " or " certain embodiments " must not
Refer both to identical embodiment.And specific feature, structure or characteristic can be in one or more embodiments to appoint
What mode is combined.Each feature disclosed in specification any can provide replacing for identical, impartial or similar purpose
Replace for property feature.Therefore it is only impartial or similar features general examples except having special instruction, revealed feature.
A kind of reaction unit of alkane catalytic dehydrogenation, including conversion zone and reactor settling section, reactor settling section are located at
The top of conversion zone, wherein the cross-sectional diameter of the conversion zone tapers into from top to bottom；
The reaction unit further includes catalyst regeneration inclined tube and feed distributor, and catalyst regeneration inclined tube stretches into instead
It answers in section, feed distributor is located at the lower section of the outlet end of the catalyst regeneration inclined tube in conversion zone.
Preferably, the outlet end of the catalyst regeneration inclined tube is located at the lower part of conversion zone.
In gas phase and solid phase flowing hybrid reaction system, back-mixing, also known as reverse mixing, is a kind of mixing phenomena.Narrow sense
Ground understands that it refers to the mixing of the material caused by movement opposite with main flow direction in continuous process.In following for alkane catalytic dehydrogenation
Ring bed fluidized reaction process, the air-teturning mixed phenomenon of gas phase are also to influence dehydrating alkanes olefine selective and one of conversion ratio important
Factor.In this application, catalyst outlet end is located at the lower part of conversion zone.In conversion zone, catalyst and reactant are simultaneously
It flows up, as gradual undergauge, the i.e. direction of the diameter of conversion zone cross section from top to bottom gradually decrease conversion zone upwards, that
The linear velocity of gas in conversion zone also gradually rises.The air-teturning mixed phenomenon that can be conducive to reduce gas in this way, to reduce
Dehydrating alkanes generate the secondary conversion of alkene, improve the selectivity of alkene.
A kind of embodiment is internally provided with catalyst riser in conversion zone, and catalyst regeneration inclined tube goes out in conversion zone
Mouth end is connected with catalyst riser.Preferably, the side wall phase of the outlet end of catalyst regeneration inclined tube and catalyst riser
Connection.
In some embodiments, the outlet end of the catalyst riser inside conversion zone is located at the lower part of conversion zone.
In some embodiments, it is additionally provided with pre-lift pipe in catalyst riser, medium is promoted for conveying catalyst
One end of pre-lift pipe be located at outside reaction unit, the other end is located in catalyst riser.
When catalyst regeneration inclined tube is connected with catalyst riser, high-temperature regenerated catalyst is introduced into instead by regenerator sloped tube
It answers in the catalyst riser in section.On the one hand, this set can directly be endothermic dehydrating alkanes reaction heat supply, this heat supply
Mode is that efficiency is highest.
On the other hand, if usually directly contacted high temperature catalyst with oil gas, localized hyperthermia, serious heat can be caused anti-
The defects of olefine selective should be reduced.And the application it is preheated paraffinic feedstock it is upward from reactor bottom, go out with from riser
Mouthful high temperature catalyst sprayed flows up together, not only contributes to coming into full contact with and uniformly mixing for raw material and catalyst, and
And the highly endothermic effect of the raw material and dehydrogenation reaction using low temperature is also helped, the temperature of catalyst is reduced rapidly, part is avoided
The thermal response that high temperature causes, to improve the selectivity of dehydrogenation.In addition, high temperature catalyst sprays into dense bed, high catalyst
Density is conducive to terminate the transmission of free radical, is also beneficial to reduce thermal response, improves the olefine selective of dehydrogenation.
In this application, the diameter of conversion zone cross section tapers into from top to bottom, including various ways, for example, reaction
The diameter of section cross section is successional to become smaller；Alternatively, since the lower end of conversion zone, first undergauge variation and then isometrical transition, again
Undergauge changes, and changes successively, until conversion zone top and reactor settling section lower end junction.
In some embodiments, conversion zone top is extend into reactor settling section.
The part conversion zone in reactor settling section is being stretched into, the diameter of cross section can be isometrical from top to bottom
, can also be first one section of undergauge from top to bottom, it is then again etc. radially extending.Specific conversion zone is stretched in reactor settling section
Enter how long distance, can need to be arranged according to actual process, as long as convenient for catalyst and Oil-gas Separation.
In some embodiments, in this application, catalyst riser, promotion medium tube are isometrical pipeline.
In some embodiments, it promotes medium tube and riser is stretched by the bottom or side wall of catalyst riser
It is interior.
The position of the outlet end of the catalyst riser is located at reaction pars infrasegmentalis.Here, reaction pars infrasegmentalis refers to leaning on
The space of proximal response section bottom end.
In some embodiments, the outlet end of pre-lift pipe is located at the position of regenerator sloped tube feed opening upper limb or more.It is logical
Often, catalyst riser is placed vertically, and regenerator sloped tube is connected with catalyst riser side wall, so, regenerator sloped tube outlet end
The namely opening of catalyst riser side wall.
Preferably, in the axial direction, the outlet end of pre-lift pipe is higher by the distance of regenerator sloped tube feed opening upper limb and is no more than
0.1m.It is furthermore preferred that the outlet end of pre-lift pipe is in same level with regenerator sloped tube feed opening upper limb.
In some embodiments, the cross section of conversion zone is circle, and catalyst riser is with conversion zone in coaxial arrangement.
The bottom of catalyst riser can be closed, or open state.As long as in catalyst riser
Promotion medium during constantly running up, negative pressure can be formed near regenerator sloped tube feed opening, in this way can be with
Increase the motive force that catalyst enters reactor from regenerator.
In some embodiments, the bottom of catalyst riser is closed state.
The application passes through conversion zone to be promoted with catalyst by the way that catalyst riser, regenerator sloped tube are arranged inside conversion zone
Pipe connects, under the suction and promotion for promoting medium, during regenerated catalyst is constantly run up along riser, again
Raw inclined tube feed opening can nearby form negative pressure, increase the motive force that catalyst enters reactor from regenerator；In addition, being situated between being promoted
Under matter pushes, catalyst is sprayed from riser upper port high speed, is conducive to high temperature catalyst and the catalyst in conversion zone is quick
Mixing avoids and forms localized hyperthermia in bed.It is furthermore preferred that in order to ensure that pre-lift pipe has good suction to catalyst
And impetus, the outlet of pre-lift pipe can be in the position on riser central axes.
It is true according to the angle of regenerator sloped tube, the length of riser and leg outlet position for regenerator sloped tube outlet port
It is fixed.In this application, regenerator sloped tube and catalyst riser connection, from catalyst riser in the opening on riser
The distance that edge is exported to catalyst riser is about 0.1m~2.0m, preferably 0.3m~1.0m.
In the reaction unit of the application, in order to achieve the purpose that reduce gas velocity so that catalyst sedimentation, the diameter of settling section
It is greater than the diameter of conversion zone.
In some embodiments, in conversion zone, the lower section of catalyst riser is equipped with feed distributor.Feed system
Close to reactor bottom.Preferably, feed distributor is the ring pipe of one or more arrangements in the same plane, in ring pipe
It is equipped with nozzle.
Wherein, the direction of nozzle can towards it is upper or towards under, it is preferable that towards downwardly direction.
Reacted in order to enable catalyst comes into full contact with raw material in conversion zone, in conversion zone, feed distributor it is upper
Portion is equipped with grid or multihole distributor.Preferably percent opening is not more than 50% distribution grid.
In some embodiments, in conversion zone, the adjacent two layers grid that the top of feed inlet is equipped with or porous distribution
The distance between plate is 0.01~2.0m；It is preferred that 0.1~0.7m.Constantly change gas by the setting of grid or multihole distributor
The distribution of body and catalyst promotes raw material to be come into full contact with catalyst and reacts, improves gas-solid contact and reaction efficiency.
Be equipped with oil gas vent on reaction unit top, be equipped with cyclone separator in reactor settling section, cyclone separator with
Oil gas vent is connected.
In this application, reclaimable catalyst can be extracted out from reactor settling section close to the side of bottom, through inclined tube to be generated
Into in regenerator.Reclaimable catalyst can be directly entered regenerator section dense bed, can also enter regenerator settling section.It is preferred that
, reclaimable catalyst enters regenerator settling section.Catalyst spent agent enters regenerator settling section, is in gas phase fluidization state,
Be conducive to the quick burn off of coke.
The reaction unit of dehydrating alkanes alkene provided by the present application can be with catalyst regenerator disclosed in the prior art
In conjunction with the ciculation fluidized dehydrogenation reaction of progress.
In certain modes, catalyst regenerator includes catalyst regeneration section and regeneration settling section, and regenerator section is located at sedimentation
The lower part of the lower part of section, reactor settling section is connect with the lower part of regeneration settling section by inclined tube to be generated；One end of regenerator sloped tube
It is connect with catalyst riser, the bottom connection of the other end and regenerator section.
Using the preparation method for the dehydrating alkanes alkene that the reaction unit of above-mentioned dehydrating alkanes alkene carries out, including such as
Lower step, raw material enter conversion zone from feed distributor, and raw material is flowed up with catalyst cocurrent, and the two contact be catalyzed anti-
It answers, wherein conversion zone is in reactor settling section lower end at the section of same level, and the average linear velocity control of gas exists
0.3~10.0m/s, reaction temperature are preferably controlled between 500~650 DEG C, are 0.1~15h when the quality sky of reaction.
On the other hand, in conversion zone, the gas average linear velocity control at catalyst riser exit cross-section exists
0.01~3m/s, best 0.2~0.7m/s.Gas linear velocity in the conversion zone of undergauge, conversion zone can gradually rise, favorably
In the back-mixing for reducing gas.
In some embodiments, reaction temperature control is between 550~620 DEG C.
In this application, the reaction temperature in conversion zone is the mean temperature of conversion zone.The assay method of mean temperature is
5~10 temperature measuring points are set in not coaxial, radial position in conversion zone, the average value of these temperature measuring point temperature is then in conversion zone
Reaction temperature.
In some embodiments, it is 1~8h when the quality sky of reaction.
Pressure at the top of the settling section of reaction unit is controlled in -0.01~0.1MPa, preferably 0~0.05MPa (table).
In some embodiments, the superficial gas velocity in riser is in 0.5~20m/s, it is preferable that in 3~10m/s.
In some embodiments, medium tube exit is being promoted, is promoting the wire velocity control of medium in 5~50m/s, it is excellent
It is selected in 15~30m/s.
In this application, the promotion medium can be dehydrogenation feed, water vapour, nitrogen, hydrogen, dry gas or others
Small molecule hydrocarbon etc., most handy dehydrogenation feed or nitrogen.
Catalyst regeneration device provided herein, including catalyst regeneration section and regeneration settling section, regenerate settling section
Positioned at catalyst regeneration section top, outer circulating tube is equipped between regeneration settling section and catalyst regeneration section.
The outer circulating tube refer to be located at regeneration settling section and catalyst regeneration section outside and with regeneration settling section and
The pipeline of catalyst regeneration section connection.
The high temperature catalyst part for entering regenerator settling section is extracted out and is returned through outer circulating tube by the setting of outer circulating tube
Regenerator bottoms.In this way, can effectively avoid, regenerator bottoms temperature is too low and flame-out, influences the operational safety of device；Meanwhile
Local temperature is excessively high in avoidable bed, leads to sintering of catalyst.
In some embodiments, the following side of one end connection catalyst regeneration section of outer circulating tube, the other end connect again
The following side of raw settling section.
One layer of multihole distributor is set every 0.01~2m, best 0.1~0.7m in the close phase section of catalyst regeneration section
Or grid, preferably grid.Can guarantee catalyst burns effect, promotes the heat transfer of gas-particle two-phase.
Term " the close phase section of catalyst regeneration section " is the common term of chemical field, also referred to as dense-phase flow in this application
Change section, is the main region of catalyst regeneration reaction, it is corresponding with gas phase fluidization section.
In the stripping section that the close phase pars infrasegmentalis of catalyst regeneration section is regenerator section.Herringbone is equipped in the stripping section of catalytic section
Shape baffle or other inner members with promotion gas-particle two-phase mass transfer.It can ensure air lift effect in this way, reduce catalyst to the greatest extent
The exhaust gas volumn of carrying.
Stripping medium can be water vapour, nitrogen, dry gas or other gases for not influencing catalytic dehydrogenation reactivity worth
Catalyst regeneration device provided by the present application can be combined with all dehydrogenation reaction devices of the prior art.For simultaneously
Carry out the dehydrogenation for the raw material that two or more have reaction condition requirement certain difference, can two or several reaction units share
One regenerating unit, such reaction condition can require to be set separately according to the reaction of specific raw material.Theoretically react
The number of device is unrestricted, but in view of the operability in engineering, the number of reactor is preferably not more than two.
Using the catalyst recovery process of above-mentioned catalyst regeneration device, including：
(1) reclaimable catalyst, fuel burn under conditions of 600~850 DEG C of temperature in the regenerator section of regenerating unit,
(2) catalyst of regenerator section enters settling section under the promotion of flue gas, wherein enters the part high temperature in settling section
Catalyst is by outer circulating tube back in regenerator section, it is preferable that return to regenerator section bottom, again with the catalyst of regenerator section one
Combust.
Preferably, fuel burns under conditions of 630~750 DEG C of temperature in the regenerator section of regenerating unit.
The fuel can be gaseous fuel, can also be the liquid fuel of not sulfur-bearing and metal.
In this application, fuel is injected in the close phase section of regenerator section, and fuel can be sprayed from different axial position multiple spots
Enter, also can only be sprayed into a certain axial position, preferably multiple spot sprays into, and minimum penetrating position should be on air distribution pipe.
Compared with prior art, the advantage of the application is：
1) reactant and catalyst cocurrent flow up in reactor, can effectively improve the uniform of reactor temperature distribution
Property, localized hyperthermia is avoided, to reduce thermal response, improves the selectivity of dehydrating alkanes alkene.
2) reactor is along the gradual undergauge of fluid flow direction, the secondary conversion of alkene caused by reducing back-mixing, to improve
The yield and selectivity of alkene.
3) high temperature regeneration agent is injected directly into reactor dense bed bottom, not only contributes to urge in high temperature catalyst and reactor
The quick mixing of agent avoids forming localized hyperthermia in bed, and the catalyst of dense fluidized also helps termination free radical
Transmission improve the selectivity of dehydrating alkanes alkene to reduce thermal response.
4) pre-lift medium sprays at a high speed near regenerator sloped tube catalyst feed opening upper limb, can be formed near feed opening
Negative pressure increases the motive force that catalyst enters reactor from regenerator, increases the flexibility for adjusting catalyst circulation amount.
5) spent agent is directly entered the settling section of regenerator, and gas phase fluidization is conducive to quickly burning for spent agent.
6) afterburning in regenerator dense fluidized section, the residence time of catalyst and fuel in regenerator is long, is conducive to
Coke on abundant burn off catalyst, ensures full combustion of fuel, while also helping gas-particle two-phase and fully conducting heat, and improves energy
Utilization rate.
7) use external catalyst circulation pipe that the high temperature catalyst in regenerator settling section is recycled to the bottom of regenerator, it can
It avoids regenerator bottoms too low and flame-out because of temperature, to eliminate the security risk brought by afterburning, can avoid localized hyperthermia,
Lead to sintering of catalyst.
Embodiment 1
It is the reaction unit and the application of alkane catalytic dehydrogenation provided by the present application shown in the present embodiment refer to the attached drawing 1,2
The catalyst regeneration device of offer is used in combination.This two covering device can be used separately, and be reacted respectively with other of the prior art
Device or catalyst regeneration device are used in combination.
The reaction unit of attached alkane catalytic dehydrogenation shown in FIG. 1 includes conversion zone 10 and reactor settling section 11, reactor
Settling section 11 is located at the top of conversion zone 10, and the diameter of 10 cross section of conversion zone tapers into from top to bottom, and catalyst regeneration is oblique
Pipe 5 stretches into conversion zone 10, and the outlet end of catalyst regeneration inclined tube 5 is located at the lower part of conversion zone 10.In the present embodiment, instead
It answers and continuously becomes smaller to upper under the diameter of 10 cross section of section.
Lower part in conversion zone 10 is equipped with catalyst riser 17.In conversion zone 10, catalyst regeneration inclined tube 5 passes through
Conversion zone wall enters in conversion zone and is connected with catalyst riser 17, and the pre-lift pipe 3 for conveying hoisting medium, which is located at, urges
In agent riser 17.Catalyst riser bottom be it is closed, pre-lift pipe 3 by the bottom of catalyst riser 17 or
Side wall stretches into riser 17.The distance that the outlet end of promotion medium tube 3 is higher by 5 feed opening upper limb of regenerator sloped tube is no more than
0.1m.It is furthermore preferred that the outlet end of promotion medium tube is in same level with regenerator sloped tube feed opening upper limb.It is being promoted in this way
Promotion medium in medium tube can form negative pressure during constantly running up near regenerator sloped tube feed opening, can be with
Increase the motive force that catalyst enters reactor from regenerator.
In the present embodiment, the cross section of conversion zone 10 is circle, catalyst riser 17, in catalyst riser
Pre-lift pipe 3 with conversion zone 10 be coaxially disposed.
In conversion zone 10, the lower section of catalyst riser 17 is equipped with charging ring pipe 4, and nozzle is equipped on ring pipe,
The direction of nozzle can towards it is upper or towards under, it is preferable that towards downwardly direction.In conversion zone 10, feed the upper of ring pipe 4
Portion is equipped with grid or multihole distributor.The distance between adjacent two layers grid or multihole distributor are 0.01~2.0m；It is excellent
Choosing, 0.1~0.7m.
It is equipped with oil gas vent 12 on the top of reaction unit, that is, settling section, cyclone separator is equipped in reactor settling section 11
16, cyclone separator 16 is connected with oil gas vent 12.10 upper end of conversion zone is stretched into reactor settling section 11.In present embodiment
In, the conversion zone in reactor settling section 11, from top to bottom, first undergauge are rear isometrical to extend to conversion zone upper end outlet.
Above-mentioned catalyst regeneration inclined tube 5 is connect with the bottom of the catalyst regeneration section 1 of regenerating unit.Catalyst is to be generated tiltedly
The first end of pipe 6 is connect with reactor settling section 11 close to the side of bottom, and second end and the regeneration of catalyst inclined tube 6 to be generated fill
That sets urges regeneration settling section 15 to connect.The regeneration settling section 15 of the regenerating unit is located at the top of regenerator section 1.
It is equipped with outer circulating tube 18 in the outside of regeneration settling section 15 and catalyst regeneration section 1, one end of outer circulating tube 18 connects
Connect the following side of catalyst regeneration section 1, the following side of other end connection regeneration settling section 15.
Go out 13 equipped with flue gas mouth at the top of regeneration settling section 15, cyclone separator 16, rotation are equipped in regeneration settling section 15
Wind separator 16 is connected with exhanst gas outlet 13.
The technological process of the reaction-regenerative device of embodiment 1 is as follows：Reaction raw materials by charging ring pipe 4 nozzle into
Enter in the conversion zone 10 of reaction unit, in high-temperature regenerated catalyst inflow catalyst riser 17, is promoting medium suction and pushing away
Dynamic effect sprays into conversion zone upwards along catalyst riser 17.High temperature catalyst and raw material together in conversion zone to
Upper flowing, in the process, raw material is contacted with catalyst carries out catalysis reaction.During flowing up, due to conversion zone from
Under to being above undergauge variation, the average linear velocity of gas gradually rises, and can effectively reduce axial mixing in gas phase phenomenon.
Then under the drive for promoting medium, enter in reactor settling section 11 entrainment of catalyst, carry catalyst
After cyclone separator detaches, product flows out product through oil gas vent.The catalyst isolated most exists through stripping medium 14 afterwards
Reactor settling section is extracted out close to the side of bottom and enters catalyst pipe 6 to be generated, subsequently into regenerating unit settling section 15
It is interior.
In regenerating unit, it can also be not to spray into air 8 and fuel 9, fuel gas fuel in the close phase section of regenerator section
The liquid fuel of sulfur-bearing and metal, by the coke burn off of reclaimable catalyst in regenerator section, under the promotion of flue gas, catalyst into
Enter to regenerate settling section 15, the catalyst member in settling section again returns to settling section bottom by outer circulating tube.Regeneration catalyzing
Agent enters by catalyst regeneration inclined tube 5 in the catalyst riser in conversion zone 10.It is carried out as above-mentioned in conversion zone 10
Circular response-regenerative response is realized in reaction.
Embodiment 2：
Preparing propylene by dehydrogenating propane, using the equipment of the embodiment of the present invention 1
Raw material：The propane of 99wt%, inlet amount 0.6t/h
Catalyst：Environment-friendly metal oxide catalyst ADHO-1 (ZL 201110123675.1)
Reaction condition：One layer of grid is arranged every 0.5m in conversion zone internal catalyst bed layer；Bed mean temperature, 600 DEG C；It is heavy
Device pressure, 0.03MPa drop；When quality sky, 3h；Leg outlet section gas average linear velocity, 0.5m/s in conversion zone；Reaction
At the section that device settling section bottom is connect with reactor, gas average linear velocity 2m/s.
Regeneration condition：Can one layer of grid be set every 0.5m in the close phase section of regenerator；The close phase section temperature of regenerator, 700 DEG C.
Reaction-regeneration system structure type：The present invention；Comparison, patent application CN2016 1,104 2006.0.
The reaction of the alkane catalytic dehydrogenation of patent application CN2016 1,104 2006.0-regenerative response device includes：
Conversion zone and settling section, settling section are located at the top of conversion zone, and settling section is isometrical tank structure, and conversion zone is etc.
The diameter of diameter tubular structure, conversion zone is smaller than the diameter of settling section.It is undergauge section (stripping section), undergauge section in the lower part of conversion zone
It is connected with catalyst inclined tube to be generated, baffle is equipped in undergauge section.
Be internally provided with catalyst riser in conversion zone, in conversion zone the outlet of catalyst regeneration inclined tube promoted with catalyst
Pipe is connected, and the promotion medium tube for conveying hoisting medium is located in catalyst riser.Conversion zone and promotion medium tube are equal
For tubular structure, and the two is coaxially disposed.The bottom for promoting medium tube is closed, promotes medium tube and passes through catalyst riser
Bottom or side wall stretch into riser.The highest point for promoting the outlet end of medium tube and the outlet of catalyst regeneration inclined tube exists
Near, most preferably in the same level, or slightly higher than regenerator sloped tube outlet.
It is equipped with charging ring pipe in the lower end of conversion zone, nozzle is equipped on ring pipe, the direction of nozzle is under.Anti-
It answers in section, the top of charging ring pipe is equipped with grid or multihole distributor.The diameter of settling section is greater than the diameter of conversion zone,
The maximum gauge of settling section and the diameter ratio of conversion zone are 4/1~1.1/1.
The reaction unit of CN2016 1,104 2006.0 can be with the arbitrary catalyst regeneration device of the prior art to cooperation
It uses.Here, the structure of used regenerating unit and its connection are as follows：
The other end of above-mentioned catalyst regeneration inclined tube, catalyst inclined tube to be generated regenerates sedimentation with urging for regenerating unit respectively
Section is connected with regenerator section, and the regeneration settling section of the regenerating unit is located at the top of regenerator section.The reclaimable catalyst of conversion zone
Enter undergauge section from conversion zone bed lower part, after nitrogen or other gas air lifts for not influencing raw material dehydrogenation reaction, through to be generated
Inclined tube enters regenerator section.
Outer circulating tube is equipped between regeneration settling section and catalyst regeneration section, one end connection catalyst of outer circulating tube is again
The following side of raw section, the following side of other end connection regeneration settling section.
The regenerator sloped tube close to regeneration settling section at be arranged one section of standpipe, the standpipe be and regeneration settling section
The parallel pipeline of axial direction.Chev(e)ron baffle is set in standpipe.
Other settings are consistent with the present invention's in reactor settling section and regeneration settling section.
Its comparing result is as shown in table 1：
The distribution of dehydrogenating propane product and Propylene Selectivity that 1. content of table is 99wt%, wt%
The implementation result of the present invention and the implementation result of comparison scheme are as shown in table 1.It is of the invention compared with comparison scheme
High 1.34 percentage point, the high selectivity of propylene 3.75 percentage point of the propylene once through yield than comparing scheme, it is aobvious to promote effect
It writes.
Embodiment 3：
Preparing isobutene through dehydrogenation of iso-butane, using the equipment of the embodiment of the present invention 1
Raw material：The iso-butane of 98wt%, inlet amount 0.5t/h
Catalyst：Environment-friendly metal oxide catalyst ADHO-1 (ZL 201110123675.1)
Reaction condition：One layer of grid is arranged every 0.5m in conversion zone internal catalyst bed layer；Bed mean temperature, 580 DEG C；It is heavy
Device pressure, 0.025MPa drop；When quality sky, 3h；Conversion zone leg outlet section gas average linear velocity, 0.45m/s；Reaction
At the section that device settling section bottom is connect with reactor, gas average linear velocity 1.8m/s.
Regeneration condition：Can one layer of grid be set every 0.5m in the close phase section of regenerator；The close phase section temperature of regenerator, 700 DEG C.
Reaction-regeneration system structure type：The present invention；Comparison, patent application CN2016 1,104 2006.0.
The reaction-regenerative device of patent application CN2016 1,104 2006.0 is consistent as described in Example 2.
The distribution of dehydrogenation of isobutane product and selective isobutene that 2. content of table is 98wt%, wt%
The implementation result of the present invention and the implementation result of comparison scheme are as shown in table 2.It is of the invention compared with comparison scheme
High 3.82 percentage point, the high selectivity of isobutene 3.69 percentage point, to isobutyl of the isobutene once through yield than comparing scheme
The selectivity of alkene promotes effect clearly.
Claims (10)
1. a kind of reaction unit of alkane catalytic dehydrogenation, including conversion zone and reactor settling section, reactor settling section is located at anti-
Answer the top of section, wherein the cross-sectional diameter of the conversion zone tapers into from top to bottom；
The reaction unit further includes catalyst regeneration inclined tube and feed distributor, and catalyst regeneration inclined tube stretches into conversion zone
Interior, feed distributor is located at the lower section of the outlet end of the catalyst regeneration inclined tube in conversion zone；
Preferably, the outlet end of the catalyst regeneration inclined tube is located at the lower part of conversion zone.
2. reaction unit according to claim 1, which is characterized in that be internally provided with catalyst riser in conversion zone, instead
The outlet end of catalyst regeneration inclined tube in section is answered to be connected with catalyst riser；
Preferably, the outlet end of catalyst regeneration inclined tube is connected with the side wall of catalyst riser.
3. reaction unit according to claim 2, which is characterized in that the outlet of the catalyst riser inside conversion zone
End is positioned at the lower part of conversion zone.
4. according to claim 1-3 any one of them reaction units, which is characterized in that be additionally provided with pre- carry in catalyst riser
Riser, the outlet end of pre-lift pipe are located at the position of catalyst regeneration inclined tube outlet end upper limb or more；
Preferably, in the axial direction, the outlet end of pre-lift pipe is higher by the distance of catalyst regeneration inclined tube outlet end upper limb and does not surpass
Cross 0.1m；
It is furthermore preferred that the outlet end of pre-lift pipe is in same level with catalyst regeneration inclined tube outlet end upper limb.
Most preferably, pre-lift pipe exports the position on catalyst riser central axes.
5. according to claim 1-4 any one of them reaction units, which is characterized in that the cross section of conversion zone is circle, is urged
Agent riser is with conversion zone in coaxial arrangement.
6. according to claim 3-5 any one of them reaction units, which is characterized in that catalyst regeneration inclined tube is carried with catalyst
Riser connection, the distance exported from catalyst regeneration inclined tube outlet end upper limb to catalyst riser are 0.1m~2.0m；
It is preferred that 0.3m~1.0m.
7. the dehydrating alkanes system that a kind of reaction unit using claim 1-6 any one of them dehydrating alkanes alkene carries out
The preparation method of alkene, includes the following steps, raw material enters conversion zone, raw material and catalyst cocurrent to upstream from feed distributor
Dynamic, the two contact carries out catalysis reaction, wherein and conversion zone is in reactor settling section lower end at the section of same level,
In 0.3~10.0m/s, reaction temperature controls between 500~650 DEG C for the average linear velocity control of gas, and the quality of reaction is empty
When be 0.1~15h；
Preferably, reaction temperature control is between 550~620 DEG C；
Preferably, it is 1~8h when the quality sky of reaction.
8. preparation method according to claim 7, which is characterized in that in conversion zone, exported in catalyst riser horizontal
Gas average linear velocity at section is controlled in 0.01~3m/s, best 0.2~0.7m/s.
9. preparation method according to claim 7 or 8, which is characterized in that superficial gas velocity in riser 0.5~
20m/s, it is preferable that in 3~10m/s.
10. preparation method according to claim 7 or 8, which is characterized in that in pre-lift pipe exit, promote medium
Wire velocity control is in 5~50m/s, preferably in 15~30m/s.
Priority Applications (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710213552.4A CN108654526B (en) | 2017-04-01 | 2017-04-01 | Reactor capable of reducing back mixing and used for preparing olefin through alkane dehydrogenation and preparation method |
| US15/887,399 US10307721B2 (en) | 2017-04-01 | 2018-02-02 | Reaction-regeneration device and process for alkane dehydrogenation to alkene |
| US16/239,643 US10343128B2 (en) | 2017-04-01 | 2019-01-04 | Reaction-regeneration device and process for alkane dehydrogenation to alkene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710213552.4A CN108654526B (en) | 2017-04-01 | 2017-04-01 | Reactor capable of reducing back mixing and used for preparing olefin through alkane dehydrogenation and preparation method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108654526A true CN108654526A (en) | 2018-10-16 |
| CN108654526B CN108654526B (en) | 2021-04-16 |
Family
ID=63783818
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710213552.4A Active CN108654526B (en) | 2017-04-01 | 2017-04-01 | Reactor capable of reducing back mixing and used for preparing olefin through alkane dehydrogenation and preparation method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108654526B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111715152A (en) * | 2019-03-18 | 2020-09-29 | 上海卓然工程技术股份有限公司 | Combined reactor for preparing olefin by alkane dehydrogenation and hydrocarbon catalytic cracking |
| CN112973579A (en) * | 2021-02-07 | 2021-06-18 | 中国科学院过程工程研究所 | Gas-solid short contact time reaction device and application thereof |
| CN114426489A (en) * | 2020-10-15 | 2022-05-03 | 中国石油化工股份有限公司 | Device and method for preparing aniline by nitrobenzene hydrogenation |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1820835A (en) * | 2006-01-20 | 2006-08-23 | 哈尔滨工业大学 | Conical wall-less effect reactor |
| CN202122945U (en) * | 2011-05-11 | 2012-01-25 | 上海河图石化工程有限公司 | Circulating fluidized bed type low-carbon alkane dehydrogenizing and olefin generating device |
| CN103450921A (en) * | 2012-06-01 | 2013-12-18 | 中国石油天然气集团公司 | Method for selectively preparing propylene and clean gasoline through using methanol |
-
2017
- 2017-04-01 CN CN201710213552.4A patent/CN108654526B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1820835A (en) * | 2006-01-20 | 2006-08-23 | 哈尔滨工业大学 | Conical wall-less effect reactor |
| CN202122945U (en) * | 2011-05-11 | 2012-01-25 | 上海河图石化工程有限公司 | Circulating fluidized bed type low-carbon alkane dehydrogenizing and olefin generating device |
| CN103450921A (en) * | 2012-06-01 | 2013-12-18 | 中国石油天然气集团公司 | Method for selectively preparing propylene and clean gasoline through using methanol |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111715152A (en) * | 2019-03-18 | 2020-09-29 | 上海卓然工程技术股份有限公司 | Combined reactor for preparing olefin by alkane dehydrogenation and hydrocarbon catalytic cracking |
| CN114426489A (en) * | 2020-10-15 | 2022-05-03 | 中国石油化工股份有限公司 | Device and method for preparing aniline by nitrobenzene hydrogenation |
| CN112973579A (en) * | 2021-02-07 | 2021-06-18 | 中国科学院过程工程研究所 | Gas-solid short contact time reaction device and application thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108654526B (en) | 2021-04-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104437274B (en) | Fluidized bed reactor used for light olefin cracking and Methanol To Olefin (MTO) | |
| CN109012513B (en) | Methanol-to-olefin reactor | |
| CN111807916B (en) | Device for producing low-carbon olefin by efficient oxygen-containing compound | |
| CN103571530B (en) | Wax catalysis cracking is for the method for low-carbon alkene | |
| CN109499486B (en) | Circulating fluidized bed reaction device for preparing olefin by catalytic dehydrogenation or catalytic cracking of alkane | |
| CN103540345A (en) | Catalytic cracking method | |
| CN108654526A (en) | A kind of reactor and preparation method of the dehydrating alkanes alkene reducing back-mixing | |
| US20190134590A1 (en) | Reaction-regeneration device and process for alkane dehydrogenation to alkene | |
| CN103540346B (en) | A kind of Desending catalytic cracking device | |
| CN103341341A (en) | Fluidized bed reactor for preparing butadiene | |
| CN111875465B (en) | Method for producing low-carbon olefin by oxygen-containing compound | |
| CN206014776U (en) | Catalytic cracking unit | |
| CN111871343A (en) | Device for producing low-carbon olefin by using oxygen-containing compound | |
| CN104419458A (en) | Catalytic cracking method and device | |
| CN103788993A (en) | Catalytic cracking unit | |
| CN102040438A (en) | Coaxial circular reaction-regeneration device with embedded riser | |
| CN111875464B (en) | Method for producing low-carbon olefin by high-efficiency oxygen-containing compound | |
| CN108079912A (en) | A kind of reaction unit and its reaction method of alkane catalytic dehydrogenation | |
| CN109107615B (en) | Regeneration method and regeneration device for alkane dehydrogenation catalyst | |
| CN103788992A (en) | Catalytic cracking method | |
| CN105218288B (en) | High-efficiency rapid gas-solid separation and settlement method for methanol-to-olefin | |
| CN1140607C (en) | apparatus for producing low carbon olefines by high-tmep. catalyzing contact cracking from heavy petroleum hydrocarbon | |
| CN109499485B (en) | Circulating fluidized bed reaction device for preparing olefin by alkane dehydrogenation-cracking | |
| CN202658136U (en) | Petroleum hydrocarbon catalytic cracking device | |
| CN202829956U (en) | Petroleum hydrocarbon catalytic cracking device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |