CN110325495A - For dehydrogenation C3-C5The equipment of alkane - Google Patents
For dehydrogenation C3-C5The equipment of alkane Download PDFInfo
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- CN110325495A CN110325495A CN201880013179.0A CN201880013179A CN110325495A CN 110325495 A CN110325495 A CN 110325495A CN 201880013179 A CN201880013179 A CN 201880013179A CN 110325495 A CN110325495 A CN 110325495A
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- 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
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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
- Y02P20/10—Process efficiency
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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
-
- 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
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- Chemical Kinetics & Catalysis (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The present invention relates to one kind to make C3‑C5Equipment of the paraffin dehydrogenation to produce corresponding alkene.The equipment includes: the reactor and regenerator of the fluidized bed with particulate chromia-alumina catalyst；For make equilibrium catalyst from reactor cycles to regenerator (vice versa) pipe；For by raw material supply to reactor and the pipe for being used to supply air to regenerator；For removing the pipe of contact gas and regeneration gas, the pipe is connected to the cyclone separator that the top of reactor and regenerator is arranged in；Shell and tube heat exchanger is installed on the tube, to recycle the heat of these gases when contacting gas and regeneration gas is fed into the pipe side of heat exchanger；With wet type device for trapping and dry type device for trapping, described device is used to retain the catalyst dust of entrainment from contact gas and regeneration gas.The characteristics of equipment, is that it includes system, and the system is used to for equilibrium catalyst being supplied to the pipe side entrance of heat exchanger from reactor-regenerator system；Device, described device are used to retain the catalyst of contact gas and/or regeneration gas exit from shell and tube heat exchanger pipe side, and the catalyst of retention is returned to the top of the fluidized bed of reactor and/or regenerator.Claimed equipment stabilizes the operation of dehydrogenation unit and increases the production capacity of alkene by reducing the blocking of the heat exchanger as caused by catalyst dust, and the heat exchanger is used to recycle the heat of contact gas and regeneration gas.
Description
Technical field
The present invention relates to petro chemical industries, in particular to are used for C3-C5Paraffin dehydrogenation is setting for corresponding alkene
Standby, the alkene is used to produce the basic monomer of synthetic rubber, and for producing polypropylene, methyl tertiary butyl ether(MTBE) etc..
Background technique
It is known it is a kind of using mobile coarse grain catalyst be used to make paraffin dehydrogenation equipment (Ya.Ya.Kirnos and
O.B.Litvin, commercial run (the Current Industrial Methods of Butadiene of current butadiene synthesis
Synthesis), analytical relatively comment (Analytical comparative reviews), central information research institute
(Central Research Institute of Information), the technical economic investigation of oil refining and petrochemical industry
(Technical and Economic Studies in Oil Refinery and Petrochemical Industry),
Synthetic rubber production series, Moscow, page 1967,81).
The shortcomings that existing equipment includes: complicated design and the equipment that can not design high capacity.
The substantive distinguishing features of analogous technical are embodied in a kind of equipment that normal butane is dehydrogenated to butylene
(I.L.Kirpichnikov, V.V.Beresnev, L.M.Popov, China Synthetic Rubber Industry foundation engineering process books
(Flowchart Book of Basic Works in Synthetic Rubber Industry), Leningrad, chemistry,
Page 1986,8-12).The equipment includes: the reactor and regenerator of the fluidized bed with particulate chromia-alumina catalyst；
For make catalyst from reactor cycles to regenerator (vice versa) pipe；For supplying raw material to reactor and to regenerator
Supply the pipe of air；For removing the pipe of contact gas and regeneration gas, it is connected to and is arranged in reactor and regenerator top
Cyclone separator；The shell and tube heat exchanger (recycling boiler) of installation on the tube, in contact gas and regeneration gas
It is admitted to the pipe side of heat exchanger and when condensed water is fed into shell-side to generate steam, recycles the heat of these gases；With
Device for the wet type from contact gas and regeneration gas and the catalyst dust of dry type retention entrainment.
However, in the device, the catalyst dust that recycling boiler tube is carried secretly from the fluidized bed of reactor and regenerator
Deposit blocking.Which reduce the heat transfers (coefficient) on recycling boiler tube, reduce the steam generation in recycling boiler, increase
Furnace pressure drop, therefore reactor pressure is increased, and therefore reduce olefins yield.
Such case also results in the confusion of the heat pattern for washer that is cooling and washing contact gas, with recycling pot
The higher temperature of the contact gas in the exit of furnace is related, and correspondingly, in the inlet of washer, causes washer cold
But the higher load of the heat exchanger in system, and further result at the contact gas access of product turbo-compressor
Higher temperature and pressure, therefore reduce its capacity.Therefore, the disadvantage causes the technology of certain embodiments and economic performance worse
(for example, leading to that the raw material capacity of reactor is lower, yield is lower, and therefore leads to target product and recycle the steam in boiler
The generation of yield is lower), and interrupted with the frequent operation that relevant cost cleans recycling boiler.
The substantive distinguishing features of analogous technical, which are also embodied in one kind, makes C in chromia-alumina catalyst fluidized bed3-C5's
Alkane and the equipment of isoparaffin dehydrogenation (Russ P 2591159,07 С 5/333 of IPC С；B01J8/00, publication date
10.07.2016), wherein the equipment includes: reactor and regenerator with separation grid, and there is row at an upper portion thereof
The cyclone separator of dirt dipleg (dipleg)；For hydrocarbon raw material to be supplied to reactor and supplies air to the pipe of regenerator；
Pipe for the recycling catalyst between reactor and regenerator；For removing contact gas from reactor and coming from regenerator
Regeneration gas pipe, connect with the cyclone separator in reactor and regenerator；For contacting gas and regeneration gas
The heat exchanger (recycling boiler) of recuperation of heat；For the device of wet type and dry type retention catalyst dust, the catalyst dust
From reactor and regenerator entrainment, from contact gas and regeneration gas；With for making dust back to reactor-regenerator system
The pipe of system.Here, the port of the pipe for returning to the catalyst dust retained in dry type device for trapping is connected to reactor
With the dust discharge dipleg of the cyclone separator in regenerator, for making the catalyst dust of retention back to reactor and regenerator
Fluidized bed.The inverse of regenerator is arranged in the port of pipe for returning to the catalyst dust retained in wet type device for trapping
Third separates under grid, i.e., in catalyst oxide regions.The dust discharge dipleg of cyclone separator in reactor and regenerator
The end of (for returning to the catalyst dust retained in cyclone separator and dry type device for trapping) is in fluidized bed height
The lower part of the fluidized bed of reactor and regenerator is arranged in the horizontal place of 2-14%.
However, the equipment does not solve the pipe side of catalyst dust deposit blocking recovery heat exchanger (recycling boiler)
The problem of and this blocking all above-mentioned consequences.In addition, by being retained in the dry type device for trapping for being used for catalyst dust
Dust stream make that the device is complicated by cyclone dip-leg and change, and by increasing residual interference of the catalyst from dehydrogenation system
The operation of cyclone separator.When the dry catalyst dust with fine grain retention is returned to reactor and regeneration by this equipment
When the fluidized bed lower part of device, which quickly enters the delivery pipe of catalyst recycling system, and urges with the balance of circulation
Agent is transferred to the Disengagement zone of reactor and regenerator together, actually bypasses fluidized bed, and which increases catalyst from system
In residual.It is noted here that the equilibrium catalyst recycled in reactor-regenerator system is such catalyst: being catalyzed
In agent use process, according to the abrasion of the characteristic of catalyst, the efficiency, catalyst of dust retention system in system initial charge
The feed mode of the fresh catalyst of its loss of (decomposition) and supplement, to determine the size distribution of catalyst.Equilibrium catalyst
Average particle size is significantly higher than the average particle size for the catalyst dust carried secretly from fluidized bed.Slurry (after wet dust retention) returns
The temperature that catalyst zoneofoxidation into regenerator can damage catalyst oxidizing condition, reduce zoneofoxidation, and respectively, catalysis
Agent oxidizability deteriorates dehydrogenation (olefins yield).
The immediate prior art (Russ P 2129111, IPC С 07 С 5/333, publication date 20.04.1999) is public
It has opened a kind of for making C3-C5The similar equipment of paraffin dehydrogenation, wherein dry type and the catalyst dust of wet type retention are fluidizing
Back to the middle part of reactor and the fluidized bed of regenerator at the level of the 15-85% of bed height.However, will have relative low temperature
The dry catalyst dust of retention and the wet dust as slurry be supplied to dehydrogenation zone and regeneration that the region makes reactor
Temperature Distribution deformation in the catalyst zoneofoxidation of device, reduces the temperature in the region, and therefore makes dehydrogenation (alkene production
Rate) deteriorate.
A kind of equipment (Russ P 2523537,07 С 5/333 of IPC С for by dehydrogenating propane at propylene known；
С07С11/06；B01J8/18；B01J38/32, publication date 20.07.2014), which includes: with particulate chromium oxide-oxygen
Change the reactor and regenerator of Al catalysts fluidized bed；For raw material vapor to be supplied to the pipe of reactor, vertically pacify thereon
Equipped with shell and tube heat exchanger, which is used to carry out recuperation of heat to the contact gas being discharged from reactor.Here, former
Material steam is supplied to the shell-side of heat exchanger, and contacts gas and be supplied to pipe side, then before being supplied to reactor
Raw material vapor is fed in furnace to overheat.The recuperation of heat for leaving the regeneration gas of regenerator recycles heat exchange in shell-tube type
It is carried out in device, regeneration gas is fed into the pipe side of heat exchanger, while the regeneration to heat exchanger shell-side is fed at this time
The air of device is preheated.
As above-mentioned all devices, which not can solve catalyst dust deposit for contacting gas and regeneration
On the pipe of gas the problem of blocking heat-exchanger pipe.
Summary of the invention
The purpose of the present invention is improve dehydrogenating technology by the blocking for reducing the heat exchanger caused by catalyst dust
Technology and economic performance, steady operation dehydrogenation unit and the production capacity for increasing equipment, the heat exchanger is for recycling
Contact the heat of gas and regeneration gas.
In order to realize given purpose, what is proposed is used for C3-C5Paraffin dehydrogenation is the equipment packet of corresponding alkene
Include: reactor 1 and regenerator 2, the reactor 1 and regenerator 2 have the fluidized bed of particulate chromia-alumina catalyst；
Pipe 7,8, the pipe 7,8 is for making equilibrium catalyst (vice versa) from reactor cycles to regenerator；Pipe 5, the pipe 5 are used for
By raw material supply to reactor；Pipe 6, the pipe 6 is for supplying air to regenerator；For removing contact gas 9 and regeneration
The pipe of gas 10, the pipe are connect with the cyclone separator 3 on the top that reactor 1 and regenerator 2 is arranged in；Shell-tube type heat exchange
Device 11,12, the shell and tube heat exchanger 11,12 is installed on the tube, to be supplied in contact gas and regeneration gas
The heat of these gases is recycled when to the pipe side of heat exchanger；With wet type device for trapping 13 and dry type device for trapping 14, the dress
Set the catalyst dust for retaining entrainment from contact gas and regeneration gas.
The equipment includes: system, and the system is used to equilibrium catalyst being supplied to package from reactor-regenerator system
The pipe side entrance of formula heat exchanger 11 and/or 12；Device, described device is for being trapped in for contacting gas and/or for again
Catalyst at the pipe side outlet of the shell and tube heat exchanger of angry body, and by the catalyst of retention back to reactor and/or
The top of the fluidized bed of regenerator.
System for equilibrium catalyst to be supplied to recovery heat exchanger entrance can be equipped with pipe 23,24, be used for from reaction
Remove equilibrium catalyst in device-regenerator system, the end of the pipe is used for the catalyst charge to being used for recuperation of heat
The upstream of heat exchanger 11,12, in the pipe for contacting gas 9 and/or regeneration gas 10, wherein the end and heat are handed over
Parallel operation 11,12 separates, and the distance separated is 1 to 12 times for contacting the diameter of the pipe of gas 9 and/or regeneration gas 10,
In, it is external cyclone 20,21 after heat exchanger 11,12, the external cyclone 20,21 has pipe 27,28,
The pipe 27,28 is used to make the catalyst of retention in reactor and/or regenerator at the level of the 86-98% of fluidized bed height
Back in the fluidized bed of reactor and/or regenerator.
The port 29 or set that pipe 23 for removing equilibrium catalyst from reactor-regenerator system may be connected on pipe 8
The port in the fluidized bed region of reactor 1 is set, the pipe 8 is used to that catalyst to be made to be recycled to reactor 1 from regenerator 2,
In, the port 25 being arranged on the pipe for contacting gas 9 is connected to for supplying the end of pipe 23 of catalyst.
Pipe 24 for removing equilibrium catalyst from reactor-regenerator system may be connected to port or setting on pipe 7
Port 30 in the fluidized bed region of regenerator 2, the pipe 7 are used to that catalyst to be made to be recycled to regenerator 2 from reactor 1,
In, the port 26 being arranged on the pipe for regeneration gas 10 is connected to for supplying the end of pipe 24 of catalyst.
For returning to the catalyst retained in external cyclone 20 (it is in the pipe for contacting gas)
Pipe 27 may be coupled to the port 31 in the fluidized bed region of reactor 1.
For returning to the catalyst retained in external cyclone 21 (it is in the pipe for regeneration gas)
Pipe 28 may be coupled to the port 32 in the fluidized bed region of regenerator 2.
Pipe 16 for returning to the catalyst pulp from the device 13 for wet type retention catalyst dust can flow
The horizontal place for changing the 86-98% of bed height is connected to the port 33 being arranged in the fluidized bed of regenerator 2.
Pipe 15 for returning to catalyst dust from the device 14 for dry type retention catalyst dust can be in fluidized bed
The horizontal place of the 86-98% of height is connected to the port 32 being arranged in the fluidized bed of regenerator 2.
The system of shell-side inlet for supplying catalyst to recovery heat exchanger may include independent hopper, described
Hopper is for measuring and supplying balance and/or fresh dehydrogenation to clean pipe.
External cyclone 20 in the pipeline for contacting gas is configurable to secured shell (strong
Casing the cyclone separator group in).
External cyclone 21 in the pipeline for regeneration gas is configurable to one or more of parallel arrangement
A cyclone separator.
Reactor 1 and regenerator 2 can be parallel to each other or be coaxially arranged.The circulation of catalyst in the previous case may be used
To be carried out by two identical U-shaped delivery pipes, and in the latter case can be by logical in reactor and internal regenerator
The straight delivery pipe crossed carries out.
For contacting gas 25 and regeneration gas 26 pipe, for these gases recuperation of heat heat exchanger 11,
12 may include that for example the recycling boiler for being supplied with condensed water and generating steam；Recovery heat exchanger, the recovery heat exchanger
For preheat for example further be supplied to reactor 1 gaseous paraffin hydrocarbons (contact gas pipeline in), and for preheat into
One step is supplied to the air of regenerator 2 (in regeneration gas pipeline).
The device from the fluidized bed catalyst dust carried secretly and the equilibrium catalyst of supply is retained for dry type can include: rotation
Wind separator, electrofilter, cartridge filter, hose filter, box type filter and other can separate institute in a dry form
The dust device for trapping of the continuous operation of the catalyst dust of retention.
May include for the system by the catalyst back to reactor and/or regenerator, for example, storage hopper and for making
With pipe come the system of pneumatic transfer catalyst, the catalyst that the pipe is used to retain is returned in fluidized bed
The system of entrance for equilibrium catalyst to be supplied to recovery heat exchanger may include storage hopper and be used for by
The pipe of equilibrium catalyst pneumatic transfer.The system can have the flowmeter for measuring equilibrium catalyst flow velocity.It is independent
Storage hopper can have the volume for being enough single transfer catalyst, and single transfer amount is needed for the pipe of regular cleaning heat exchanger
Amount.It can have equilibrium catalyst from reactor-regenerator system and new by the pipe of weigh-hatching plant cleaning heat exchanger
Fresh dehydrogenation or in any proportion their mixture of mixed catalyst.Equilibrium catalyst can be in batches or continuously
Mode is supplied to the entrance of recovery heat exchanger.For example, air or nitrogen can be used for catalyst pneumatic transfer to regenerator system
System, and nitrogen, unstrpped gas used in equipment, natural gas etc. can be used for catalyst pneumatic transfer to reactor.
Wet type device for trapping for catalyst dust can be used such as plate and grid, filling and other water injections
Column, Venturi scrubber (Venturi scrubbers) or their combination etc..Catalyst pulp can accumulate in column bottom or list
In only pond.System for returning to the catalyst of retention may include: storage pool, mashing pump and be used for catalyst pulp
Back to the pipe of regenerator.Slurry concentrator, such as centrifuge may be used herein.It is obtained in the pipeline for contacting gas
Slurry can have the organic matter of high-content, such as heavy hydrocarbon and tar, can return to regenerator and burn wherein to produce
Raw additional heat, therefore save the fuel gas for being supplied to regenerator.
The raw material used in a device may include C3-C5Alkane, for example, propane, normal butane, iso-butane, isopentane and
Their mixture.
Suitable catalyst may include, for example, chromium (VI) and average grain diameter containing 1.5-3.5 weight % are 45-90 μ
The particulate chromia-alumina catalyst AOK-73-24 of m.
Detailed description of the invention
Fig. 1, which is shown, makes C3-C5The flow chart of paraffin dehydrogenation is to illustrate the present invention.The equipment includes: to aoxidize with particulate
The reactor 1 and regenerator 2 of chromium-aluminium oxide catalyst fluidized bed, wherein being equipped on their top has dust discharge dipleg 4
Cyclone separator 3；It is respectively used to supply hydrocarbon raw material and the pipe 5 and 6 to regenerator supply air to reactor；For reacting
The pipe 7 and 8 of recycling catalyst between device 1 and regenerator 2；Carry out the contact gas 9 of autoreactor and from regenerator for removing
Regeneration gas 10 pipe, the pipe connect with cyclone separator 3, heat recovery heat exchanger 11 and 12；Wet type device for trapping 13
(washer) and dry type device for trapping 14 (electrofilter), described device are used to retain catalysis from contact gas and regeneration gas
Agent dust；Pipe 15 and 16 for returning to catalyst with wet (slurry) form in a dry form.Contact gas and regeneration gas
Pass through the pipe side of corresponding recovery heat exchanger.For recycling catalyst pipe 7 (its be configured to for by catalyst from reactor
1 pneumatic transfer is to regenerator 2) be equipped with pipe 17 for supplying air, and be configured to for by catalyst from regenerator pneumatic
The pipe 8 of reactor is transferred to equipped with the pipe 18 for supplying hydrocarbon raw material steam 18.The pipe 19 of regenerator is configured to for supplying combustion
Expect gas, fuel gas is to heat the catalyst in regenerator 2.The equipment has pipe 23 and 24, is used for from reactor-again
Equilibrium catalyst is removed in raw device system, the end of the pipe is connected to port 25 and 26, for arriving the catalyst charge
In the pipe for contacting gas 9 and/or regeneration gas 10 of the upstream of recovery heat exchanger 11 and 12.The cloth of cyclone separator 20 and 21
It sets in the downstream of heat exchanger 11,12, and is equipped with pipe 27 and 28, the catalyst for that will retain is back to reactor 1 and regenerates
The fluidized bed of device 2.
In the apparatus, it is connected to for removing the pipe 23 of equilibrium catalyst from system for making catalyst from regeneration
Device 2 is recycled to the port 29 on the pipe 8 of reactor 1, and the pipe 24 for removing equilibrium catalyst is connected to setting and is regenerating
Port 30 in the fluidized bed region of device.Here, for returning to catalyst (it is trapped in external cyclone 20)
The end of pipe 27 be connected to the port 31 that the fluidized bed top of reactor is set, for making catalyst, (it is trapped within outer
In portion's cyclone separator 21 and collect in hopper 22) end of pipe 28 that returns is connected on the fluidized bed that regenerator is arranged in
The port 32 in portion.
Pipe for returning to the catalyst pulp from the device (washer 13) for wet type retention catalyst dust
16 are connected to the port 33 that the fluidized bed top of regenerator is arranged in.
For returning the catalyst dust being trapped in the device (electrofilter 14) for dry type retention from regeneration gas
The pipe 15 returned is connect with for the pipe 28 by the catalyst being trapped in external cyclone 21 back to regenerator.
The fluidized bed of catalyst is divided with horizontal grate in reactor and regenerator.
The equipment is by following operation.Hydrocarbon raw material (alkane) steam is by 5 supplied reactor of pipe below catalyst fluidized bed
1.Raw material vapor is by the fluidized bed (it is divided with horizontal grate) of reactor 1, with the catalyst adverse current recycled downwards.It generates
Contact gas further passes through the separated space (disengaging space) of reactor 1, and will carry secretly from fluidized bed
Catalyst fines leave reactor after being trapped in cyclone separator 3.The catalyst fines being trapped in cyclone separator 3 are logical
Dust discharge dipleg 4 is crossed back to the top of fluidized bed in reactor.In addition, the contact gas with desorption temperature is supplied by pipe 9
It is given in heat recovery heat exchanger 11 and is cooled down, then pass through external cyclone 20 first and further pass through washer
13, the washer 13 is used for the washing from contact gas and removes the tar formed in catalyst dust and dehydrogenating technology.
Then contact gas is added in the unit for being used to be condensed and separate as the alkene of dehydrogenation target product.
Air supplies regenerator 2 by the pipe 6 below fluidized bed.By the fluidized bed of regenerator, (it uses horizontal grate to air
Segmentation), with the catalyst adverse current recycled downwards.The regeneration gas generated in this way passes through the separated space of regenerator 2, and is inciting somebody to action
The catalyst fines carried secretly from fluidized bed leave regenerator after being trapped in cyclone separator 3.Catalyst fines are trapped within rotation
In wind separator 3, and pass through the fluidized bed top that dust discharge dipleg 4 returns to regenerator 2.In addition, will have regeneration by pipe 10
The regeneration gas of temperature is supplied in heat recovery heat exchanger 12 and is cooled down, and then passes through external cyclone 21 first,
Then by electrofilter 14, the electrofilter 14 is used for the Cress from regeneration gas and removes catalyst dust, then
Regeneration gas is discharged into the atmosphere by chimney.Fuel gas by pipe 19 supply regenerator fluidized bed top, burning with
The catalyst of heat cycles simultaneously provides heat for the heat absorption dehydrogenation reaction in reactor 1.Herein, in the fluidized bed of reactor 1
Scenario earthquake, so that the temperature on fluidized bed top is higher than the temperature of fluidized bed lower part.In regenerator 2, fluidized bed it is upper
Temperature of the temperature in portion (fuel gas area) also above fluidized bed lower part.It consumes in reactor 1 and de- due to absorbing heat
Hydrogen reaction and catalyst with a lower temperature by means of the air supplied by pipe 17 by the pipe 7 for recycling catalyst, from
The fluidized bed lower part of regenerator 2 is transferred to fluidized bed top.The catalyst of regeneration and heating is former by means of the hydrocarbon supplied by pipe 18
Material (paraffin vapor) is transferred to the fluidisation of reactor by the pipe 8 for recycling catalyst from the fluidized bed lower part of regenerator 2
Bed top.A part of the equilibrium catalyst recycled in reactor-regenerator system passes through port 29 and pipe 23 periodically
Or continuously taken out from pipe 8, and pipe 9 is entered by port 25, so that contact gas enters the entrance of recovery heat exchanger 11.
Equilibrium catalyst is occurs either periodically or continuously taken out from the fluidized bed of regenerator by port 30 and pipe 24, and passes through port 26
Into pipe 10, so that regeneration gas enters the entrance of recovery heat exchanger 12.Coarse grain equilibrium catalyst with from fluidized bed carry secretly
The pipe side that catalyst dust passes through recovery heat exchanger 11,12 together enters contact gas stream and regeneration gas stream, will be catalyzed
Agent dust deposit is removed from the inner surface of the pipe in recovery heat exchanger.It is produced by periodical or without interruption equilibrium catalyst
On the inner surface for the pipe that raw " sandblasting " effect prevents catalyst dust to be deposited in recovery heat exchanger 11,12, and exclude
Catalyst dust blocking pipe, it reduce therefore yields that the pressure in reactor 1 simultaneously improves alkene.This improves recycling heat
Heat transfer efficiency (heat transfer coefficient) in exchanger, to promote the recuperation of heat of higher degree.For example, when using recycling boiler
When, steam generation increases.
Fig. 2 shows the curve graphs of more high heat transfer coefficient in recycling boiler, and the recycling boiler erection is in equipment for connecing
On the pipe for touching gas, which is used for dehydrogenation of isobutane and equilibrium catalyst is periodically fed to boiler inlet.From the song
Line chart can be seen that during blocking pipe, and when equilibrium catalyst is fed to boiler inlet, heat transfer coefficient increases sharply,
And when feeding termination, heat transfer coefficient is gradually reduced.When the supply for entering reactor is the 10% of raw material flow rate, cleaning
Boiler is in acceptable heat exchange level (at least 52kcal/m after pipe2HK the working time) is 21 days, when for 5%,
Steaming hour is 16 days.Here, balance between supply and demand catalyst is to clean the duration of recycling boiler tube as 7 hours.For
With the 10% of raw material flow rate, 5% and 1% by equilibrium catalyst be sent into reactor, it can be achieved that heat transfer coefficient be respectively 66kcal/
m2·h·K、64kcal/m2HK and 60kcal/m2·h·K.In view of the catalyst of fluidized bed lower part is coarse grained potential
Separation removes equilibrium catalyst from system to clean the pipe of recovery heat exchanger and preferably carry out from the lower part of fluidized bed.Consider
To sandblasting effect is strengthened, thicker catalyst is preferably supplied for removing catalyst dust deposit from pipe.It is urged from described
The distance of the point of agent charging to heat exchanger is 1 to 12 times of pipe diameter, makes the catalyst of charging and contacts gas stream and again
Raw even mixing, and it is uniformly distributed the equilibrium catalyst of charging along the pipe of heat exchanger 11,12.It is handed in recuperation of heat heat
Model of the retention efficiency of the equilibrium catalyst fed in the external cyclone 20,21 of parallel operation arranged downstream 40% to 99%
In enclosing, and the catalyst for providing acceptable level returns to reactor-regenerator system.Due to (the catalysis of fluidized bed top
Agent returns to area) temperature be controlled so as to the temperature more than fluidized bed remainder (lower part), therefore it is preferred that in reactor 1 and regenerator
The horizontal place of the 86-98% of fluidized bed height makes catalyst pulp and the retention with a lower temperature due to heat loss in 2
Catalyst returns.Fuel gas is supplied to control the temperature on fluidized bed top in regenerator 2 by pipe 19, and is supplied by pipe 8
The temperature on fluidized bed top in reactor 1 is controlled to the recycling catalyst overheated in a regenerator.Herein, it is catalyzed in fluidized bed
The range that agent returns to area does not influence the Temperature Distribution of the fluidized bed height along reactor and regenerator, promotes dehydrogenation and urges
The stabilization of agent regeneration technology.In order to provide the safety condition of dehydrogenating technology, for flat by the recycling of recovery heat exchanger pipe
(equilibrium catalyst is taken out from system, catalyst is supplied to clean the pipe of recovery heat exchanger, incites somebody to action in two circuits of weighing apparatus catalyst
Catalyst is trapped in external cyclone, and makes the catalyst of retention back to reactor-regenerator system) it should belong to
Reactor assembly or regenerator system, as shown in the flowchart (Fig. 1).The preferred disposition of external cyclone in secured shell
Also provide better process safety condition.
Technological achievement is: claimed equipment is improved by reducing the blocking of the heat exchanger as caused by catalyst dust
The technology and economic performance of dehydrogenating technology, the production capacity for stabilizing the operation of dehydrogenation unit and increasing alkene, the heat
Exchanger is used to recycle the heat of contact gas and regeneration gas.
Preferred forms of the invention
The embodiment of present invention disclosed above is optimal.
Industrial applicibility
What is proposed is used for dehydrogenation C3-C5The equipment of alkane can be used for producing polypropylene, methyl tertiary butyl ether(MTBE) etc..
Claims (11)
1. one kind is used for C3-C5Paraffin dehydrogenation is the equipment of corresponding alkene, and the equipment includes: reactor (1) and regeneration
Device (2), the reactor (1) and regenerator (2) have the fluidized bed of particulate chromia-alumina catalyst；(7), (8) are managed,
The pipe (7), (8) are for making equilibrium catalyst from reactor cycles to regenerator, and vice versa；It manages (5), the pipe (5) is used
In by raw material supply to reactor；With pipe (6), the pipe (6) is for supplying air to regenerator；Gas is contacted for removing
(9) and the pipe of regeneration gas (10), the pipe are connected to setting in the cyclonic separation on the top of reactor (1) and regenerator (2)
Device (3)；Shell and tube heat exchanger (11), (12), the shell and tube heat exchanger (11), (12) installation on the tube, so as to
The heat of these gases is recycled when contacting gas and regeneration gas is fed into the pipe side of heat exchanger；With wet type device for trapping
(13) and dry type device for trapping (14), described device are used to retain the catalyst powder of entrainment from contact gas and regeneration gas
Dirt,
It is characterized in that, the equipment includes system, the system is used for equilibrium catalyst from reactor-regenerator system
It is supplied to the pipe side entrance of shell and tube heat exchanger (11), (12)；Device, described device come from shell-tube type heat exchange for retaining
The contact gas of device pipe side and/or the catalyst in regeneration gas exit, and by the catalyst of retention back to reactor and/or
The top of the fluidized bed of regenerator.
2. equipment according to claim 1, which is characterized in that enter for equilibrium catalyst to be supplied to recovery heat exchanger
The system of mouth is equipped with pipe (23), (24), and the pipe (23), (24) are for removing equilibration catalyst from reactor-regenerator system
Agent, the end of the pipe be used to for the catalyst being supplied to the heat exchanger (11), (12) that are used for recuperation of heat upstream, use
In the pipe of contact gas (9) and/or regeneration gas (10), wherein the end is separated with heat exchanger (11), (12), every
The distance opened is 1 to 12 times for contacting the pipe diameter of gas (9) and/or regeneration gas (10), wherein external cyclonic separation
Device (20), (21) setting are in the downstream of heat exchanger (11), (12), and the external cyclone is equipped with pipe (27), (28), institute
State pipe (27), (28) are used to make the level of the catalyst 86-98% of fluidized bed height in reactor and/or regenerator carried secretly
Place returns in the fluidized bed of reactor and/or regenerator.
3. equipment according to claim 1, which is characterized in that for removing equilibration catalyst from reactor-regenerator system
The port (29) or be connected to the port being arranged in the fluidized bed region of reactor (1) that the pipe (23) of agent is connected on pipe (8),
The pipe (8) is for making catalyst be recycled to reactor (1) from regenerator (2), wherein for supplying the pipe (23) of catalyst
End is connected to port (25) of the setting on the pipe for contacting gas (9).
4. equipment according to claim 1, which is characterized in that for removing equilibration catalyst from reactor-regenerator system
The port or be connected to the port (30) being arranged in the fluidized bed region of regenerator (2) that the pipe (24) of agent is connected on pipe (7),
The pipe (7) is for making catalyst be recycled to regenerator (2) from reactor (1), wherein for supplying the pipe (24) of catalyst
End is connected to port (26) of the setting on the pipe for regeneration gas (10).
5. equipment according to claim 1, which is characterized in that for by the external whirlwind on the pipe for being used to contact gas
The pipe (27) that the catalyst retained in separator (20) returns is connected to the port (31) in the fluidized bed region of reactor (1).
6. equipment according to claim 1, which is characterized in that for by the external whirlwind on the pipe for being used for regeneration gas
The pipe (28) that the catalyst retained in separator (21) returns is connected to the port (32) in the fluidized bed region of regenerator (2).
7. equipment according to claim 1, which is characterized in that for making from the dress for wet type retention catalyst dust
The catalyst pulp for setting (13) send the pipe (16) returned to be connected to setting in regenerator at the horizontal place of the 86-98% of fluidized bed height
(2) port (33) in fluidized bed.
8. equipment according to claim 1, which is characterized in that the device for making to carry out self-drying type retention catalyst dust
(14) catalyst dust send the pipe (15) returned to be connected to setting in regenerator at the horizontal place of the 86-98% of fluidized bed height
(2) port (32) in fluidized bed.
9. equipment according to claim 1, which is characterized in that for supplying catalyst to the shell-side of recovery heat exchanger
The system of entrance includes independent hopper, and the hopper is for measuring and supplying balance and/or fresh dehydrogenation
Cleaning pipe.
10. equipment according to any one of claim 1 to 9, which is characterized in that in the pipeline for contacting gas
External cyclone (20) is configured to the cyclone separator group in secured shell.
11. equipment according to any one of claim 1 to 9, which is characterized in that in the pipeline for regeneration gas
External cyclone (21) is configured to one or more cyclone separators of parallel arrangement.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| RU2017114893 | 2017-04-26 | ||
| RU2017114893A RU2638934C1 (en) | 2017-04-26 | 2017-04-26 | Installation of dehydration of paraffin hydrocarbons c3-c5 |
| PCT/RU2018/000214 WO2018199805A1 (en) | 2017-04-26 | 2018-04-03 | Plant for dehydrogenating c3-c5 paraffin hydrocarbons |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110325495A true CN110325495A (en) | 2019-10-11 |
Family
ID=60718639
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201880013179.0A Pending CN110325495A (en) | 2017-04-26 | 2018-04-03 | For dehydrogenation C3-C5The equipment of alkane |
Country Status (3)
| Country | Link |
|---|---|
| CN (1) | CN110325495A (en) |
| RU (1) | RU2638934C1 (en) |
| WO (1) | WO2018199805A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2024059600A1 (en) * | 2022-09-14 | 2024-03-21 | Dow Global Technologies Llc | Methods for dehydrogenating hydrocarbons utilizing regenerators |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2129111C1 (en) * | 1998-01-05 | 1999-04-20 | Открытое акционерное общество Научно-исследовательский институт "Ярсинтез" | Plant for dehydrogenation of paraffin hydrocarbons c3-c5 |
| CN103214333A (en) * | 2013-05-10 | 2013-07-24 | 神华集团有限责任公司 | System and process for gas-solid separation and heat exchange of alkene product prepared from organic oxygen-containing compound |
| CN103449948A (en) * | 2012-06-01 | 2013-12-18 | 中国石油天然气集团公司 | Method for preparing olefin through dehydrogenating alkane |
| CN103539610A (en) * | 2012-07-09 | 2014-01-29 | 中国石油化工集团公司 | Device for producing alkene from oxygenated compound |
| CN105585400A (en) * | 2014-10-20 | 2016-05-18 | 中国石油化工股份有限公司 | Method for preparing light olefin from light alkane |
| RU2591159C1 (en) * | 2015-06-03 | 2016-07-10 | Публичное Акционерное Общество "Нижнекамскнефтехим" | Plant for dehydrogenation of paraffins or isoparaffins c3-c5 in chromia-alumina catalyst fluidised bed |
-
2017
- 2017-04-26 RU RU2017114893A patent/RU2638934C1/en active
-
2018
- 2018-04-03 WO PCT/RU2018/000214 patent/WO2018199805A1/en active Application Filing
- 2018-04-03 CN CN201880013179.0A patent/CN110325495A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2129111C1 (en) * | 1998-01-05 | 1999-04-20 | Открытое акционерное общество Научно-исследовательский институт "Ярсинтез" | Plant for dehydrogenation of paraffin hydrocarbons c3-c5 |
| CN103449948A (en) * | 2012-06-01 | 2013-12-18 | 中国石油天然气集团公司 | Method for preparing olefin through dehydrogenating alkane |
| CN103539610A (en) * | 2012-07-09 | 2014-01-29 | 中国石油化工集团公司 | Device for producing alkene from oxygenated compound |
| CN103214333A (en) * | 2013-05-10 | 2013-07-24 | 神华集团有限责任公司 | System and process for gas-solid separation and heat exchange of alkene product prepared from organic oxygen-containing compound |
| CN105585400A (en) * | 2014-10-20 | 2016-05-18 | 中国石油化工股份有限公司 | Method for preparing light olefin from light alkane |
| RU2591159C1 (en) * | 2015-06-03 | 2016-07-10 | Публичное Акционерное Общество "Нижнекамскнефтехим" | Plant for dehydrogenation of paraffins or isoparaffins c3-c5 in chromia-alumina catalyst fluidised bed |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2024059600A1 (en) * | 2022-09-14 | 2024-03-21 | Dow Global Technologies Llc | Methods for dehydrogenating hydrocarbons utilizing regenerators |
Also Published As
| Publication number | Publication date |
|---|---|
| RU2638934C1 (en) | 2017-12-19 |
| WO2018199805A1 (en) | 2018-11-01 |
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Application publication date: 20191011 |