CN110237779A - A kind of catalyst multi-stage fluidized regeneration method and catalyst regenerator - Google Patents
A kind of catalyst multi-stage fluidized regeneration method and catalyst regenerator Download PDFInfo
- Publication number
- CN110237779A CN110237779A CN201810535704.7A CN201810535704A CN110237779A CN 110237779 A CN110237779 A CN 110237779A CN 201810535704 A CN201810535704 A CN 201810535704A CN 110237779 A CN110237779 A CN 110237779A
- Authority
- CN
- China
- Prior art keywords
- catalyst
- regenerative response
- response area
- gas
- regeneration
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Catalysts (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to the catalyst regeneration techniques fields of petroleum and chemical field gas-solid phase fluidized catalytic reaction process, more particularly to a kind of catalyst multi-stage fluidized regeneration method, it is divided into catalyst regeneration reactive moieties (5) and gas-solid separate section (6) inside catalyst regenerator, catalyst regeneration reactive moieties (5) are divided into concatenated three-level fluidized bed regeneration reaction zone up and down, 1st regenerative response area (54A) is in bottom, 2nd regenerative response area (54B) is in the top, 3rd regenerative response area (54C) is between the 1st regenerative response area (54A) and the 2nd regenerative response area (54B)；It is gas solid separation part (6) above 2nd regenerative response area (54B), catalyst regeneration reaction process is resolved into three-level, hydrogen reaction and most of carbon reaction are completed in the 1st and the 2nd grade of catalyst regeneration reaction；The reaction of 3rd level progress residual carbon；2nd grade is reacted to form counter-current regeneration condition with 3rd level catalyst regeneration.
Description
Technical field
The present invention relates to the catalyst regeneration techniques of petroleum and chemical field gas-solid phase fluidized catalytic reaction process, especially
It is related to a kind of catalyst multi-stage fluidized regeneration method and catalyst regenerator.
The prior art
Catalytic cracking of petroleum hydrocarbon reaction is the secondary processing process of crude oil, and reaction is the reaction based on gas-solid phase cracking, is urged
Change the coke that cracking reaction raw material reaction process generally generates inlet amount 5.5%~10.0%, these coke are attached to catalyst
Surface, blocking catalyst micropore, it is necessary to circular regeneration.
Reclaimable catalyst ratio containing weight of coke into catalyst regenerator is about 1%, and catalyst regeneration uses oxygen-containing
Gas is generally compressed air, oxygen content about 20%；The catalyst coke content of outflow catalyst regenerator is generally below
0.05%, oxygen content of smoke gas is better closer to zero naturally；Oxygen content and coke content in obvious catalyst regeneration reaction zone
Far below the numerical value for entering regenerator, it is most important for how improving the reactant concentration in regenerative response process or regenerator
's.
Reclaimable catalyst regenerative response principle after raw material reaction is very simple, and mainly carbon is reacted with oxygen generates carbon monoxide
Or carbon dioxide and Hydrogen In The Coke react into vapor with oxygen.But with the progress of reaction, concentration of carbon, hydrogen concentration and oxygen
Concentration can all reduce, and reaction efficiency just reduces naturally, and temperature is also determined by reaction depth, and temperature is also again the significant of reaction speed
Influence factor, how to improve the concentration, temperature of reactant in reaction process is critical issue to reaction efficiency.
Hydrogen reaction speed original is faster than carbon reaction speed, and the vapor that hydrogen reaction generates will affect the activity of regenerated catalyst again
(hydrothermal deactivation), can be with by controlling timing node and the position of hydrogen production reaction so make good use of the difference of hydrogen and carbon reaction speed
Reduce influence of the vapor to catalyst activity.
Since catalytic cracking is large-size chemical process, catalyst regenerator equipment is huge, interior catalyst inventory also Chang Da
The quantity of hundreds of tons, the compression oxygen-containing gas such as air that catalyst regeneration process needs is up to tens of ten thousand stere/hours, even
Million cubic metres hours, compressed air be also required to increase 300-400KPa, catalyst regeneration process is the master of catalytic cracking unit
Want energy consumption link.
Either plant investment, operation energy consumption or maintenance cost, catalyst regeneration process in catalytic cracking process all
Occupy main status.Reducing Excess oxygen content in regenerative process flue gas just reduces the usage amount of compression oxygen-containing gas, also just drops
Low energy consumption；The catalyst inventory for reducing regenerative system can reduce the pressure drop of regeneration gas, also reduce catalyst regeneration process
Energy consumption；Catalyst hydrothermal deactivation caused by hydrogen reacts is reduced, it is all significant to catalytic cracking process.
And catalyst regeneration is realized in fluidized bed, either regenerative response efficiency (rate) or gas pressure drop
Both depend on the reactor types of regenerative response or the fluidization form of catalyst.
Having than more typical catalyst regeneration techniques includes two-stage regeneration of connecting up and down, adverse current two-stage regeneration technology.Especially
It is that the adverse current two-stage regeneration technology that Uop Inc. and middle petrochemical industry Beijing designing institute develop embodies higher efficiency.Uop Inc. and
Ashland company discloses the two-phase up-flow regeneration reaction regeneration technology of its joint development in US4299687,
CN97121795.5 discloses a kind of heavy oil fluidized catalyzed conversion eclipsed form two-stage regeneration technology.
Concatenated regeneration techniques above and below domestic-developed recirculating fluidized bed and dense-phase fluidized bed.After being reacted in recirculating fluidized bed
Gas and catalyst fully enter the dense-phase fluidized bed of enlarged-diameter the reaction was continued.The dense-phase fluidized bed reaction zone of this technology
Reaction medium transmission speed and oxygen content are all lower, need by increasing catalyst inventory, the extension reaction time makes up.
Under recirculating fluidized bed fluidized state, due to gas become continuous phase, reaction medium transmitting improve it is more, but
There is also the low problems of density of catalyst, and especially with the progress of reaction, the content of carbon and oxygen is all reduced rapidly, reaction effect
Rate decline.It is lower that dense-phase fluidized bed transmission efficiency in form is burnt in recirculating fluidized bed and dense-phase fluidized bed series connection.
China Petroleum East China exploration and design institute develops recirculating fluidized bed single hop coke burning regeneration technology, and catalyst is in recycle stream
Change and completes regenerative response in bed.Although recirculating fluidized bed fluidization form solves reaction medium problem of transmission, it is possible to reduce urge
The reserve of agent, but due to the progress with reaction, the carbon content of oxygen content and catalyst in gas all gradually decreases, and recycles
It has been regenerative agent level that fluidized bed single hop, which burns technology rear portion carbon content, and oxygen also runs out of substantially, and reaction efficiency is very low, needs
Increase reactor volume, increases construction investment.
Catalyst regeneration reaction process is in addition to completing to catalyst regeneration, it is also necessary to be adapted with raw material reaction process.With
Raw material fluid catalytic cracking reaction technology.Progress, new demand also proposed to catalyst regeneration reaction process.Raw material fluidisation
Catalytic cracking reaction process generally requires the catalyst of different regenerated outcomes.Existing catalyst fluidization regeneration techniques tend not to
Meet the needs of raw material catalytic cracking reaction.
Summary of the invention
The purpose of the present invention is to provide a kind of catalyst multi-stage fluidized regeneration methods, can balance hydrogen reaction and oxidation of coal
The influence of the heavy metal of reaction and deposition, can improve the transmission efficiency of the reactant in reaction process, can also improve reaction
Concentration of medium realizes that energy-efficient, catalyst inventory is few, oxygen consumes less, good economy performance catalyst regeneration target.
Invention also provides a kind of catalyst regenerators for realizing catalyst multi-stage fluidized regeneration method.
The reaction process surface of regenerating catalyst in fluidized bed sees that principle is very simple, mainly oxygen, carbon reaction and oxygen, hydrogen
Reaction, and hydrogen reaction speed is faster.Since catalytic cracking unit is in large scale, regenerator investment and energy consumption all account for catalytic cracking
It is significant to improve catalyst regeneration from major part for device.Catalyst regeneration reaction is gas-solid phase reaction, and it is anti-to improve regeneration
Oxygen transmits and the oxygen concentration that contact with coke during answering, raising carbon monoxide and carbon dioxide, vapor in fluidized bed
Transmission speed, balanced reaction medium transmitting and reaction medium concentration relationship, catalyst regeneration reaction efficiency could be improved.
Improve catalyst regeneration reaction efficiency, it is important to make good use of catalyst fluidization technology, form catalyst and oxygen-containing gas good
Good fluidization form.
In order to achieve the above object, being used for petroleum hydrocarbon raw material the present invention provides a kind of catalyst multi-stage fluidized regeneration method
Reclaimable catalyst regeneration after fluid catalytic cracking reaction；
The catalyst multi-stage fluidized regeneration method is completed in a catalyst regenerator, is divided into inside catalyst regenerator and being urged
Agent regenerative response part and gas-solid separate section, catalyst regeneration reactive moieties are divided into concatenated three-level fluidized bed regeneration up and down
Reaction zone, three-level regenerative response area are coaxially disposed up and down, the 1st regenerative response area (the 1st grade of catalyst regeneration zones or the 1st catalysis
Agent regenerative response area or the first renewing zone) in bottom, the 2nd regenerative response area (the 2nd grade of catalyst regeneration zones or the 2nd catalysis
Agent regenerative response area or the second renewing zone) in the top, the 3rd regenerative response area (3rd level catalyst regeneration zones or the 3rd catalysis
Agent regenerative response area or third renewing zone) between the 1st regenerative response area and the 2nd regenerative response area, the 1st regenerative response Qu Yu
It is separated between 3 regenerative response areas with partition；It is gas solid separation part above 2nd regenerative response area；
Catalyst regeneration reaction process are as follows:
1) reclaimable catalyst for, carrying out autoreactor enters the 1st regenerative response area from spent agent delivery pipe, and the 1st regenerative response area is
Low-temp recovery reaction zone；(fresh) the first oxygen-containing compressed gas from compressor is by being located at the 1st regenerative response area bottom zone
The first gas distributor in domain enter the 1st regenerative response area, oxygen contacted with catalyst realization preliminary catalyst regenerative response and
The reaction of Hydrogen In The Coke；
2), the catalyst in the 1st regenerative response area and gas enter the delivery pipe being located inside the 3rd regenerative response area, are transported to
2nd regenerative response area of top carries out further catalyst regeneration reaction；The oxygen-containing oxygen in the 1st regenerative response area continues and catalysis
Agent haptoreaction；Remaining oxygen and catalyst residual coke are in the 1st regenerative response area residual hydrogen of the 2nd regenerative response area completion in gas
Reaction and most of oxidation of coal；When it is implemented, exporting setting catalyst and flue gas orifice plate, the 1st regenerative response in delivery pipe
Gas and catalyst in area enter the 2nd regenerative response area by the catalyst and flue gas orifice plate；By in the 2nd regenerative response area
Catalyst inventory and temperature control the 2nd regenerative response area in catalyst regenerative response degree and area's catalyst phosphorus content；
It improves the catalyst inventory in the 2nd regenerative response area or improves the area temperature Dou Shigai regenerative response ratio and improve, keep catalyst carbon containing
It reduces；
3), after the 2nd regenerative response area realizes the further regenerative response of catalyst, reflux catalyst is heavy by catalyst return pipe
Drop to the 3rd regenerative response area of lower section；(fresh) the second oxygen-containing compressed gas of another part from compressor is by being located at the 3rd
The second gas distributor of regenerative response area bottom section enters the 3rd regenerative response area, realizes to from the 2nd regenerative response area
The 3rd level oxidation reaction of reflux catalyst residue charcoal, completes catalyst regeneration；Or second oxygen-containing compressed gas with come from the 2nd
The catalyst in regenerative response area is mixed to cooling catalyst；The 2nd is controlled again by the catalytic amount conveyed from catalyst return pipe
The regenerative response ratio of catalyst inventory and the 2nd regenerative response area in raw reaction zone；It is urged by what is conveyed from catalyst return pipe
Agent amount controls the catalytic amount flowed out in the 2nd regenerative response area to catalyst inventory in the 3rd regenerative response area of control, in turn
It limits gas and carries catalyst into the 2nd regenerative response area；The adjustable each area of the catalyst inventory in each regenerative response area is again
Raw reaction ratio；Gas (flue gas) after 3rd regenerative response area regenerative response becomes high-temperature gas, these high temperature oxygen-containing gas to
On leave the 2nd regenerative response area for entering top after the 3rd regenerative response area catalyst fluidized bed bed, in gas remaining oxygen after
The continuous reaction for participating in the 2nd regenerative response area forms the tandem reaction of oxygen-containing gas；
4) flue gas, from the 1st regenerative response area and the gas from the 3rd regenerative response area are in the 2nd regenerative response Qu Jinyi
The catalyst fluidized bed bed that the 2nd regenerative response area is left after step progress catalyst regeneration reaction, is introduced into gas solid separation part
Dilute-phase zone, subsequently into gas-solid separator, regenerated flue gas exports outflow catalyst regenerator from regenerated flue gas；
5) regenerative agent delivery pipe, is set in the 3rd catalyst fluidized bed area, regenerative response area, regenerated catalyst is conveyed from the regenerative agent
Pipe outflow catalyst regenerator.
Above-mentioned catalyst multi-stage fluidized regeneration method, the 2nd regenerative response area and the 3rd regenerative response area use turbulent fluidised
Bed reaction formation, gas superficial flow velocity are not more than 1.1m/s；1st regenerative response area is anti-using turbulent fluidized bed or recirculating fluidized bed
Form is answered, gas superficial flow velocity is not more than 2.0m/s.
Above-mentioned catalyst multi-stage fluidized regeneration method, the catalyst and gas in the 1st regenerative response area and the 3rd regeneration
The gas of reaction zone passes through respective distribution grid respectively or orifice plate enters the 2nd regenerative response area；Or using distribution after first mixing
Plate or orifice plate enter the 2nd regenerative response area.
Above-mentioned catalyst multi-stage fluidized regeneration method, the gas and catalyst in the 1st regenerative response area are by urging
Agent and flue gas orifice plate enter the 2nd regenerative response area, and the gas in the 3rd regenerative response area enters the 2nd again by gas distribution grid
Raw reaction zone.
Above-mentioned catalyst multi-stage fluidized regeneration method, the gas in the 3rd regenerative response area first pass through delivery pipe and go out
Channel in the delivery pipe outlet cone (also known as delivery pipe export centrum) at mouthful place enters in delivery pipe outlet cone, and comes from the
Then the catalyst and gas mixing in 1 regenerative response area enter the 2nd regenerative response area by catalyst and flue gas orifice plate again.Tool
When body is implemented, channel is designed as porous type or slot type or the various different types of socket joint type, and channel allows the 3rd regenerative response area
Gas enters in delivery pipe, and the gas and catalyst in delivery pipe from the 1st regenerative response area cannot reversely be flowed out into the 3rd again
Raw reaction zone；Channel cross-sectional flow area is designed by flow velocity not less than 2.0m/s by the gas in the 3rd regenerative response area；
Above-mentioned catalyst multi-stage fluidized regeneration method, when catalyst heat collector or cooler 7 is arranged, heat collector or cooler
7 catalyst inlet pipe (i.e. the catalyst transport of catalyst regenerator to heat collector) is located at the 2nd regenerative response area, from the 2nd
Regenerative response area and the 3rd regenerative response area take out extra heat；Heat or catalyst after cooling is taken to enter the 3rd regenerative response
Area reduces the catalyst temperature in the 3rd regenerative response area；Take heat anti-in the 2nd regenerative response area and the 3rd regeneration by heat collector
The distribution in area is answered to adjust the temperature in the 2nd regenerative response area and the 3rd regenerative response area, takes heat or catalyst after cooling to be generated
Regenerative response efficiency shadow of the catalyst in the 1st regenerative response area does not generate sound.
In the method for the present invention, when catalyst regeneration heat release surplus, that is, regenerator needs to take heat, the 2nd regenerative response area or
Temperature in settable heat removing tube in 3 regenerative response areas, directly the 2nd regenerative response area of reduction or the reaction of the 3rd renewing zone.
In the method for the present invention:
The regeneration agent flux for being located at the delivery pipe in the 3rd regenerative response area is realized to catalyst inventory or stream in the 3rd regenerative response area
Change the control of bed bed height, and realizes that the gas in the 3rd regenerative response area from the abjection of catalyst fluidized bed, while limiting the 3rd
Regenerative response area gas carries catalyst and enters the 2nd regenerative response area；
When needing to improve the 1st regenerative response area temperature, reflux is set between the 2nd regenerative response area and the 1st regenerative response area
Pipe makes partial catalyst return to the 1st regenerative response area from the 2nd regenerative response area；
When needing, catalyst outflux, that is, catalyst or semi regeneration agent delivery pipe are set in the 2nd regenerative response area, reacted for raw material
Part provides catalyst or appropriate carbon containing semi regeneration agent；
By changing the ratio of burning in the 2nd regenerative response area and the 3rd regenerative response area, or changes and be input to the 3rd regenerative response
The catalyst in area takes heat or cooling energy, or adjusts the oxygen-containing gas for entering the 2nd regenerative response area and the 1st regenerative response area
Ratio realizes the adjusting to the 3rd regenerative response area catalyst temperature, or realizes the drop of the 3rd regenerative response area catalyst temperature
It is low.
1st regenerative response area of the present invention is using turbulent fluidized bed or the reactor of recirculating fluidized bed form, gas meter
It sees flow velocity and is not higher than 2.0m/s；2nd regenerative response area and the 3rd regenerative response area use the reactor of turbulent fluidized bed form, gas
Body apparent velocity is not more than 1.1m/s.
Invention also provides a kind of catalyst regenerator of catalyst multi-stage fluidized regeneration method,
It is divided into catalyst regeneration reactive moieties and gas-solid separate section inside the catalyst regenerator；The gas solid separation part
It is provided with gas-solid separator, dilute-phase zone and regenerated flue gas outlet；
It is divided into three fluidized bed regeneration reaction zones up and down in catalyst regeneration reactive moieties in catalyst regenerator shell, respectively
The 1st regeneration for the 1st regenerative response area, the 3rd regenerative response area and the 2nd regenerative response area, three area's coaxial arrangements, bottom is anti-
It answers and is separated between area and the 3rd regenerative response area at middle part with partition, in the outlet of the 1st regenerative response area and the 3rd regenerative response area
It is vertically arranged delivery pipe, conveying tube inlet (i.e. lower end) and the 1st regenerative response area connection, delivery pipe exit is that diameter gradually increases
The conical form added i.e. delivery pipe outlet cone, outlet (i.e. upper end) the setting catalyst and smoke hole of delivery pipe outlet cone
Plate, the catalyst and flue gas orifice plate become the boundary in the 1st regenerative response area and the 2nd regenerative response area of the top, anti-in the 3rd regeneration
It answers and gas distribution grid is set between the 2 regenerative response area Qu Yu, which becomes the 3rd regenerative response area and the 2nd regeneration
The boundary of reaction interval；The gas solid separation part is set to above the 2nd regenerative response area；Catalysis in the 3rd regenerative response area
Agent dense-phase fluidized bed area is equipped with regenerative agent delivery pipe, is equipped with spent agent in the dense fluidizing bed of catalyst area in the 1st regenerative response area
Delivery pipe；
When the outlet of delivery pipe outlet cone is identical as position catalyst regenerator size, (catalyst regenerator is same
Cross sectional dimensions at absolute altitude), the catalyst and flue gas orifice plate of delivery pipe outlet cone outlet end become the 2nd regenerative response area of top
With the boundary in intermediate 3rd regenerative response area, while also becoming the boundary in the 1st regenerative response area of the 2nd regenerative response area and lower section, and
As the gas distribution grid in the 2nd regenerative response area, channel, the gas in the 3rd regenerative response area are set in delivery pipe outlet cone
Entered in delivery pipe outlet cone by the channel, and the 1st regenerative response area urges from below inside delivery pipe outlet cone
After agent and gas mixing, the 2nd regenerative response area is entered back into；The 1st regenerative response area bottom section setting first gas point
Second gas distributor is arranged in cloth device, the 3rd regenerative response area bottom section, and second gas distributor is distributor pipe.
The catalyst regenerator of above-mentioned catalyst multi-stage fluidized regeneration method, when the 1st regenerative response area and the 2nd regeneration are anti-
When answering one delivery pipe of setting between area, delivery pipe is arranged on catalyst regenerator axis, defeated when multiple delivery pipes are arranged
Send pipe circumferentially uniformly distributed in catalyst regenerator cross section；In delivery pipe exit, delivery pipe outlet cone, delivery pipe outlet are set
Catalyst and flue gas orifice plate is arranged in cone upper end.
The catalyst regenerator of above-mentioned catalyst multi-stage fluidized regeneration method (is reacted according to corresponding raw material to catalysis
The requirement of agent), catalyst or semi regeneration agent delivery pipe, catalyst or semi regeneration agent are set from the catalysis in the 2nd regenerative response area
Agent or semi regeneration agent delivery pipe outflow catalyst regenerator.
Catalyst heat collector or cooler is arranged in the catalyst regenerator of above-mentioned catalyst multi-stage fluidized regeneration method,
The catalyst inlet pipe of heat collector or cooler is located at the 2nd regenerative response area, and (catalyst after taking heat is defeated for catalyst outlet pipe
Send pipe) it is located at the 3rd regenerative response area.
In above-mentioned catalyst regenerator, the outlet of the 1st regenerative response area and the delivery pipe main body in the 2nd regenerative response section with
Expansion joint is arranged between delivery pipe outlet cone part or is designed as free socket joint to adapt to the heat of equipment with the structure of free wxpansion
Expansion requirements.
The task of the present invention is what is be achieved:
Oxygen-containing compressed gas preferentially selects air, and compressed air provides the oxygen that catalyst regeneration needs, about 40-75%'s or so
For compressed air from first gas distributor into the 1st regenerative response area, the reclaimable catalyst from raw material reactor enters the 1st regeneration
Reaction zone, most of hydrogen-oxygen in the coke that area's reclaimable catalyst carries are melted into vapor；Gas after regenerative response is defeated
The 2nd regenerative response area for sending catalyst to enter top, then it is anti-to enter the 3rd intermediate regeneration from catalyst return pipe again for catalyst
Answer area；Regenerated catalyst flows out regenerator from the 3rd regenerative response area；The compressed air of about 25-60% is from second gas distributor
Into the 3rd regenerative response area, after the 3rd regenerative response area is reacted with catalyst residual carbon, gas enters back into the 2nd regenerative response
Area, remaining oxygen continue to participate in regenerative response in the 2nd regenerative response area；The gas in the 2nd regenerative response area completes reaction and leaves catalysis
It is introduced into the dilute phase of gas solid separation part after agent fluidized bed, then enters back into cyclone gas-solid separator, is flowed after isolating catalyst
Regenerator out.
Invention effect
Compared with prior art, the present invention realizes that the series connection oxygen-containing gas relay of catalyst multistage fluidized bed is anti-in a regenerator
Answer, the present invention realized between the 2nd regenerative response area and the 3rd regenerative response area to catalyst regeneration reaction in oxygen content gas,
The carbon containing control with hydrogen and reaction temperature of catalyst, the 3rd regenerative response area realize high keto content gas and low carbon content catalysis
Agent reaction condition improves the reaction efficiency of low carbon-contained catalyst；2nd regenerative response area phosphorus content is higher than the 3rd regenerative response area,
The characteristics of regeneration efficiency in the 2nd regenerative response area is also guaranteed, realizes counter-current regeneration；Reclaimable catalyst reaction (the 1st regeneration
Reaction zone) and regenerative agent reaction (the 3rd regenerative response area) separate scheme and avoid low temperature is low from carbon containing the catalyst after heat being taken to treat
Influence of the raw catalyst in the regenerative response efficiency in the 1st regenerative response area；Meanwhile the present invention realizes that reclaimable catalyst low level enters
Regenerator, a regenerative agent high position flow out regenerator, had both significantly reduced investment compared with existing counter-current regeneration technology, are also more convenient raw material
The design of reactor simplifies device arrangement, reduces operating cost；The present invention realizes semi regeneration agent circulation, can react for raw material
Process provides catalyst of different nature, provides item to improve adaptability, selectivity and the benefit of catalytically cracked material reaction
Part.
Detailed description of the invention
Fig. 1 is the apparatus structure structure schematic diagram of catalyst multi-stage fluidized regeneration method embodiment one of the invention；
Fig. 2 is the apparatus structure structure schematic diagram of catalyst multi-stage fluidized regeneration method embodiment two of the invention, in delivery pipe
Channel is arranged in outlet cone；
Fig. 3 is the apparatus structure structure schematic diagram of catalyst multi-stage fluidized regeneration method embodiment three of the invention, and setting takes heat
Device or cooler.
Number mark is as follows in figure:
5 catalyst regeneration reactive moieties, 50 reclaimable catalysts, 50B spent agent delivery pipe, the oxygen-containing compressed gas of 51A first, 51B
Second oxygen-containing compressed gas, 52A first gas distributor, 52B second gas distributor, 53 delivery pipes, 53B delivery pipe outlet cone
Body, the 1st regenerative response area 54A, the 2nd regenerative response area 54B, the 3rd regenerative response area 54C, 55 partitions, 56A catalyst and flue gas
Orifice plate, 56B gas distribution grid, the channel 56C, 57B catalyst return pipe, 57 reflux catalyst, 58 regenerated catalysts, 58B regeneration
Agent delivery pipe, 59 catalyst or semi regeneration agent, 59B catalyst or semi regeneration agent delivery pipe；6 gas solid separation parts, 61 gas-solids point
From device, the outlet of 62 regenerated flue gas, 63 dilute-phase zones, 64 regenerated flue gas；7 heat collectors or cooler, 71 take heat or catalysis after cooling
Agent, 71B catalyst outlet pipe, 72 catalyst, 72B catalyst inlet pipe.
Specific embodiment
The technical solution that the present invention will be described in detail with reference to the accompanying drawings and embodiments, protection scope of the present invention include still
It is without being limited thereto.The routine techniques of fields can be used in the device structure not referred in detail in the present invention.
Embodiment one:
A kind of catalyst multi-stage fluidized regeneration method, it is anti-by catalyst regeneration using catalyst regenerator device as shown in Figure 1
Part 5 and gas-solid separate section 6 is answered to form；
Catalyst regeneration reactive moieties 5 are divided into concatenated three-level fluidized bed regeneration reaction zone up and down, above and below three-level regenerative response area
Coaxial arrangement, the 1st regenerative response area 54A exist in bottom, the 2nd regenerative response area 54B in the top, the 3rd regenerative response area 54C
Between 1st regenerative response area 54A and the 2nd regenerative response area 54B, between the 1st regenerative response area 54A and the 3rd regenerative response area 54C
It is separated with partition 55；It is gas solid separation part 6 above 2nd regenerative response area 54B；
Delivery pipe 53,53 entrance of delivery pipe and the 1st are vertically arranged in the outlet of the 1st regenerative response area and the 3rd regenerative response area 54C
Regenerative response area 54A connection, 53 exit of delivery pipe are delivery pipe outlet cone 53B, the outlet delivery pipe outlet cone 53B setting
Catalyst and flue gas orifice plate 56A, are arranged gas distribution grid between the 3rd regenerative response area 54C and the 2nd regenerative response area 54B
56B is equipped with regenerative agent delivery pipe 58B in the dense fluidizing bed of catalyst area of the 3rd regenerative response area 54C, in the 1st regenerative response area
The dense fluidizing bed of catalyst area of 54A is equipped with spent agent delivery pipe 50B；
First gas distributor 52A is set in the 1st regenerative response area 54A bottom section, in the 3rd regenerative response area bottom zone 54C
Second gas distributor 52B is arranged in domain, and second gas distributor 52B is distributor pipe；
Reclaimable catalyst 50 is introduced into the 1st catalyst regeneration reaction zone, and then sequence passes through the 1st regenerative response area 54A, the 2nd again
Raw reaction zone 54B and the 3rd regenerative response area 54C, compressed air are divided into two parts in parallel, and the first oxygen-containing compressed gas 51A is first
Into the 1st regenerative response area, subsequently into the 2nd regenerative response area, the second oxygen-containing compressed gas 51B is introduced into the 3rd regenerative response
Then area enters back into the 2nd regenerative response area of top；
1st regenerative response area is designed as turbulent fluidized bed or recirculating fluidized bed condition；2nd regenerative response area and the 3rd regenerative response
It is designed by fluid bed conditions in area；
Specific implementation process are as follows:
1) 500 DEG C or so of reclaimable catalyst 50 for, carrying out autoreactor enters the 1st again from spent agent delivery pipe 50B and distributor
Raw reaction zone 54A, the 1st regenerative response area 54A are low-temp recovery reaction zone；The total amount that catalyst regeneration from compressor needs
The oxygen-containing compressed gas 51A of the first of 40%-75% is distributed by being located at the first gas of the 1st regenerative response area 54A bottom section
Device 52A enters the 1st regenerative response area 54A, and oxygen contacts realization preliminary catalyst regenerative response and Hydrogen In The Coke with catalyst
Reaction；Realize that the carbon reaction of 10%-30% or so and the hydrogen of 50%-100% are reacted in the area；560 DEG C of area's regenerative response temperature
To 620 DEG C or so；Gas superficial flow velocity be not more than 2.0m/s, general 1.0m/s-2.0m/s, gas residence time 3 seconds to 8 seconds；
2), the catalyst in the 1st regenerative response area 54A and gas enter the delivery pipe being located inside the 3rd regenerative response area 54C
53, and enter delivery pipe outlet cone 53B, enter the through catalyst and flue gas orifice plate 56A in the outlet delivery pipe outlet cone 53B
2 regenerative response area 54B carry out further catalyst regeneration reaction；The oxygen-containing oxygen of 1st regenerative response area 54A continues and catalyst
Haptoreaction；Remaining oxygen and catalyst residual coke are remaining in the 1st regenerative response area of the 2nd regenerative response area 54B completion in gas
The reaction of hydrogen and most of oxidation of coal, catalyst temperature also further increase；Delivery pipe 53 is set by gas flow rate 10m/s-20m/s
Meter；2nd regenerative response area gas superficial flow velocity be 0.4m/s to 0.7m/s, 660 DEG C to 720 DEG C of temperature；In the 2nd regeneration when needing
Semi regeneration agent delivery pipe 59B is arranged in reaction zone, and catalyst material position passes through in the catalyst inventory or fluidized bed in the 2nd regenerative response area
Through catalyst return pipe 57B reflux reflux catalyst 57 or pass through catalyst or semi regeneration agent delivery pipe 59B outflow catalysis
Agent or semi regeneration agent 59 control；
3), after the 2nd regenerative response area 54B realizes the further regenerative response of catalyst, reflux catalyst 57 is returned by catalyst
Flow tube 57B is deposited to the 3rd regenerative response area 54C of lower section；The 25%-60%'s of reproduced high air total amount from compressor
Second oxygen-containing compressed gas 51B enters the 3rd by being located at the second gas distributor 52B of the 3rd regenerative response area 54C bottom section
Regenerative response area 54C, second gas distributor 53B use distributor pipe, high oxygen containing fresh compressed air and low carbon containing reflux
Catalyst 57 is realized in the 3rd regenerative response area 54C to the 3rd level oxidation reaction of the remaining charcoal of reflux catalyst 57, and catalyst is completed
Regeneration；3rd regenerative response area 54C is designed by gas superficial flow velocity 0.6m/s-0.8m/s, and gas residence time 5 seconds to 10 seconds, instead
Answer 620 DEG C -680 DEG C of temperature；3rd regenerative response area undertakes the carbon reaction of 10%-30%；The flue gas of 3rd regenerative response area 54C passes through
Gas distribution grid 56B enters the 2nd regenerative response area 54B；
4) flue gas, from the 1st regenerative response area 54A and the flue gas from the 3rd regenerative response area 54C are in the 2nd regenerative response
The catalyst fluidized bed bed that the 2nd regenerative response area 54B is left after the reaction of area's further progress catalyst regeneration, is introduced into gas-solid
The dilute-phase zone 63 of separate section 6, subsequently into gas-solid separator 61, regenerated flue gas 64 exports 62 outflow catalysts from regenerated flue gas
Regenerator；
5), the 3rd regenerative response area 54C catalyst fluidized bed area be arranged regenerative agent delivery pipe 58B, regenerated catalyst 58 from this again
Raw agent delivery pipe 58B outflow catalyst regenerator.By the quantity control for flowing out the regenerated catalyst 58 in the 3rd regenerative response area
Catalyst inventory and fluid catalyst material position in 3 regenerative response area 54C, limiting catalyst are carried to the 2nd regeneration by flue gas
Reaction zone；
When it is implemented, catalyst and flue gas orifice plate 56A and gas distribution grid 56B are designed by pressure drop 4-10KPa, gas via hole stream
Speed is designed by 15m/s-25m/s；Second gas distributor pressure drop is designed by 4kpa-7kpa；4- is pressed in first gas distributor pressure drop
6kpa design；
Gas solid separation part is made of dilute-phase zone 63 and two stage cyclone gas-solid separator 61, using conventional design.
Embodiment two:
Catalyst multi-stage fluidized regeneration method, using catalyst regenerator device as shown in Figure 2, by catalyst regeneration reacting part
Divide 5 and the composition of gas-solid separate section 6；
The outlet delivery pipe outlet cone 53B is identical as position catalyst regenerator size, and delivery pipe outlet cone 53B goes out
The catalyst and flue gas orifice plate 56A at mouth end become point of the 2nd regenerative response area 54B of top and the 3rd regenerative response area 54C of centre
Boundary, while also becoming the boundary of the 1st regenerative response area 54A of the 2nd regenerative response area 54B and lower section, and become the 2nd regenerative response area
The gas distribution grid of 54B, is arranged porous channel 56C on delivery pipe outlet cone 53B, and the gas of the 3rd regenerative response area 54C is logical
It crosses channel 56C to enter in delivery pipe outlet cone 53B, with the 1st regenerative response from below inside delivery pipe outlet cone 53B
After the catalyst and gas mixing of area 54A, the 2nd regenerative response area 54B is entered back into.
Other parts apparatus structure is identical as embodiment one.
Embodiment three:
Catalyst multi-stage fluidized regeneration method, using catalyst regenerator device as shown in Figure 3, by catalyst regeneration reacting part
Divide 5 and the composition of gas-solid separate section 6；
Setting catalyst heat collector or cooler 7, catalyst inlet pipe 72B are located at the 2nd regenerative response area 54B, and catalyst goes out
Mouth pipe 71B is located at the 3rd regenerative response area 54C, and the catalyst 72 in the 2nd regenerative response area is entered by catalyst inlet pipe 72B to be taken
Hot device or cooler 7 take heat or catalyst 71 after cooling to enter the 3rd regenerative response area by catalyst outlet pipe 71B, take heat
Or catalyst 71 after cooling realizes the cooling to the 3rd regenerative response area.
Other parts apparatus structure is identical as embodiment one.
Embodiment
The regeneration of catalyst multi-stage fluidized is carried out using catalyst regenerator of the invention, can be realized catalyst multi-stage fluidized
Bed series connection oxygen-containing gas relay reaction, reclaimable catalyst reaction and regenerative agent reaction separate, compared with existing counter-current regeneration technology,
Investment is significantly reduced, the design of raw material reactor is also more convenient, simplifies device arrangement, reduce operating cost；Specific implementation condition
It is as follows: operating pressure at the top of the dilute-phase zone of gas solid separation part: 0.3MPaG；Regenerated load: 20 tons of coke/hours；Coke hydrogen contains
Amount: 7%w；It compresses oxygen-containing gas and uses air, air enters 200 DEG C of temperature；2000 ton/hours of reclaimable catalyst amount, temperature
500℃；1st regenerative response area air capacity, 15400 standard cube m/h, 56 tons of catalyst inventory, gas mean flow rate
1.1m/s；1.8 meters of internal diameter of delivery hose；
3rd regenerative response area air capacity, 6600 standard cube m/h, gas mean flow rate 0.7m/s；60 tons of catalyst inventory,
690 DEG C of regenerative response temperature；
It is designed by complete regeneration scheme, the oxygen content of smoke gas 1.5% that regenerative response heel row is removed；
2nd 80 tons of regenerative response area catalyst inventory, 680 DEG C of reaction temperature, gas mean flow rate 0.6m/s；
Regenerative agent delivery pipe conveys 1400 ton/hours of regenerative agent, and catalyst or semi regeneration agent delivery pipe convey semi regeneration agent 580
Ton/hour；Catalyst and smoke hole anode drop 7kpa, gas distribution grid pressure drop 7kpa；Second gas distributor pressure drop 6kpa；The
One gas distributor pressure drop 5kpa, using distributor pipe；
1st 8 meters of regenerative response area diameter, more than first gas distributor 4 meters of height (are free of divider height)；
10 meters of 3rd regenerative response area height (being free of partition), 4 meters of the close phase material position of catalyst fluidized bed；
2nd regenerative response area is located at the tapered zone between the 3rd regenerative response area and gas-solid separate section dilute-phase zone；
13 meters of gas solid separation part dilute-phase zone diameter, 12 meters of height (being free of tapered zone).
According to process above condition, technical staff can complete the design of this method.
Claims (10)
1. a kind of catalyst multi-stage fluidized regeneration method, which is characterized in that the catalysis of the catalyst multi-stage fluidized regeneration method
Agent internal regenerator is divided into catalyst regeneration reactive moieties (5) and gas-solid separate section (6), catalyst regeneration reactive moieties (5)
It is divided into concatenated three-level fluidized bed regeneration reaction zone up and down, three-level regenerative response area is coaxially disposed up and down, the 1st regenerative response area
(54A) in bottom, the 2nd regenerative response area (54B) is in the top, and the 3rd regenerative response area (54C) is in the 1st regenerative response area
Between (54A) and the 2nd regenerative response area (54B)；It is gas solid separation part (6) above 2nd regenerative response area (54B)；Catalyst
Regenerative response process are as follows:
1) reclaimable catalyst (50) for, carrying out autoreactor enters the 1st regenerative response area (54A) from spent agent delivery pipe (50B), the
1 regenerative response area (54A) is low-temp recovery reaction zone；The first oxygen-containing compressed gas (51A) from compressor is by being located at the 1st
The first gas distributor (52A) of regenerative response area (54A) bottom section enters the 1st regenerative response area (54A), oxygen and catalysis
The reaction of preliminary catalyst regenerative response and Hydrogen In The Coke is realized in agent contact；
2), the catalyst in the 1st regenerative response area (54A) and gas, which enter, is located at the internal conveying in the 3rd regenerative response area (54C)
Pipe 53, the 2nd regenerative response area (54B) for being transported to top carry out further catalyst regeneration reaction；1st regenerative response area
The oxygen-containing oxygen of (54A) continues and catalyst haptoreaction；It is remaining that the 1st regenerative response area is completed in the 2nd regenerative response area (54B)
The reaction of hydrogen；
3), after the 2nd regenerative response area (54B) realizes the further regenerative response of catalyst, reflux catalyst (57) passes through catalysis
Agent return pipe (57B) is deposited to the 3rd regenerative response area (54C) of lower section；Second oxygen-containing compression of the another part from compressor
Gas (51B) enters the 3rd regeneration instead by being located at the second gas distributor (52B) of the 3rd regenerative response area (54C) bottom section
It answers area (54C), realizes the 3rd level oxidation reaction to the remaining charcoal of the reflux catalyst (57) from the 2nd regenerative response area (54B),
Complete catalyst regeneration；Or oxygen-containing compressed gas (51B) mixes with the catalyst from the 2nd regenerative response area (54B) to urging
Agent cooling；3rd regenerative response area regenerative response is catalyzed with the upward out 3rd regenerative response area of the mixed gas of catalyst
Enter the 2nd regenerative response area (54B) of top after agent fluidized bed bed, remaining oxygen continues to participate in the 2nd regenerative response in gas
The reaction in area forms the tandem reaction of oxygen-containing gas；
4), the flue gas from the 1st regenerative response area (54A) and the gas from the 3rd regenerative response area (54C) are in the 2nd regeneration
The catalyst fluidized bed bed in the 2nd regenerative response area (54B) is left after the reaction of reaction zone further progress catalyst regeneration, it is advanced
The dilute-phase zone (63) for entering gas solid separation part (6), subsequently into gas-solid separator (61), regenerated flue gas (64) goes out from regenerated flue gas
Mouth (62) outflow catalyst regenerator；
5) regenerative agent delivery pipe (58B), is set in the 3rd (54C) catalyst fluidized bed area, regenerative response area, regenerated catalyst (58)
From regenerative agent delivery pipe (58B) the outflow catalyst regenerator.
2. catalyst multi-stage fluidized regeneration method as described in claim 1, which is characterized in that the 2nd regenerative response area (54B) and
3rd regenerative response area (54C) uses turbulent fluidized bed reaction formation, and gas superficial flow velocity is not more than 1.1m/s；1st regenerative response
Area (54A) uses turbulent fluidized bed or recirculating fluidized bed reaction formation, and gas superficial flow velocity is not more than 2.0m/s.
3. catalyst multi-stage fluidized regeneration method as described in claim 1, which is characterized in that the 1st regenerative response area
The catalyst and gas of (54A) and the gas in the 3rd regenerative response area (54C) pass through respective distribution grid or orifice plate respectively and enter the
2 regenerative response areas (54B)；Or enter the 2nd regenerative response area (54B) using distribution grid or orifice plate after first mixing.
4. catalyst multi-stage fluidized regeneration method as claimed in claim 3, which is characterized in that the 1st regenerative response area
Gas and catalyst in (54A) enter the 2nd regenerative response area (54B), the 3rd regeneration by catalyst and flue gas orifice plate (56A)
Gas in reaction zone (54C) enters the 2nd regenerative response area (54B) by gas distribution grid (56B).
5. catalyst multi-stage fluidized regeneration method as claimed in claim 3, which is characterized in that the 3rd regenerative response area
Gas in (54C) first passes through the channel (56C) in the delivery pipe outlet cone (53B) in delivery pipe (53) exit and enters conveying
In pipe outlet cone (53B), then catalyst and gas mixing with the 1st regenerative response area (54A) is come from pass through catalyst again
Enter the 2nd regenerative response area (54B) with flue gas orifice plate 56A.
6. catalyst multi-stage fluidized regeneration method as described in claim 1, which is characterized in that when setting catalyst heat collector or
When cooler (7), the catalyst inlet pipe (72B) of heat collector or cooler (7) is located at the 2nd regenerative response area (54B), from the 2nd
Regenerative response area (54B) and the 3rd regenerative response area (54C) take out extra heat；Take heat or catalyst (71) after cooling into
Enter the 3rd regenerative response area (54C), reduces the catalyst temperature in the 3rd regenerative response area (54C)；Heat is taken to exist by heat collector
The distribution in the 2nd regenerative response area (54B) and the 3rd regenerative response area (54C) regenerates to adjust the 2nd regenerative response area (54B) and the 3rd
The temperature of reaction zone (54C).
7. a kind of catalyst regenerator for realizing catalyst multi-stage fluidized regeneration method, it is characterised in that:
It is divided into catalyst regeneration reactive moieties (5) and gas-solid separate section (6) inside the catalyst regenerator；
It is divided into three fluidized bed regeneration reaction zones up and down in catalyst regeneration reactive moieties in catalyst regenerator shell, three
Area's coaxial arrangement, uses partition (55) between the 1st regenerative response area (54A) of bottom and the 3rd regenerative response area (54C) at middle part
It separates, is vertically arranged delivery pipe (53) in the 3rd regenerative response area (54C), delivery pipe (53) entrance and the 1st regenerative response area
(54A) connection, delivery pipe (53) exit are the delivery pipe outlet cone (53B) that diameter gradually increases, delivery pipe outlet cone
The outlet (53B) setting catalyst and flue gas orifice plate (56A), the catalyst and flue gas orifice plate (56A) become the 1st regenerative response area
The boundary of (54A) and the 2nd regenerative response area (54B) of the top, in the 3rd regenerative response area (54C) and the 2nd regenerative response area
Gas distribution grid (56B) is set between (54B), which becomes the 3rd regenerative response area (54C) and the 2nd regeneration
Boundary between reaction zone (54B)；
When the outlet delivery pipe outlet cone (53B) is identical as position catalyst regenerator size, delivery pipe outlet cone
The catalyst and flue gas orifice plate (56A) of the outlet end body (53B) become the 2nd regenerative response area (54B) of top and the 3rd regeneration of centre is anti-
The boundary of area (54C) is answered, while also becoming the boundary in the 1st regenerative response area (54A) of the 2nd regenerative response area (54B) and lower section, and
As the gas distribution grid in the 2nd regenerative response area (54B), channel (56C) is set on delivery pipe outlet cone (53B)；It is described
First gas distributor (52A) is arranged in 1st regenerative response area (54A) bottom section, the 3rd regenerative response area (54C) bottom
Second gas distributor (52B) is arranged in region, and second gas distributor (52B) is distributor pipe.
8. realizing the catalyst regenerator of catalyst multi-stage fluidized regeneration method as claimed in claim 7, which is characterized in that when
When a delivery pipe being arranged between the 1st regenerative response area (54A) and the 2nd regenerative response area (54B), delivery pipe is arranged in catalyst
On regenerator axis, when multiple delivery pipes are arranged, delivery pipe is circumferentially uniformly distributed in catalyst regenerator cross section；Go out in delivery pipe
Delivery pipe outlet cone is set at mouthful, and catalyst and flue gas orifice plate is arranged in delivery pipe outlet cone upper end.
9. realizing the catalyst regenerator of catalyst multi-stage fluidized regeneration method as claimed in claim 7, which is characterized in that
Catalyst or semi regeneration agent delivery pipe (59B) is arranged in 2nd regenerative response area (54B).
10. realizing the catalyst regenerator of catalyst multi-stage fluidized regeneration method as claimed in claim 7, which is characterized in that
It is anti-that the catalyst inlet pipe (72B) of setting catalyst heat collector or cooler (7), heat collector or cooler (7) is located at the 2nd regeneration
It answers area (54B), catalyst outlet pipe (71B) is located at the 3rd regenerative response area (54C).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810535704.7A CN110237779A (en) | 2018-05-29 | 2018-05-29 | A kind of catalyst multi-stage fluidized regeneration method and catalyst regenerator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810535704.7A CN110237779A (en) | 2018-05-29 | 2018-05-29 | A kind of catalyst multi-stage fluidized regeneration method and catalyst regenerator |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110237779A true CN110237779A (en) | 2019-09-17 |
Family
ID=67882880
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810535704.7A Pending CN110237779A (en) | 2018-05-29 | 2018-05-29 | A kind of catalyst multi-stage fluidized regeneration method and catalyst regenerator |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110237779A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111992142A (en) * | 2020-08-07 | 2020-11-27 | 北京航天试验技术研究所 | Device for isothermal conversion reaction of para-hydrogen |
Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4664778A (en) * | 1985-04-05 | 1987-05-12 | Total Engineering And Research Company | Method for regeneration of resid cracking catalyst |
| CN101391234A (en) * | 2008-10-30 | 2009-03-25 | 石宝珍 | Catalyst multistage regeneration method and device |
| CN103739428A (en) * | 2012-10-17 | 2014-04-23 | 中国石油化工股份有限公司 | Device for producing low-carbon olefins from methanol |
| CN104549566A (en) * | 2013-10-17 | 2015-04-29 | 中国石油化工股份有限公司 | Catalytic conversion catalyst regenerator and regeneration method |
| CN105505441A (en) * | 2016-01-06 | 2016-04-20 | 石宝珍 | Catalytic cracking reaction regeneration method and device |
| CN105521832A (en) * | 2014-09-30 | 2016-04-27 | 中国石油化工股份有限公司 | Catalytic cracking catalyst regeneration method and device |
| CN105849235A (en) * | 2014-10-09 | 2016-08-10 | 石宝珍 | Regeneration method for catalytic cracking reaction |
| CN105983455A (en) * | 2015-01-28 | 2016-10-05 | 中国石化工程建设有限公司 | Regeneration method of catalyst for producing aromatic hydrocarbon from organic oxide through catalytic conversion |
| CN106732823A (en) * | 2016-11-16 | 2017-05-31 | 青岛京润石化设计研究院有限公司 | A kind of regenerating catalyst in fluidized bed method |
| CN108889341A (en) * | 2018-07-12 | 2018-11-27 | 青岛京润石化设计研究院有限公司 | A kind of regenerating catalyst in fluidized bed method |
-
2018
- 2018-05-29 CN CN201810535704.7A patent/CN110237779A/en active Pending
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4664778A (en) * | 1985-04-05 | 1987-05-12 | Total Engineering And Research Company | Method for regeneration of resid cracking catalyst |
| CN101391234A (en) * | 2008-10-30 | 2009-03-25 | 石宝珍 | Catalyst multistage regeneration method and device |
| CN103739428A (en) * | 2012-10-17 | 2014-04-23 | 中国石油化工股份有限公司 | Device for producing low-carbon olefins from methanol |
| CN104549566A (en) * | 2013-10-17 | 2015-04-29 | 中国石油化工股份有限公司 | Catalytic conversion catalyst regenerator and regeneration method |
| CN105521832A (en) * | 2014-09-30 | 2016-04-27 | 中国石油化工股份有限公司 | Catalytic cracking catalyst regeneration method and device |
| CN105849235A (en) * | 2014-10-09 | 2016-08-10 | 石宝珍 | Regeneration method for catalytic cracking reaction |
| CN105849235B (en) * | 2014-10-09 | 2017-11-03 | 石宝珍 | A kind of catalytic cracking reaction renovation process |
| CN105983455A (en) * | 2015-01-28 | 2016-10-05 | 中国石化工程建设有限公司 | Regeneration method of catalyst for producing aromatic hydrocarbon from organic oxide through catalytic conversion |
| CN105505441A (en) * | 2016-01-06 | 2016-04-20 | 石宝珍 | Catalytic cracking reaction regeneration method and device |
| CN106732823A (en) * | 2016-11-16 | 2017-05-31 | 青岛京润石化设计研究院有限公司 | A kind of regenerating catalyst in fluidized bed method |
| CN108889341A (en) * | 2018-07-12 | 2018-11-27 | 青岛京润石化设计研究院有限公司 | A kind of regenerating catalyst in fluidized bed method |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111992142A (en) * | 2020-08-07 | 2020-11-27 | 北京航天试验技术研究所 | Device for isothermal conversion reaction of para-hydrogen |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105505441B (en) | A kind of catalytic cracking reaction regeneration method and device | |
| CN101391234B (en) | Catalyst multistage regeneration method and device | |
| CN105849235B (en) | A kind of catalytic cracking reaction renovation process | |
| CN103028449B (en) | catalytic conversion catalyst regenerator | |
| CN105585396A (en) | Method for preparing low carbon olefin by oxygen-containing compound | |
| CN104549566B (en) | Catalytic conversion catalyst regenerator and renovation process | |
| CN204474555U (en) | A kind of system of organic oxygen compound catalytic cracking aromatic hydrocarbons | |
| CN114262624B (en) | Method and device for catalytic cracking of double-component granular catalyst coupling fluidized bed | |
| CN103028450B (en) | catalytic conversion catalyst regeneration method | |
| US8128807B2 (en) | FCC separator without a reactor | |
| CN110237779A (en) | A kind of catalyst multi-stage fluidized regeneration method and catalyst regenerator | |
| CN104419457B (en) | A kind of double lift pipe catalytic cracking method and device | |
| CN104342196B (en) | A kind of catalyst cracking method and device thereof | |
| CN107262162A (en) | A kind of renovation process of coked catalyst | |
| CN108889341A (en) | A kind of regenerating catalyst in fluidized bed method | |
| US5215720A (en) | Conversion of side by side FCC unit | |
| CN204469680U (en) | The regenerative system of a kind of organic oxygen compound catalytic cracking arenes catalytic agent | |
| CN104549567A (en) | Method for regenerating catalyst for reducing nitrides in flue gas | |
| CN104341259B (en) | A kind of catalyzing methanation of synthesis gas method and device | |
| CN104513670B (en) | A kind of catalyst cracking method and device | |
| CN206996619U (en) | A kind of catalytic cracked regenerated system | |
| CN201313049Y (en) | Catalyst multi-stage regeneration device | |
| CN105713676B (en) | Method and device for gasifying coke-containing solid particles | |
| CN205774340U (en) | A kind of catalytic cracking reaction regenerating unit | |
| CN104342197B (en) | A kind of double lift pipe catalytic cracking method and device thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20190917 |