CN107987869A - A kind of fluidized catalytic cracker of riser and its composition - Google Patents
A kind of fluidized catalytic cracker of riser and its composition Download PDFInfo
- Publication number
- CN107987869A CN107987869A CN201711422907.7A CN201711422907A CN107987869A CN 107987869 A CN107987869 A CN 107987869A CN 201711422907 A CN201711422907 A CN 201711422907A CN 107987869 A CN107987869 A CN 107987869A
- Authority
- CN
- China
- Prior art keywords
- section
- catalyst
- riser
- sedimentation separation
- cracking
- 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
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
-
- 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
- B01J8/005—Separating solid material from the gas/liquid stream
- B01J8/007—Separating solid material from the gas/liquid stream by sedimentation
-
- 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
- B01J8/1872—Details of the fluidised bed reactor
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Combustion & Propulsion (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides a kind of riser and its fluidized catalytic cracker of composition.A kind of riser, includes putting forward section, first cracking conversion zone, the first sedimentation separation section, the second soaking section and the second sedimentation separation section in advance from the bottom to top successively；Settlement separator is respectively provided with the first sedimentation separation section and the second sedimentation separation section.The present invention can not only avoid cracking reaction, but also can reduce the difficulty of device replacement, reduce the threshold of technological change, make MFCC techniques be more easy to promote.
Description
Technical field
The present invention relates to chemical technology field, disguises more particularly, to the fluidized catalytic cracking of a kind of riser and its composition
Put.
Background technology
As increasingly deficient and industrial chemicals the diversification and scale of crude resources, the few aerogenesis body of crude oil processing are more
Production light oil has become a kind of long-term trend, and catalytic cracking is as main crude oil secondary operation technique, the development of its technology
Adapt to the requirement of this trend and seem even more important.
At present, both sides is main below petroleum chemical industry, conventional riser fluid catalytic cracking generally existing
Problem.
(1) reaction time is long, diesel product is of poor quality：
The reaction time of riser reactor is generally higher than 3 seconds (being determined by lifting length of tube or process form), long
Reaction time exacerbates the cracking reaction (i.e. so-called secondary response) excessively of raw material product, causes cracked gas yield high, vapour, bavin
Oil distillate yield reduces, and the catalytic diesel oil quality of generation is gradually deteriorated also with the extension in reaction time.
(2) regenerated catalyst temperature is high, oil ratio is low
The regeneration temperature of catalyst is generally at 670~720 DEG C.Limited by device thermal balance, higher regenerated catalyst temperature
Make the oil ratio of heavy oil riser reactor relatively low, generally 5~7；
For this reason, each major oil companies are directed to the research and development of new catalytic cracking process technology one after another both at home and abroad.
The FDFCC- III of Sinopec Luoyang Petrochemical Engineering Corporation's exploitation and the MZCC techniques of Petroleum Univ.'s exploitation have run through " oil
The technical concept of the contact of agent low temperature, high agent-oil ratio ".III technology industrial implementations of FDFCC- the result shows that, " finish low temperature connects
Tactile, high agent-oil ratio " technology inhibits the heat cracking reaction carried out in accordance with free radical mechanism, enhances the catalysis of carbonium ion mechanism
Cracking reaction, makes catalytic cracking product selectively be improved.
Milliscond Catalytic Cracking Process (MSCC) work that UOP is developed jointly with CEPOC companies
The gas-solid short contact down-flow fluidized bed using ECT that skill technology, Stone＆Webster, Texco companies and chemical industry system of Tsinghua University were once studied
Reaction technology etc..The common ground of these technologies be all by varying reactor pattern reach shorten the reaction time (1 second with
It is interior) purpose, so as to reduce the secondary response of oil gas in reactor, reduce coke, dry gas yied, improve yield of light oil.
The technical characterstic of MSCC techniques (United States Patent (USP) USP5462652) is：A. catalyst is conventional FCC catalyst or special
Use catalyst.B. reacting-settler top sets catalyst blending tank, and blending tank carries out the uniformly mixed of catalyst using water vapour
Close；Mixed catalyst room is set at the top of reacting-settler, and catalyst enters reacting-settler by mixed catalyst room central opening.
C. the stripping of the reaction of catalyst and raw material and reclaimable catalyst carries out in reacting-settler, catalyst flow direction to
Under, raw material injection direction and catalyst flow direction are into an angle of 90 degrees, the plug-in cyclone separator of reacting-settler.D. it is a part of to be generated
Catalyst is promoted to regenerator by first riser and carries out coke burning regeneration, and another part reclaimable catalyst is by second riser
Catalyst blending tank is promoted to, the catalyst after regeneration is promoted to catalyst blending tank and reclaimable catalyst by the 3rd riser
Mix to be lowered into the mixed catalyst temperature of reacting-settler.Due to above technical characteristic, MSCC technologies are settled in reaction
Raw material short reaction time, low finish Contact Temperature, high agent-oil ratio operation are realized in device, declines the dry gas of device, coke yield,
Liquid yield increases substantially, and product, which is distributed, to be improved.At present, MSCC technologies have been successfully made industrial implementation.With
Conventional FCC is compared, and the dry gas yied of MSCC reduces by 2%, and petrol and diesel oil yield improves 11v%.Phase early 1990s, the U.S.
Its 500,000 t/aFCC plant modification is MSCC commerical test devices by Derby oil plants, in feedstock oil mixed with nearly 20% de- drip
Blue or green oil (DAO), (R+M)/2 due to requiring gasoline are not less than 87 so that riser cracking operation is transported in the case where crossing cracking pattern
OK.The result shows that the short oil agent time of contact due to MSCC techniques so that the selectivity of dry gas substantially improves, and due to urging
Agent charcoal difference declines, and reduces regeneration temperature and adds oil ratio.Therefore, the conversion ratio of feedstock oil is improved from 60%~80%
To 70%~85%, particularly gasoline selective significantly improves (gasoline yield increase about 13%), while fluid product (including liquid
Change gas, gasoline and diesel oil) total recovery also increases.In addition, its hydrogen output and hydrogen/methane ratio decline about 25%, the tolerance to Ni
Property enhancing, and reduce tonic amount.Octane number and diesel cetane-number also increase.
2002, the FlyingJ oil plants in the U.S. filled its 500,000 tons/year of moving bed catalytic cracking plant modifications for MSCC
Put.MSCC technologies have 2 sets of industrialized units and are operating at present.A set of EaglePoint positioned at Coastal companies is refined oil
Factory, disposal ability are 2,800,000 tons/year；Another set of to build TranAmerican oil refinery companies in, disposal ability is 5,000,000 tons/year.
Using such as table 1 below of the typical production data before and after MSCC technological transformations.
Table 1
| Product | Conventional FCC | MSCC |
| Dry gas, % | 4.0 | 2.0 |
| Raw material for alkylation, v% | 16.0 | 21.0 |
| Gasoline+light cycle oil, v% | 74.0 | 85.0 |
| Bottom of tower heavy oil, v% | 11.0 | 4.0 |
Although MSCC technologies have many advantages, but still have the following disadvantages：
(1) in high agent-oil ratio operation, the catalyst for participating in reaction is the mixture of regenerated catalyst and reclaimable catalyst,
The mixed catalyst is relatively low to the cracking activity of raw material, product certainly will be distributed and bring adverse effect.
(2) technical process and complicated.The basic nothing of MSCC technological transformations is carried out on existing catalytic cracking commercial plant
Method carries out (unless new device).It is set to be difficult to promote, spread to major refinery.
In conclusion by being improved the process equipment of existing catalytic cracking unit, short reaction time, big agent are realized
Oil can reduce cracked gas and coke yield, improve yield of light oil, to being refined by leading China of catalytic cracking process than operation
Oily industry has great importance.
The millisecond fluidisation of Sinopec Engineering (Group) Co., Ltd. Luoyang Technology R ＆ D Center exploitation is urged for this
Change cracking (Millisecond Fluid Catalytic Cracking, abbreviation MFCC) technique using short reaction time (0.3~
1.2 seconds) and high agent-oil ratio (7~12) technical measures, can make compared with conventional FCC dry gas yied reduce by 40% or so, liquefaction
Gas reduces by 2~5 percentage points, and light oil yield improves 3~7 percentage points, and coke yield slightly reduces, and product property substantially changes
Kind, the economic benefit of catalytic cracking unit is significantly improved.The main business development of the technology and Sinopec is closely related,
It should be with a wide range of applications.
3rd, the technical principle and technical characteristic of MFCC techniques
(1) shorten the reaction time, suppress secondary response.It is catalytic cracked into a typical parallel sequence reaction process.With
The extension in reaction time, the secondary response aggravation of generation oil gas, product selectivity deteriorate；If shortening the reaction time, can reduce
Secondary response, improves product selectivity；MFCC techniques realize that short reaction time operates for (0.3~1.2 second) using novel reactor,
Farthest suppress generation oil gas secondary response.
(2) high agent-oil ratio operation is carried out, it is ensured that the conversion per pass depth of raw material.Raw material can be made by significantly shortening the reaction time
Conversion per pass declines, and improving reaction temperature, raising catalyst activity or oil ratio can make up since the reaction time contracts
Feed stock conversion caused by short loses.Heat cracking reaction can be aggravated by improving reaction temperature, using high activated catalyst or raising
The equilibrium activity of device catalyst will then pay through the nose, and therefore, preferably select to properly increase device operation oil ratio, that is, carry
The dynamic activity of high catalyst ensures the conversion per pass depth of raw material.MFCC techniques are exactly to use of a relatively high oil ratio (7
~12) Hydrocarbon Content by Catalytic Cracking Operation is carried out to overcome the reaction time to shorten the negative effect to reaction process.
(3) using the method for the secondary injection riser reactor of catalyst, realize that riser reactor catalyst relay is anti-
Should.So as to ensure the conversion per pass of riser reactor, the elimination riser reactor reaction time is short, and conversion per pass is low
Influence.
Although comparing FCC techniques, MFCC techniques have many advantages, such as, the cost as how relatively low replaces with FCC techniques
MFCC techniques are the main problem to be solved at present.
In view of this, it is special to propose the present invention.
The content of the invention
The first object of the present invention is to provide a kind of riser, and the riser solves conventional FCC process replacement
The problem of more exchange device causes cost high comprehensively is needed for MFCC techniques.
The second object of the present invention is to provide a kind of fluidized catalytic cracker, which only needs to fill in conventional FCC
The interlude for the riser put adds settlement separator, and therefore, the cost of more new process is low, easily promotes.
In order to realize the above object the present invention provides following technical scheme：
A kind of riser, includes carrying section, first cracking conversion zone, the first sedimentation separation section, second in advance from the bottom to top successively
Soaking section and the second sedimentation separation section；
Settlement separator is respectively provided with the first sedimentation separation section and the second sedimentation separation section.
The riser of the present invention can be suitably used for MFCC techniques, that is, realize that the catalysis of " contact of finish low temperature, high agent-oil ratio " is split
Change technology, and compared with traditional FCC riser reactors, change is smaller, it is only necessary to (this hair in the middle part of existing riser
The bright medium position is not centre, but is determined by soaking time) position adds settlement separator, so as to pre-
Finish separation first is carried out to cracked reaction product, so as to achieve the purpose that to terminate catalytic cracking reaction.In other words, it is of the invention to carry
Riser is to be divided existing riser by the settlement separator (settlement separator in corresponding first sedimentation separation section) added
For two conversion zones, the first conversion zone (i.e. first cracking conversion zone) is important soaking section, since space length shortens,
Reaction duration also necessarily shortens, therefore can realize the purpose reacted in short term, avoids cracking reaction.In the first sedimentation separation section,
After finish separation, reclaimable catalyst recycling, oil gas enters the second soaking section, in this conversion zone oil gas reaction terminating or hair
Raw faint catalytic cracking reaction, due to shortage catalyst, the catalytic cracking reaction in this section was not cracking reaction.It
Material enters the second sedimentation separation section afterwards, is separated by finish, collects various oil gas.
In summary, the reaction structure and length difference of the riser used in riser and conventional FCC process of the invention
It is different little, therefore, when FCC techniques are replaced with MFCC techniques, it is only necessary to add settlement separator i.e. in the interlude of riser
Can, comprehensive more exchange device is avoided, therefore, renewal cost is low, easily promotes.
The structure of above riser can also be improved from the following aspect, such as：
Preferably, the one end of the second sedimentation separation section away from second soaking section is also associated with stripping section,
The solids outlet port of the first sedimentation separation section is passed through the stripping section.
The stripping section is identical with the stripping section effect in existing riser, i.e., with the oil adsorbed on vapor Removal of catalyst
Oil gas between gas and displacement catalyst granules, in case it by catalyst entrainment to catalyst regenerator, increases the burning of regenerator
Burnt load.
The solids outlet port of the first sedimentation separation section is the outlet of catalyst, and the position of the outlet is preferably above
The entry position of catalyst in the stripping section, to make catalyst save energy consumption from flowing into stripping section using gravity,
For this reason, stripping section can be set with the first sedimentation separation section parallel side-by-side.
Preferably, second soaking section is additionally provided with catalyst inlet.
Fresh or regenerated catalyst is injected in the second soaking section, by adjusting low oil ratio, makes oil gas few
Beneficial cracking reaction occurs under the action of amount catalyst, rather than crosses cracking reaction, vapour can be improved to a certain extent, diesel oil evaporates
Divide yield.In other words, fresh or regenerated catalyst is injected in the second soaking section, can guarantee that the one way of riser reactor
Conversion ratio, the elimination first segment riser reactor reaction time is short, the low influence of conversion per pass.
Preferably, stripping distribution rings are additionally provided with the bottom of settler in the first sedimentation separation section.
The stripping distribution rings are identical with the effect of traditional stripping section, can remove and be inhaled on first time sedimentation separation rear catalyst
Oil gas between attached oil gas and displacement catalyst granules.
Preferably, the top of the first cracking conversion zone is additionally provided with catalyst inlet.
Equally, in addition to carrying the catalyst of section supply in advance, catalyst inlet is passed through on the top of first cracking conversion zone
Fresh or regenerated catalyst is injected, oil ratio can be improved, so as to improve cracking effect.
Preferably, the settlement separator during the first sedimentation separation section and the second sedimentation separation section are interior is three leaf grooves
Fast parted hair type or ejection separate fast parted hair type.
The present invention is not limited the model of settlement separator, and the first sedimentation separation section and second sedimentation
Settlement separator in segregation section can use identical or different type.
When the riser of the present invention is used for fluid catalytic cracking process, should also arrange in pairs or groups other necessaries composition fluidisations
Catalytic cracking single unit system, such as catalyst regenerator is further included, the stripping section is connected with the catalyst regenerator.
Catalyst regeneration is a flow critically important in catalytic cracking, can largely reduce cost, extends device
Service life.
Preferably, regeneration feed bin is further included.
Regeneration feed bin can be used as terminal, and regenerated catalyst is supplied for riser.
Preferably, when second soaking section is equipped with catalyst inlet, the regeneration feed bin is split with described second
Change the catalyst inlet connection of conversion zone.
Regenerate feed bin and provide less amount of regenerated catalyst for the second soaking section, promotion is conducive to generate petrol and diesel oil
Reaction carry out.
Preferably, when the first cracking conversion zone is equipped with catalyst inlet, the regeneration feed bin is split with described first
Change the catalyst inlet connection of conversion zone.
With the progress of reaction, the catalyst activity on the top of first cracking conversion zone reduces, and steps into urge thereto at this time
Agent, it is ensured that the catalyst activity in first cracking conversion zone is consistent, is conducive to improve the yield of petrol and diesel oil.
To sum up, compared with prior art, invention achieves following technique effect：
(1) present invention can not only avoid cracking reaction, but also can reduce the difficulty of device replacement, reduce technological change
Threshold, makes MFCC techniques be more easy to promote；
(2) relay that can realize catalyst in riser by setting the supplementing structure of catalyst is reacted, so as to ensure
The conversion per pass of riser reactor, the elimination first segment riser reactor reaction time is short, the low influence of conversion per pass.
Brief description of the drawings
, below will be to specific in order to illustrate more clearly of the specific embodiment of the invention or technical solution of the prior art
Embodiment or attached drawing needed to be used in the description of the prior art are briefly described, it should be apparent that, in describing below
Attached drawing is some embodiments of the present invention, for those of ordinary skill in the art, before not making the creative labor
Put, other attached drawings can also be obtained according to these attached drawings.
Fig. 1 is the schematic diagram for the fluidized catalytic cracker that the embodiment of the present invention 1 provides；
Fig. 2 is the schematic diagram for the fluidized catalytic cracker that the embodiment of the present invention 2 provides；
Fig. 3 is the schematic diagram for the fluidized catalytic cracker that the embodiment of the present invention 3 provides；
Reference numeral：
1- gas distribution rings, 2- regenerative agent feed bins, 3- regenerative agent pipes, 4- regenerative agent conveying hoisting pipes, 5- propose section distribution in advance
Ring, 6- put forward section in advance, 7- regenerator sloped tubes, 8- raw material nozzles, 9- first segment riser reactors, 10- spent agent circulation pipes, and 11- is thick
Distribution rings are stripped, 12- separating of oil and agent settlers, 13- oil, agent are through quick disconnector, 14- second segment riser reactors, 15-
Regenerative agent inlet, 16- settlers, 17- stripping sections, 18- inclined tubes to be generated.
Embodiment
Technical scheme is clearly and completely described below in conjunction with the drawings and specific embodiments, but
Be it will be understood to those of skill in the art that following described embodiment is part of the embodiment of the present invention, it is rather than whole
Embodiment, is merely to illustrate the present invention, and is not construed as limiting the scope of the invention.Based on the embodiments of the present invention, ability
Domain those of ordinary skill all other embodiments obtained without making creative work, belong to guarantor of the present invention
The scope of shield.The person that is not specified actual conditions in embodiment, the condition suggested according to normal condition or manufacturer carry out.Agents useful for same
It is the conventional products that can be obtained by commercially available purchase or production firm person is not specified in instrument.
The core of the present invention is improved in the riser in catalytic cracking unit just like lower structure：
A kind of riser, includes carrying section, first cracking conversion zone, the first sedimentation separation section, second in advance from the bottom to top successively
Soaking section and the second sedimentation separation section；
Settlement separator is respectively provided with the first sedimentation separation section and the second sedimentation separation section；
It is described pre- to carry section, the first cracking conversion zone, the first sedimentation separation section and second soaking section
It is preferred that it is coaxially disposed.
The riser of the present invention can be suitably used for MFCC techniques, that is, realize that the catalysis of " contact of finish low temperature, high agent-oil ratio " is split
Change technology, and compared with traditional FCC riser reactors, change is smaller, it is only necessary to (this hair in the middle part of existing riser
The bright medium position is not centre, but is determined by soaking time) position adds settlement separator, so as to pre-
Finish separation first is carried out to cracked reaction product, so as to achieve the purpose that to terminate catalytic cracking reaction.In other words, it is of the invention to carry
Riser is to be divided existing riser by the settlement separator (settlement separator in corresponding first sedimentation separation section) added
For two conversion zones, the first conversion zone (i.e. first cracking conversion zone) is important soaking section, since space length shortens,
Reaction duration also necessarily shortens, therefore can realize the purpose reacted in short term, avoids cracking reaction.In the first sedimentation separation section,
After finish separation, reclaimable catalyst recycling, oil gas enters the second soaking section, in this conversion zone oil gas reaction terminating or hair
Raw faint catalytic cracking reaction, due to shortage catalyst, the catalytic cracking reaction in this section was not cracking reaction.It
Material enters the second sedimentation separation section afterwards, is separated by finish, collects various oil gas.
Different embodiments do following optimization on this nuclear structure：
Preferably, the one end of the second sedimentation separation section away from second soaking section is also associated with stripping section,
The solids outlet port of the first sedimentation separation section is passed through the stripping section.
Preferably, second soaking section is additionally provided with catalyst inlet.
Preferably, stripping distribution rings are additionally provided with the bottom of settler in the first sedimentation separation section.
Preferably, the top of the first cracking conversion zone is additionally provided with catalyst inlet.
Preferably, the settlement separator during the first sedimentation separation section and the second sedimentation separation section are interior is three leaf grooves
Fast parted hair type or ejection separate fast parted hair type.
Embodiment 1
The device of fluid catalytic cracking is as shown in Figure 1：
Regenerated catalyst (or fresh catalyst) from regenerator initially enter it is pre- put forward section 6, interior be equipped with pre- puies forward section point
Cloth ring 5 is carried regenerator sloped tube 7 is also set up in section 6 in advance, to pass through regenerated catalyst so that catalyst fully fluidizes.In pre-lift vapour
And under the feedstock oil double action sprayed into through raw material nozzles 8, catalyst together enters first segment riser reactor with feedstock oil
9, carry out catalytic cracking reaction.After the reaction time of MFCC technological requirements is reached (i.e. first segment reaction length with it is required
Reaction time is related), oil, agent enter oil, agent pre-separation settler 12 through quick disconnector 13, and are promptly released.After separation
Reclaimable catalyst by after the stripped vapor tentatively stripping of thick stripping distribution rings 11, enter through spent agent circulation pipe 10 and strip
Section 17；Oil gas enters second segment riser reactor 14 after separation.Into second segment riser reactor 14 oil gas with coming from
The regenerative agent that regenerative agent feed bin 2 is injected through regenerative agent conveying hoisting pipe 4, regenerative agent inlet 15 continues Catalytic Cracking Unit of Measure
Should.So as to ensure the conversion per pass of riser reactor, the elimination first segment riser reactor reaction time is short, conversion per pass
The low influence of rate.After the completion of reaction, oil, agent are together separated into settler 16.The oil gas isolated introduces fractionating column from top
Fractionate out qualified products；Spent agent introduces regenerator through inclined tube 18 to be generated after stripping section 17 fully stripping and burns.Regeneration is completed
Regenerative agent afterwards is reintroduced into regenerative agent feed bin 2 and pre lift zone 6, completes whole cyclic process.It is equipped with regenerative agent feed bin
Gas distribution rings 1, so as to which regenerated catalyst is promoted in reactor using gas, are additionally provided with regenerative agent pipe 3 to access regeneration
In device (not shown).
It can be seen from figure 1 that section 6, first segment riser reactor 9, quick disconnector 13 and second segment riser are carried in advance
Reactor, so as to the efficient transportation of raw material, improves energy utilization rate to be coaxially disposed.
Embodiment 2
Difference lies in the position of regenerative agent inlet is different from embodiment 1：It is incomplete in first segment riser reactor 9
Before completing reaction, regenerated catalyst is injected, the agent of 9 reaction of increase first segment riser reactor, oily ratio, come in this form
Ensure the conversion per pass of riser reactor, the elimination first segment riser reactor reaction time is short, and conversion per pass is low
Influence.Other technical process of the embodiment are the same as embodiment 1.
Embodiment 3
Technical process be 1 structure of attached drawing technical process it is identical.Its architectural feature is：By the oil of embodiment 1, agent
It is fast separately that 13 structure of quick disconnector in pre-separation settler is changed into ejection separation by three leaf grooves separately soon.The embodiment
Other technical process are the same as embodiment 1.
Finally it should be noted that：The above embodiments are only used to illustrate the technical solution of the present invention., rather than its limitations；To the greatest extent
Pipe is described in detail the present invention with reference to foregoing embodiments, it will be understood by those of ordinary skill in the art that：Its according to
Can so modify to the technical solution described in foregoing embodiments, either to which part or all technical characteristic into
Row equivalent substitution；And these modifications or replacement, the essence of appropriate technical solution is departed from various embodiments of the present invention technology
The scope of scheme.
Claims (10)
1. a kind of riser, it is characterised in that include proposing section, first cracking conversion zone, the first sedimentation point in advance from the bottom to top successively
From section, the second soaking section and the second sedimentation separation section；
Settlement separator is respectively provided with the first sedimentation separation section and the second sedimentation separation section；
It is described that pre- to carry section, the first cracking conversion zone, the first sedimentation separation section and second soaking section preferred
It is coaxially disposed.
2. riser according to claim 1, it is characterised in that the second sedimentation separation section is away from second cracking
One end of conversion zone is also associated with stripping section, and the solids outlet port of the first sedimentation separation section is passed through the stripping section.
3. riser according to claim 1, it is characterised in that second soaking section is additionally provided with catalyst injection
Mouthful.
4. riser according to claim 1, it is characterised in that in the bottom of settler in the first sedimentation separation section
It is additionally provided with stripping distribution rings.
5. riser according to claim 1, it is characterised in that the top of the first cracking conversion zone is additionally provided with catalysis
Agent inlet.
6. riser according to claim 1, it is characterised in that the first sedimentation separation section and second sedimentation point
From the settlement separator in section fast parted hair type is separated for the fast parted hair type of three leaf grooves or ejection.
7. a kind of fluidized catalytic cracker, it is characterised in that including claim 1-6 any one of them risers.
8. fluidized catalytic cracker according to claim 7, it is characterised in that catalyst regenerator is further included, it is described
Stripping section is connected with the catalyst regenerator.
9. fluidized catalytic cracker according to claim 7, it is characterised in that further include regeneration feed bin.
10. fluidized catalytic cracker according to claim 9, it is characterised in that second soaking section is equipped with
During catalyst inlet, the regeneration feed bin is connected with the catalyst inlet of second soaking section；
Preferably, when the first cracking conversion zone is equipped with catalyst inlet, the regeneration feed bin and the first cracking are anti-
The catalyst inlet of section is answered to connect.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711422907.7A CN107987869A (en) | 2017-12-25 | 2017-12-25 | A kind of fluidized catalytic cracker of riser and its composition |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711422907.7A CN107987869A (en) | 2017-12-25 | 2017-12-25 | A kind of fluidized catalytic cracker of riser and its composition |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN107987869A true CN107987869A (en) | 2018-05-04 |
Family
ID=62041865
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201711422907.7A Pending CN107987869A (en) | 2017-12-25 | 2017-12-25 | A kind of fluidized catalytic cracker of riser and its composition |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107987869A (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102453500A (en) * | 2010-10-21 | 2012-05-16 | 中国石油化工股份有限公司 | Catalytic cracking method and equipment for hydrocarbon oil |
| CN102814151A (en) * | 2011-06-08 | 2012-12-12 | 富德（北京）能源化工有限公司 | Fluidized bed reactor and method for preparing alkene from oxygen-containing compound |
| CN206014777U (en) * | 2016-08-30 | 2017-03-15 | 中石化炼化工程（集团）股份有限公司 | A kind of catalytic cracking unit |
-
2017
- 2017-12-25 CN CN201711422907.7A patent/CN107987869A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102453500A (en) * | 2010-10-21 | 2012-05-16 | 中国石油化工股份有限公司 | Catalytic cracking method and equipment for hydrocarbon oil |
| CN102814151A (en) * | 2011-06-08 | 2012-12-12 | 富德（北京）能源化工有限公司 | Fluidized bed reactor and method for preparing alkene from oxygen-containing compound |
| CN206014777U (en) * | 2016-08-30 | 2017-03-15 | 中石化炼化工程（集团）股份有限公司 | A kind of catalytic cracking unit |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107286972B (en) | A kind of catalysis conversion method of producing more propylene | |
| WO2020015603A1 (en) | Method, reactor and system for catalytic cracking of hydrocarbon oil | |
| CN102925210A (en) | Catalytic cracking method and device with low oil agent contact temperature difference | |
| WO2016110253A1 (en) | Cold regenerated catalyst circulation method and device therefor | |
| CN102952577B (en) | Catalytic conversion method for increasing propylene yield | |
| CN102234534B (en) | Method for processing inferior heavy oil | |
| EP3919589A1 (en) | Method for catalytic conversion of hydrocarbon with downer reactor and device thereof | |
| CN102212390B (en) | Double riser catalytic cracking method and device | |
| CN205821248U (en) | A kind of catalytic conversion reactor | |
| CN102268286A (en) | C4 hydrocarbon catalytic splitting and heavy oil catalytic cracking combined technology and device | |
| CN104418686A (en) | Catalytic conversion method for production of low-carbon olefins and light aromatic hydrocarbons | |
| CN103664454B (en) | A kind of Fischer-Tropsch synthesis oil catalytic reforming of less energy-consumption produces the method for propylene | |
| CN110499181A (en) | A kind of catalyst cracking method and device of the reaction of at the uniform velocity bed | |
| CN107987869A (en) | A kind of fluidized catalytic cracker of riser and its composition | |
| CN103666551B (en) | Catalytic processing method and catalytic processing device of high-temperature Fischer-Tropsch synthetic oil | |
| CN106609151B (en) | A kind of method for producing low-carbon alkene | |
| CN102268291B (en) | Catalytic cracking technology and device for reducing olefins in gasoline | |
| CN109385302B (en) | Catalytic conversion method for increasing yield of gasoline and low-carbon olefin | |
| CN109385297B (en) | Catalytic cracking conversion method for increasing gasoline yield and reducing oil slurry | |
| CN103509593B (en) | A kind of Light hydrocarbon oil catalytic conversion method | |
| CN109385296B (en) | Catalytic conversion method of hydrocarbon oil | |
| CN102268290A (en) | Catalytic cracking method and device | |
| CN105441121B (en) | A kind of catalysis conversion method for producing high-knock rating gasoline | |
| US20130211167A1 (en) | Catalytic conversion method for improving product distribution | |
| CN104418685B (en) | A kind of catalysis conversion method for producing ethene and propylene |
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 | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20180504 |
|
| RJ01 | Rejection of invention patent application after publication |