CN205528515U - Device of methyl alcohol system alkene - Google Patents
Device of methyl alcohol system alkene Download PDFInfo
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- CN205528515U CN205528515U CN201620250157.4U CN201620250157U CN205528515U CN 205528515 U CN205528515 U CN 205528515U CN 201620250157 U CN201620250157 U CN 201620250157U CN 205528515 U CN205528515 U CN 205528515U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
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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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
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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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
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Abstract
The utility model discloses a device of methyl alcohol system alkene belongs to the chemical industry equipment field. The device includes fast fluidized bed reactor and regenerator, reaction zone or tamper in it, the CA collecting region, the dilute -phase zone, feed distribution ware in the reaction zone, mix the CA distributor, extrinsic cycle CA distributor, CA subdividing orchestration, with mix the CA blender that the CA distributor is connected, get the calorimeter outward with the reactor that reactor dilute -phase zone and CA blender are connected, the extrinsic cycle pipe of being connected with low activity CA collecting region and extrinsic cycle CA distributor, main wind distributor in the tamper, extrinsic cycle CA distributor, low activity CA distributor, cold back CA distributor, CA subdividing orchestration, the extrinsic cycle pipe of being connected with regeneration CA collecting region and extrinsic cycle CA distributor, low activity CA stripping stage, regeneration CA stripping stage, the calorimeter is got outward to the regenerator, CA and reaction gas separator, CA and flue gas separation ware, cyclone in reactor dilute -phase zone and the regenerator dilute -phase zone.
Description
Technical field
This utility model relates to field of chemical equipment, particularly to the device of a kind of methanol-to-olefins.
Background technology
Along with the development of Chinese national economy, the demand of the low-carbon alkene such as ethylene, propylene is day by day climbed by modern chemical industry
Rise, wherein, produce methanol-to-olefins (the Methanol to of the low-carbon alkene such as ethylene, propylene with methanol for raw material
Olefins, MTO) technology, it has, and response speed is fast, thermal discharge big, selectivity of light olefin high, by more and more
Many attractes attention.Visible, it is provided that the device of a kind of methanol-to-olefins is the most necessary.
Prior art provides the device of such a methanol-to-olefins, this methanol-to-olefins include reactor, regeneration
Device, regenerated catalyst stripping section, reclaimable catalyst stripping section, reactor external warmer, regenerator SAPMAC method external warmer, regeneration
Device external warmer, sets gradually bottom-up in described reactor and divides outside reactor feed distributor, cold regenerated catalyst device
The distributor, reactor external warmer catalyst distributor, reactor grid and the catalyst that prop up and reaction gas segregation apparatus, institute
Regenerator main air distributor, the distributor of reclaimable catalyst Qi Wai branch, regeneration is set gradually bottom-up in stating regenerator
Device grid, described regenerator SAPMAC method external warmer connect with regenerated catalyst stripping section after with described cold regenerated catalyst device outside
The distributor of branch connects, and described reclaimable catalyst stripping section is connected with the distributor of described reclaimable catalyst Qi Wai branch.
But, designer finds that prior art at least there is problems in that
In the device of the methanol-to-olefins that prior art provides, reactor mostly is bubble bed reactor, and course of reaction is for passing
Quality Control system, while ensureing conversion ratio, the longer response time can cause the rear reaction of alkene, is substantially reduced selecting response
Property.It addition, can within it produce district of localized hyperthermia, autoreaction after the regenerated catalyst entrance reactor bed that regenerator is derived
The cold rear catalyst that device external warmer returns can within it produce district of topical hypothermia after entering reactor bed, and above each factor is equal
The selectivity of reaction can be reduced.
Utility model content
This utility model embodiment technical problem to be solved is, it is provided that one is anti-after making to avoid alkene
Should, and district of localized hyperthermia and low-temperature space occur to improve the dress of the methanol-to-olefins of reaction selectivity in avoiding reactor bed
Put.Concrete technical scheme is as follows:
This utility model embodiment provides the device of a kind of methanol-to-olefins, and described device includes that fast fluidized bed reacts
Device, by lower from the reaction zone being above successively set within described fast fluidized bed reactor, low activity catalyst collecting region, reaction
Device dilute-phase zone, fast fluidized bed regenerator, by lower from the renewing zone being above successively set on described fast fluidized bed internal regenerator,
Regenerated catalyst collecting region, regenerator dilute-phase zone, by lower methanol feed distributor in being above successively set on described reaction zone,
Mixed catalyst distributor, the first circulating catalyst distributor, the first catalyst redistributor, divide with described mixed catalyst
The catalyst blender that cloth device connects, upper and lower side is anti-with what described reactor dilute-phase zone and described catalyst blender were connected respectively
Answering device external warmer, upper and lower side connects with described low activity catalyst collecting region and described first circulating catalyst distributor respectively
The first outer circulating tube connect, by lower main air distributor in being above successively set on described renewing zone, the second circulating catalyst
Distributor, low activity catalyst distributor, cold rear catalyst distributor, the second catalyst redistributor, upper and lower side respectively with institute
State regenerated catalyst collecting region and described second circulating catalyst distributor connect the second outer circulating tube, upper and lower side respectively with
The low activity catalyst stripping section that described low activity catalyst collecting region and described low activity catalyst distributor connect, upper and lower side
The regenerated catalyst stripping section being connected with described regenerated catalyst collecting region and described catalyst blender respectively, upper and lower side is respectively
The external catalyst cooler for regenerator being connected with described regenerator dilute-phase zone and described cold rear catalyst distributor, upper and lower side lays respectively at institute
Stating catalyst and the reaction gas separator of reactor dilute-phase zone and described low activity catalyst collecting region, upper and lower side lays respectively at institute
State regenerator dilute-phase zone and the catalyst of described regenerated catalyst collecting region and smoke separator, be arranged on described reactor dilute phase
In district and the top cyclone separator that is connected and reaction gas three-stage cyclone separator, in being arranged on described regenerator dilute-phase zone and phase
One secondary cyclone of connection and regenerated flue gas three-stage cyclone separator.
Specifically, as preferably, reducer that described catalyst includes with reaction gas separator sequentially connecting from upper by lower,
Dilute phase pipe and thick cyclone separator；
The lower end of described reducer and described dilute phase pipe is respectively positioned in described low activity catalyst collecting region, described dilute phase pipe
Lower end more than part be positioned at described reactor dilute-phase zone, described thick cyclone separator top is provided with has air inlet
First riser, and described first riser is connected with described top cyclone separator.
Specifically, as preferably, described reaction gas three-stage cyclone separator part is positioned at inside described reactor dilute-phase zone,
Another part is positioned at outside described reactor dilute-phase zone, and is positioned at the three grades of whirlwind of reaction gas outside described reactor dilute-phase zone
The top of separator is provided with purification letter shoot, is positioned at the reaction gas three-stage cyclone separator within described reactor dilute-phase zone
Bottom be provided with fine powder delivery line, for the dead catalyst fine powder of regeneration being derived outside described fast fluidized bed reactor.
Specifically, as preferably, cyclone separator top, described top is provided with the second riser, described top cyclone separator
It is connected with the described reaction gas three-stage cyclone separator being positioned within described reactor dilute-phase zone by described second riser.
Specifically, as preferably, the bottom of described catalyst blender is provided with lifting medium inlet, and described catalyst
Blender by the first inclined tube and the second inclined tube respectively with described reactor external warmer and described regenerated catalyst stripping section phase
Connect, and described reactor external warmer is connected with described low activity catalyst collecting region by the 3rd inclined tube；
Be provided with first time guiding valve on described first inclined tube, described 3rd inclined tube be provided with guiding valve on first, described instead
The top answering device external warmer is provided with the first catalyst level-sensing device being connected with the guiding valve signal of telecommunication on described first, described reaction
The first temperature sensor being connected with described first time guiding valve signal of telecommunication it is provided with on the wall in district.
Specifically, as preferably, described regenerated flue gas cyclone separator part is positioned at inside described regenerator dilute-phase zone, separately
An outer part is positioned at outside described regenerator dilute-phase zone；
The top of a described secondary cyclone is provided with the 3rd riser, and described 3rd riser be positioned at described
Described regenerated flue gas cyclone separator within regenerator dilute-phase zone is connected；
It is positioned at the described regenerated flue gas cyclone separator top outside described regenerator dilute-phase zone and is provided with purifying regeneration cigarette
Letter shoot.
Specifically, as preferably, the top of described external catalyst cooler for regenerator is by the 4th inclined tube and described regenerated catalyst
Collecting region connects, and described 4th inclined tube is provided with guiding valve on second, and described external catalyst cooler for regenerator top is additionally provided with and institute
State the second catalyst level-sensing device that on second, the guiding valve signal of telecommunication connects；
The bottom of described external catalyst cooler for regenerator is connected with described cold rear catalyst distributor by the 5th inclined tube, and described the
It is provided with second time guiding valve on five inclined tubes, the wall of described regenerated catalyst collecting region is provided with and described second time guiding valve telecommunications
Number connect the second temperature sensor.
Specifically, as preferably, 1-5 described first catalyst redistributor is intervally installed in the horizontal direction, and
The porosity of the first catalyst redistributor is 60-90%；
1-5 described second catalyst redistributor is intervally installed in the horizontal direction, and the reallocation of the second catalyst
The porosity of device is 60-90%.
The technical scheme that this utility model embodiment provides has the benefit that
The device of the methanol-to-olefins that this utility model embodiment provides, the fast fluidized bed strengthened by employing is reacted
Device, and make top cyclone separator be joined directly together logical with catalyst with reaction gas separator, it is possible in time separating reaction gas with urge
Agent, significantly reduces the post-reacted generation of alkene.By use catalyst blender respectively with mixed catalyst distributor, reaction
Device external warmer and regenerated catalyst stripping section are connected, can be by regenerated catalyst with by the return after cold of reactor external warmer
It is evenly distributed on the bottom of reaction zone after low temperature catalyst mixing again by mixed catalyst distributor, so can be prevented effectively from anti-
District of localized hyperthermia and low-temperature space occur in answering device bed.By arranging the first circulating catalyst distributor and in reaction zone
One catalyst redistributor, and arrange in renewing zone the second circulating catalyst distributor, low activity catalyst distributor,
Cold rear catalyst distributor and the second catalyst redistributor, can not only ensure reactant and the temperature of catalyst and activity uniformly
Distribution, and can guarantee that reacting gas and catalyst contact effect.From the foregoing, above each factor all can help improve reaction
Selectivity.
Accompanying drawing explanation
In order to be illustrated more clearly that the technical scheme in this utility model embodiment, required in embodiment being described below
Accompanying drawing to be used is briefly described, it should be apparent that, the accompanying drawing in describing below is only realities more of the present utility model
Execute example, for those of ordinary skill in the art, on the premise of not paying creative work, it is also possible to according to these accompanying drawings
Obtain other accompanying drawing.
Fig. 1 is the structural representation of the device of the methanol-to-olefins that this utility model embodiment provides.
Reference represents respectively:
1 reactor,
101 reaction zones, 102 low activity catalyst collecting regions, 103 reactor dilute-phase zones,
2 regeneratoies,
201 renewing zones, 202 regenerated catalyst collecting regions, 203 regenerator dilute-phase zones,
3 methanol feed distributors,
4 mixed catalyst distributors,
5 first circulating catalyst distributors,
6 first catalyst redistributors,
7 catalyst blenders,
8 reactor external warmers,
9 first outer circulating tubes,
10 main air distributors,
11 second circulating catalyst distributors,
12 low activity catalyst distributors,
13 cold rear catalyst distributors,
14 second catalyst redistributors,
15 second outer circulating tubes,
16 low activity catalyst stripping sections,
17 regenerated catalyst stripping sections,
18 external catalyst cooler for regenerators,
19 catalyst and reaction gas separator,
191 reducers, 192 dilute phase pipes, 193 thick cyclone separator, 194 first riseies,
20 catalyst and smoke separator,
21 top cyclone separator,
22 reaction gas three-stage cyclone separators,
23 1 secondary cyclones,
24 regenerated flue gas three-stage cyclone separators,
25 purify letter shoot,
26 fine powder delivery lines,
27 second riseies,
28 promote medium inlet,
29 first inclined tubes,
30 second inclined tubes,
31 the 3rd inclined tubes,
32 the 3rd riseies,
33 purifying regeneration flue gas delivery pipe,
34 the 4th inclined tubes,
35 the 5th inclined tubes.
Detailed description of the invention
For making the purpose of this utility model, technical scheme and advantage clearer, new to this practicality below in conjunction with accompanying drawing
Type embodiment is described in further detail.
This utility model embodiment provides the device of a kind of methanol-to-olefins, and as shown in Figure 1, this device includes quickly
Fluidized-bed reactor 1, by lower from the reaction zone 101 being above successively set within fast fluidized bed reactor 1, low activity catalyst
Collecting region 102, reactor dilute-phase zone 103.This device also includes fast fluidized bed regenerator 2, by lower from be successively set on fast
Speed renewing zone 201 within fluid bed regenerator 2, regenerated catalyst collecting region 202, regenerator dilute-phase zone 203, by lower from depend on
Secondary be arranged in reaction zone 101 methanol feed distributor 3, mixed catalyst distributor the 4, first circulating catalyst distributor
5, the first catalyst redistributor 6.Further, this device also includes that the catalyst being connected with mixed catalyst distributor 4 mixes
Clutch 7, the reactor external warmer 8 that upper and lower side is connected with reactor dilute-phase zone 103 and catalyst blender 7 respectively, upper and lower side
The first outer circulating tube 9 being connected with low activity catalyst collecting region 102 and the first circulating catalyst distributor 5 respectively, by under
Main air distributor the 10, second circulating catalyst distributor 11 in being above successively set on renewing zone 201, low activity catalyst
Distributor 12, cold rear catalyst distributor the 13, second catalyst redistributor 14.This device this include upper and lower side respectively with regeneration
The second outer circulating tube 15 that catalyst collection district 202 and the second circulating catalyst distributor 11 connect；Upper and lower side is respectively with low
The low activity catalyst stripping section 16 that active catalyst collecting region 102 and low activity catalyst distributor 12 connect；Upper and lower side divides
The regenerated catalyst stripping section 17 not being connected with regenerated catalyst collecting region 202 and catalyst blender 7；Upper and lower side respectively with again
The external catalyst cooler for regenerator 18 that raw device dilute-phase zone 203 and cold rear catalyst distributor 13 connect；Upper and lower side lays respectively at reactor
The catalyst of dilute-phase zone 103 and low activity catalyst collecting region 102 and reaction gas separator 19；Upper and lower side lays respectively at regenerator
The catalyst of dilute-phase zone 203 and regenerated catalyst collecting region 202 and smoke separator 20；It is arranged in reactor dilute-phase zone 103
And the top cyclone separator 21 that is connected and reaction gas three-stage cyclone separator 22；In being arranged on regenerator dilute-phase zone 203 and phase
One secondary cyclone 23 of connection and regenerated flue gas three-stage cyclone separator 24.
It is understood that the fast fluidized bed reactor described in this utility model embodiment and fast fluidized bed regeneration
Device is the prior art that this area is common, and its respective internal structure is not made concrete restriction by this utility model embodiment.
It addition, " catalyst " can be referred to as CA in this utility model embodiment.For example, low activity catalyst collecting region 102
Low activity CA collecting region can also be write a Chinese character in simplified form into.
The device of the methanol-to-olefins that this utility model embodiment provides, the fast fluidized bed reactor strengthened by employing
1, and make top cyclone separator 21 be joined directly together logical with catalyst with reaction gas separator 19, it is possible in time separating reaction gas with
Catalyst, significantly reduces the post-reacted generation of alkene.By use catalyst blender 7 respectively with mixed catalyst distributor 4,
Reactor external warmer 8 and regenerated catalyst stripping section 17 are connected, can be by regenerated catalyst and cold by reactor external warmer 8
The bottom of reaction zone 101 it is evenly distributed on again by mixed catalyst distributor 4, so after the low temperature catalyst mixing of rear return
District of localized hyperthermia and low-temperature space occur in can being prevented effectively from reactor bed.By arranging the first outer circulation in reaction zone 101
Catalyst distributor 5 and the first catalyst redistributor 6, and the second circulating catalyst distribution is set in renewing zone 201
Device 11, low activity catalyst distributor 12, cold rear catalyst distributor 13 and the second catalyst redistributor 14, can not only ensure
Reactant and the temperature of catalyst and activity are uniformly distributed, and can guarantee that reacting gas and catalyst contact effect.By above-mentioned
Understanding, above each factor all can help improve the selectivity of reaction.
Further, this catalyst includes reducer 191, the dilute phase sequentially connected from upper by lower with reaction gas separator 19
Pipe 192 and thick cyclone separator 193.Wherein, the lower end of reducer 191 and dilute phase pipe 192 is respectively positioned on low activity catalyst collection
In district 102, the part more than lower end of dilute phase pipe 192 is positioned at reactor dilute-phase zone 103, and thick cyclone separator 193 top sets
It is equipped with first riser 194 with air inlet, and the first riser 194 is connected with top cyclone separator 21.By as above
Arrange, when reacting gas autoreaction district 101 is up in catalyst and reaction gas separator 19, catalyst can be carried out with anti-
Should the sharp separation of gas, reduce contacts that both are unnecessary, i.e. accelerate the discharge of reaction gas and the separation of catalyst dust,
React odds after being more conducive to reduce alkene, improve the selectivity of reaction.The most specifically, at the first riser 194
Top air inlet is set, the pressure drop of this air inlet is 500-4000Pa, for example, 800Pa, 1000Pa, 1500Pa, 2000Pa,
2500Pa, 3000Pa, 3500Pa etc., so can ensure the low activity catalyst stripping gas in reactor dilute-phase zone 103 and low
The fluidizing gas of active catalyst collecting region 102 carries out quick dust and gas by this air inlet entrance top cyclone separator 21 and divides
From.
As preferably, it is internal that reaction gas three-stage cyclone separator 22 part is positioned at reactor dilute-phase zone 103, another part
It is positioned at reactor dilute-phase zone 103 outside, by as set above, on the one hand can reduce accounting for of reaction gas three-stage cyclone separator 22
Ground, saves basis and structure is invested, and can ensure the reaction gas three-stage cyclone separator being positioned within reactor dilute-phase zone 103
22 can be joined directly together with top cyclone separator 21, it is achieved that the shortest connection and minimum elbow between the two are arranged, it is ensured that anti-
The pressure drop answering gas flow is minimum.Further, the reaction gas three-stage cyclone separation outside reactor dilute-phase zone 103 it is positioned at
The top of device 22 is provided with purification letter shoot 25, can be delivered in the upstream device of outside treat by the gas that purifies after separating
Process.Meanwhile, the bottom being positioned at the reaction gas three-stage cyclone separator 22 within reactor dilute-phase zone 103 is provided with fine powder derivation
Pipe 26, outside for dead catalyst fine powder is derived fast fluidized bed reactor 1.It is understood that this fine powder delivery line 26
Can be through the wall of reactor dilute-phase zone 103 until upstream device, or interior through reaction gas three-stage cyclone separator 22
Portion is until upstream device.
Specifically, cyclone separator 21 top, top is provided with the second riser 27, and top cyclone separator 21 is by second liter
Trachea 27 is connected with the reaction gas three-stage cyclone separator 22 being positioned within reactor dilute-phase zone 103.By arranging second liter
Trachea 27 can realize being joined directly together of the beeline between top cyclone separator 21 and reaction gas three-stage cyclone separator 22.
Further, in this utility model embodiment, the bottom of catalyst blender 7 is provided with lifting medium inlet 28,
And catalyst blender 7 by the first inclined tube 29 and the second inclined tube 30 respectively with reactor external warmer 8 and regenerated catalyst vapour
The section of carrying 17 is connected, and reactor external warmer 8 is connected with low activity catalyst collecting region 102 by the 3rd inclined tube 31.Logical
Cross catalyst blender 7 by SA with the low temperature returned by reactor external warmer 8 for highly active for high temperature regenerated catalyst
Cold rear catalyst mix homogeneously, it is ensured that mixed catalyst will not occur local in reaction zone 101 when entering reaction zone 101
High temperature or topical hypothermia, thus improve reaction selectivity.
Further, the first inclined tube 29 is provided with first time guiding valve, the 3rd inclined tube 31 is provided with guiding valve on first, instead
The top answering device external warmer 8 is provided with the first catalyst level-sensing device being connected with the guiding valve signal of telecommunication on first, reaction zone 101
The first temperature sensor being connected with first time guiding valve signal of telecommunication it is provided with on wall.This utility model embodiment is by using first
Upper guiding valve controls the first catalyst level-sensing device, and then the material position of control reactor external warmer 8 middle and upper part catalyst, can be significantly
Degree reduces catalyst to the thermal shock of heat-exchanging tube bundle in reactor external warmer 8 and abrasion, extends making of its internal heat tube bank
Use the life-span.By using the first temperature sensor can measure the temperature of reaction zone 101 in real time, simultaneously according to the temperature of reaction zone 101
Degree, utilizes the catalyst circulating load of first time guiding valve control reactor external warmer 8, and then reaches controllable precise reaction zone 101
The purpose of temperature.
As preferably, in this utility model embodiment, it is dilute that regenerated flue gas three-stage cyclone separator 24 part is positioned at regenerator
Phase region 203 is internal, and it is outside that another part is positioned at regenerator dilute-phase zone 203.It is arranged such and can reduce three grades of whirlwind of regenerated flue gas
The occupation of land of separator 24, saves basis and structure is invested.
It addition, the top of a secondary cyclone 23 is provided with the 3rd riser 32, and the 3rd riser 32 be positioned at
Regenerated flue gas three-stage cyclone separator 24 within regenerator dilute-phase zone 203 is connected, and is arranged such and achieves one or two grades of whirlwind
The shortest between separator 23 with regenerated flue gas three-stage cyclone separator 24 is connected and minimum elbow, it is ensured that regenerated flue gas is two
Flow process pressure drop between person is minimum.It is positioned at the regenerated flue gas three-stage cyclone separator 24 outside regenerator dilute-phase zone 203 to push up
Portion is provided with purifying regeneration flue gas delivery pipe 33, is transported to outside with the flue gas after purifying.Further, regenerated flue gas three grades
The bottom of cyclone separator 24 is provided with regeneration of spent catalyst fine powder delivery line, itself or through the wall of regenerator dilute-phase zone 203
Until upstream device or internal until upstream device through regenerated flue gas three-stage cyclone separator 24.
Specifically, the top of external catalyst cooler for regenerator 18 is connected with regenerated catalyst collecting region 202 by the 4th inclined tube 34,
Be provided with guiding valve on second on 4th inclined tube 34, external catalyst cooler for regenerator 18 top be additionally provided with second on the guiding valve signal of telecommunication even
The the second catalyst level-sensing device connect.By as set above, guiding valve on second can be used to control external catalyst cooler for regenerator 18 internal upper part
The material position of catalyst, and then reduce catalyst to the thermal shock of the heat-exchanging tube bundle in external catalyst cooler for regenerator 18 and abrasion, extend
Its service life.
Further, the bottom of external catalyst cooler for regenerator 18 is by the 5th inclined tube 35 with cold rear catalyst distributor 13 even
Connect, the 5th inclined tube 35 is provided with second time guiding valve, the wall of regenerated catalyst collecting region 202 is provided with and second time guiding valve electricity
The second temperature sensor that signal connects.By as set above, can collect according to the second temperature sensor measurement regenerated catalyst
The temperature in district 202, then feeds back to second time guiding valve, and utilizes the catalyst of second time guiding valve control external catalyst cooler for regenerator 18
Circulating load, and then accurately control regeneration temperature.
Specifically, as preferably, 1-5, such as 2,3,4,5 the first catalyst redistributors 6 are along level side
Be spaced setting to each other, and the porosity of the first catalyst redistributor 6 be 60-90%, for example, 65%, 70%, 75%,
80% etc., it is arranged such, when the first catalyst redistributor 6 arranged in reacting gas and catalyst pass reaction zone 101,
The air pocket in bed can be eliminated, improve the effect that contacts of catalyst and reacting gas, improve the selectivity of reaction.Similarly,
1-5, such as 2,3,4,5 the second catalyst redistributors 14 be intervally installed in the horizontal direction, and second urges
The porosity of agent redistributor is 60-90%, for example, 65%, 70%, 75%, 80% etc., and it is arranged such, works as regenerated flue gas
During with catalyst through the second catalyst redistributor 14, the air pocket in regenerator can be eliminated, it is ensured that catalyst uniformly the most again
Raw.
Specifically, the operation principle of the device of this methanol-to-olefins is as follows:
Methanol feedstock enters in methanol feed distributor 3 to the feed(raw material)inlet bottom fast fluidized bed reactor 1 and carries out all
Even distribution, in the reaction bed subsequently into reaction zone 101, now regenerated catalyst with by reactor external warmer 8 cold after
Enter mixed catalyst distributor 4 after catalyst mixing to carry out being evenly distributed to bottom, reaction zone 101, and contact with methanol feedstock
Reaction, generates the reaction gas rich in low-carbon alkene, such as ethylene and propylene.After reaction gas and participation reaction, the low activity of coking is urged
Agent separates in reaction gas separator 19 through the up catalyst that enters into of the first catalyst redistributor 6.By being catalyzed
The reacting gas that agent and reaction gas separator 19 are separated is directly entered top cyclone separator 21 through thick cyclone separator 193 and enters
Row separates again.In the process, the low activity catalyst stripping gas in reactor dilute-phase zone 103 and low activity catalyst are received
The fluidizing gas in collection district 102 divides entering top whirlwind by the air inlet on the first riser 194 on thick cyclone separator 193
From device 21, then enter reaction gas three-stage cyclone separator 22 together with reacting gas and purify, the reacting gas after purification
Downstream unit will be delivered to by purifying letter shoot 25.
Meanwhile, catalyst and reaction gas separator 19 low activity catalyst separated drains into low activity and urges
Agent collecting region 102, and low activity catalyst is divided into three parts, Part I low activity catalyst to enter instead through the 3rd inclined tube 31
Answering device external warmer 8 to cool down, the catalyst after cooling enters catalyst blender 7 through the first inclined tube 29；Part II
Low activity catalyst enters the first outer circulating tube 9 and is circulated, and is then distributed to reaction through the first circulating catalyst distributor 5
District 101；Part III low activity catalyst enters low activity catalyst stripping section 16, and after low activity catalyst conveying pipe,
It is distributed in the renewing zone 201 of fast fluidized bed regenerator 2 by low activity catalyst distributor 12.Low work in renewing zone 201
Property catalyst contact with the main air being distributed by main air distributor 10, burn, the flue gas of generation and regenerated catalyst are urged through second
Agent redistributor 14 is up, and enters catalyst and separate in smoke separator 20.The flue gas separated warp successively
Regenerated flue gas one secondary cyclone 23, regenerated flue gas three-stage cyclone separator 24 deliver to upstream device after purifying；Isolate
The regenerated catalyst come drains into regenerated catalyst collecting region 202, and now, regenerated catalyst is divided into three parts, and Part I regenerates
Catalyst enters external catalyst cooler for regenerator 18 through the 4th inclined tube 34 and cools down, and the catalyst after cooling is through supercool rear catalyst
Distributor 13 is distributed to regenerator bottom；Part II regenerated catalyst enters the second outer circulating tube 15, urges through the second outer circulation
Agent distributor 11 is distributed in regenerator；Part III regenerated catalyst is through regenerated catalyst stripping section 17, oblique through second
Enter in catalyst blender 7 after pipe 30, and mix homogeneously with the cold rear catalyst carrying out autoreactor external warmer 8, then by
Mixed catalyst distributor 4 is distributed to participation in reaction zone 101 and prepares the reaction of low-carbon alkene.
Hereinafter will be further described through this utility model by specific embodiment 1, it should be noted that implement in detail below
Example 1 have employed the device as shown in the accompanying drawing 1 that this utility model embodiment provides.
Embodiment 1
The said apparatus that the present embodiment utilizes this utility model embodiment to provide carries out the production process of methanol-to-olefins, as
Shown in lower: methanol feedstock enters bottom reaction zone 101 after being preheating to 120 DEG C, it is regenerated catalyst through regenerated catalyst stripping
After section 17 and catalyst blender 7, mixed catalyst distributor 4 it is distributed in bottom, reaction zone 101.It is 450 in reaction temperature
DEG C, reaction pressure is 0.2MPa (G), and the mass space velocity of reaction controls at 8h-1Under conditions of, methanol feedstock connects with regenerated catalyst
Touching and react, generate the reaction gas rich in low-carbon alkene, reaction waste heat is taken away by reactor external warmer 8, return
Cold catalyst is distributed in the middle part of reaction zone 101 by mixed catalyst distributor 4 after mixing with regenerated catalyst；Reaction gas is by the
One catalyst redistributor 6 is up, sequentially enters catalyst and divides with reaction gas separator 19, thick cyclone separator 193, top whirlwind
From device 21 to realize the separation of reaction gas and catalyst；Separated by thick cyclone separator 193 and top cyclone separator 21
Low activity catalyst, after low activity catalyst stripping section 16 strips, is distributed in quickly stream by low activity catalyst distributor 12
Change bed regenerator 2 bottom.Meanwhile, the reaction gas separated is entered by the second riser 27 pushed up on cyclone separator 21
The further purifying and dedusting of reaction gas three-stage cyclone separator 22, delivers to downstream unit.Main air is entered by the main air entrance of regenerator
Enter bottom renewing zone 201, be 680 DEG C in regeneration temperature, under conditions of regeneration pressure is 0.2MPa (G), low activity catalyst with
Main air contacts, burns, and obtains regenerated catalyst, and in regenerator, superfluous heat is taken away by external catalyst cooler for regenerator 18；Regeneration catalyzing
Agent, after regenerated catalyst stripping section 17, catalyst blender 7, is distributed to reaction zone 101 times by mixed catalyst distributor 4
Portion, continues to react with the methanol feedstock entered in reaction zone 101.
Embodiment 2
The present embodiment has carried out concrete mensuration to the implementation result of embodiment 1, and concrete data refer to table 1:
Table 1
| Implementation result | Embodiment 1 | Embodiment 2 | Embodiment 3 |
| Methanol conversion | 99.94% | 99.95% | 99.97% |
| Ethylene+Propylene Selectivity | 79.1% | 78.5% | 78.4% |
| Coking yield | 1.75% | 1.77% | 1.79% |
| Catalyst consumption | 0.79kg/t ethylene+propylene | 0.78kg/t ethylene+propylene | 0.78kg/t ethylene+propylene |
As shown in Table 1, prepared by the alkene utilizing the device of the methanol-to-olefins that this utility model embodiment provides to be carried out,
Its reaction selectivity is high, it is possible to obtain the carbon back selectivity of at least 79%, and the unit consumption of coking yield and catalyst is the most relatively low, has
Higher economic adaptability.
The foregoing is only preferred embodiment of the present utility model, not in order to limit protection domain of the present utility model,
All within spirit of the present utility model and principle, any modification, equivalent substitution and improvement etc. made, should be included in this reality
Within novel protection domain.
Claims (8)
1. the device of a methanol-to-olefins, it is characterised in that described device includes fast fluidized bed reactor (1), by lower from
On be successively set on the internal reaction zone (101) of described fast fluidized bed reactor (1), low activity catalyst collecting region (102),
Reactor dilute-phase zone (103), fast fluidized bed regenerator (2), by lower from be successively set on described fast fluidized bed regenerator
(2) internal renewing zone (201), regenerated catalyst collecting region (202), regenerator dilute-phase zone (203), by lower from set gradually
Methanol feed distributor (3) in described reaction zone (101), mixed catalyst distributor (4), the first circulating catalyst divide
Cloth device (5), the first catalyst redistributor (6), the catalyst blender (7) being connected with described mixed catalyst distributor (4),
The reactor external warmer that upper and lower side is connected with described reactor dilute-phase zone (103) and described catalyst blender (7) respectively
(8), upper and lower side connects with described low activity catalyst collecting region (102) and described first circulating catalyst distributor (5) respectively
The first outer circulating tube (9) connect, by lower main air distributor (10) in being above successively set on described renewing zone (201), second
Circulating catalyst distributor (11), low activity catalyst distributor (12), cold rear catalyst distributor (13), the second catalyst
Redistributor (14), upper and lower side is distributed with described regenerated catalyst collecting region (202) and described second circulating catalyst respectively
The second outer circulating tube (15) that device (11) connects, upper and lower side respectively with described low activity catalyst collecting region (102) and described low
The low activity catalyst stripping section (16) that active catalyst distributor (12) connects, upper and lower side is received with described regenerated catalyst respectively
The regenerated catalyst stripping section (17) that Ji Qu (202) and described catalyst blender (7) connect, upper and lower side respectively with described regeneration
The external catalyst cooler for regenerator (18) that device dilute-phase zone (203) and described cold rear catalyst distributor (13) connect, upper and lower side position respectively
Catalyst in described reactor dilute-phase zone (103) and described low activity catalyst collecting region (102) and reaction gas separator
(19) catalyst in, upper and lower side lays respectively at described regenerator dilute-phase zone (203) and described regenerated catalyst collecting region (202)
With smoke separator (20), it is arranged in described reactor dilute-phase zone (103) and the top cyclone separator (21) that is connected and instead
Should gas three-stage cyclone separator (22), one or the two grades of cyclonic separation being arranged in described regenerator dilute-phase zone (203) and being connected
Device (23) and regenerated flue gas three-stage cyclone separator (24).
Device the most according to claim 1, it is characterised in that described catalyst and reaction gas separator (19) include by lower from
On the reducer (191), dilute phase pipe (192) and the thick cyclone separator (193) that sequentially connect；
The lower end of described reducer (191) and described dilute phase pipe (192) is respectively positioned on described low activity catalyst collecting region (102)
In, the part more than lower end of described dilute phase pipe (192) is positioned at described reactor dilute-phase zone (103), described thick cyclonic separation
Device (193) top is provided with first riser (194) with air inlet, and described first riser (194) revolves with described top
Wind separator (21) is connected.
Device the most according to claim 1, it is characterised in that described reaction gas three-stage cyclone separator (22) part is positioned at
Described reactor dilute-phase zone (103) is internal, and it is outside that another part is positioned at described reactor dilute-phase zone (103), and is positioned at described
The top of the reaction gas three-stage cyclone separator (22) that reactor dilute-phase zone (103) is outside is provided with purification letter shoot (25),
The bottom being positioned at the internal reaction gas three-stage cyclone separator (22) of described reactor dilute-phase zone (103) is provided with fine powder delivery line
(26), for the dead catalyst fine powder of regeneration is derived outside described fast fluidized bed reactor.
Device the most according to claim 3, it is characterised in that cyclone separator (21) top, described top is provided with second liter
Trachea (27), described top cyclone separator (21) is positioned at described reactor dilute-phase zone by described second riser (27) with described
(103) internal reaction gas three-stage cyclone separator (22) is connected.
Device the most according to claim 1, it is characterised in that the bottom of described catalyst blender (7) is provided with lifting
Medium inlet (28), and described catalyst blender (7) by the first inclined tube (29) and the second inclined tube (30) respectively with described instead
Answer device external warmer (8) to be connected with described regenerated catalyst stripping section (17), and described reactor external warmer (8) is by the
Three inclined tubes (31) are connected with described low activity catalyst collecting region (102)；
It is provided with first time guiding valve on described first inclined tube (29), described 3rd inclined tube (31) is provided with guiding valve on first, institute
The top stating reactor external warmer (8) is provided with the first catalyst level-sensing device being connected with the guiding valve signal of telecommunication on described first,
The first temperature sensor being connected with described first time guiding valve signal of telecommunication it is provided with on the wall of described reaction zone (101).
Device the most according to claim 1, it is characterised in that described regenerated flue gas three-stage cyclone separator (24) partly position
Internal in described regenerator dilute-phase zone (203), it is outside that another part is positioned at described regenerator dilute-phase zone (203)；
The top of a described secondary cyclone (23) is provided with the 3rd riser (32), and described 3rd riser (32) with
The described regenerated flue gas three-stage cyclone separator (24) being positioned at described regenerator dilute-phase zone (203) internal is connected；
Described regenerated flue gas three-stage cyclone separator (24) top being positioned at described regenerator dilute-phase zone (203) outside is provided with only
Change regenerated flue gas conveying pipe (33).
Device the most according to claim 6, it is characterised in that the top of described external catalyst cooler for regenerator (18) passes through the 4th
Inclined tube (34) is connected with described regenerated catalyst collecting region (202), described 4th inclined tube (34) is provided with guiding valve on second, institute
State external catalyst cooler for regenerator (18) top and be additionally provided with the second catalyst level-sensing device being connected with the guiding valve signal of telecommunication on described second；
The bottom of described external catalyst cooler for regenerator (18) is by the 5th inclined tube (35) with described cold rear catalyst distributor (13) even
Connect, described 5th inclined tube (35) be provided with second time guiding valve, the wall of described regenerated catalyst collecting region (202) is provided with
The second temperature sensor that described second time guiding valve signal of telecommunication connects.
Device the most according to claim 1, it is characterised in that 1-5 described first catalyst redistributor (6) is along level
Direction is intervally installed, and the porosity of described first catalyst redistributor (6) is 60-90%；
1-5 described second catalyst redistributor (14) is intervally installed in the horizontal direction, and described second catalyst is again
The porosity of allotter (14) is 60-90%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620250157.4U CN205528515U (en) | 2016-03-29 | 2016-03-29 | Device of methyl alcohol system alkene |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620250157.4U CN205528515U (en) | 2016-03-29 | 2016-03-29 | Device of methyl alcohol system alkene |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108212029A (en) * | 2017-02-03 | 2018-06-29 | 青岛京润石化设计研究院有限公司 | A kind of catalytic conversion reaction method and reactor |
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2016
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108212029A (en) * | 2017-02-03 | 2018-06-29 | 青岛京润石化设计研究院有限公司 | A kind of catalytic conversion reaction method and reactor |
| CN108212029B (en) * | 2017-02-03 | 2020-09-11 | 青岛京润石化设计研究院有限公司 | Catalytic conversion reaction method and reactor |
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