CN108753356A - A kind of multi-stage countercurrent catalytic cracking/cracking system and method - Google Patents
A kind of multi-stage countercurrent catalytic cracking/cracking system and method Download PDFInfo
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- CN108753356A CN108753356A CN201810646036.5A CN201810646036A CN108753356A CN 108753356 A CN108753356 A CN 108753356A CN 201810646036 A CN201810646036 A CN 201810646036A CN 108753356 A CN108753356 A CN 108753356A
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- gas
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- fluidized bed
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- gas mixture
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Classifications
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- 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
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
- C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
- C10G55/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one catalytic cracking step
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/70—Catalyst aspects
Abstract
The present invention provides a kind of multi-stage countercurrent catalytic cracking/cracking systems and method, the system to include：In one-to-one at least the two-stage downflow fluidized bed and at least two fast gas-solid separation devices of ladder distribution；The gas vent of each fast gas-solid separation device is connected to upper level downflow fluidized bed, and its solid material outlet is connected to next stage downflow fluidized bed；Most bottom grade downflow fluidized bed receives oil gas raw material and catalyst, and gas mixture is formed after catalytic cracking/cracking reaction；Other receive gas mixtures and catalyst per level-one downflow fluidized beds, carry out catalytic cracking/cracking reaction, by after reaction gas mixture and catalyst transport give corresponding fast gas-solid separation device；Fast gas-solid separation device separation oil and gas mixture and catalyst convey gas mixture by gas vent, and conveying catalyst is exported by solid material.This programme can increase reaction motive force, can be in offer differential responses atmosphere at different levels, high producing light olefins and aromatic hydrocarbons.
Description
Technical field
The present invention relates to Petroleum Processing Technology field, more particularly to a kind of multi-stage countercurrent catalytic cracking/cracking system and side
Method.
Background technology
Catalytic cracking/cracking is an essential industry process in petroleum refining industry.It is attached in catalytic cracking/cracking process
Value added high product is mostly the intermediate product of consecutive chemical reaction, such as gasoline and kerosene etc., and strictly control the reaction time with
And reduce the generation that the gas-solid air-teturning mixed phenomenon in reactor is conducive to reaction process intermediate product.
It continues to use the upward rapid circulating fluidized bed system of cocurrent in enterprise mostly at present and carries out catalytic cracking/cracking reaction, instead
From the bottom end of reactor to tip motions, i.e. the direction of motion of oil gas raw material and catalyst is for seasonable oil gas raw material and catalyst
Inverse gravity field direction.
In the process, catalyst causes itself and oil gas raw material since gravity is easily there is a phenomenon where sliding downwards
Gas-solid back-mixing, cause reactor axis to density of catalyst be unevenly distributed, and then partial catalyst is caused to stop in the reactor
Overlong time, causes the reaction time long, is thus unfavorable for the generation of reaction intermediate.
Invention content
An embodiment of the present invention provides a kind of multi-stage countercurrent catalytic cracking/cracking system and method, be conducive to improve reaction
Selectivity, improve the yield of reaction intermediate.
In a first aspect, an embodiment of the present invention provides a kind of multi-stage countercurrent catalytic cracking/cracking systems, including：In ladder
At least two-stage downflow fluidized bed and at least two fast gas-solid separators of distribution；Wherein,
The downflow fluidized bed and the fast gas-solid separator correspond, downflow fluidized described in every level-one
The discharge port of bed reactor is connected to the gas-solid mixing phase entrance of the corresponding fast gas-solid separator；
Gas vent per the corresponding fast gas-solid separator of downflow fluidized bed described in level-one with it is corresponding
Upper level downflow fluidized bed feed inlet connection；
Solid material outlet per the corresponding fast gas-solid separator of downflow fluidized bed described in level-one with it is corresponding
Next stage downflow fluidized bed feed inlet connection；
It is anti-to carry out catalytic cracking/cracking for receiving oil gas raw material and catalyst for most bottom grade downflow fluidized bed
It answers, forms gas mixture, and the catalyst and the gas mixture are conveyed to the corresponding gas-solid quick separating
Device；
In addition to the grade downflow fluidized bed of the most bottom, downflow fluidized bed described in every level-one, for receiving
Gas mixture and catalyst, carry out catalytic cracking/cracking reaction, and by after reaction gas mixture and catalyst transport give
The corresponding fast gas-solid separator；
Each described fast gas-solid separator, for receiving gas mixture and catalyst detach,
And the gas mixture is conveyed by the gas vent of itself, the catalysis is conveyed by the solid material outlet of itself
Agent.
Optionally,
Further comprise：Stripper, regenerator and conveying hoisting pipe；Wherein,
The quick gas-solid corresponding with most bottom grade downflow fluidized bed of the catalyst granules entrance of the stripper
The solid material outlet of fast separation device；
The solid material outlet of the particle entrance of the regenerator and the stripper；
One end of the conveying hoisting pipe is connect with the feed inlet of level-one downflow fluidized bed, the other end with it is described again
The particle outlet connection of raw device；
The corresponding fast gas-solid separator of most bottom grade downflow fluidized bed, for urging described in isolating
Agent is conveyed to the stripper；
The stripper expects for stripping the gas mixture in the catalyst, and by the solid of itself
Mouth gives the catalyst transport after stripping to the regenerator；
The regenerator, for being regenerated to the catalyst；
The conveying hoisting pipe, it is downflow fluidized bed to the level-one for the catalyst transport after regenerating the regenerator
Reactor.
Optionally,
Further comprise：Fractionating column；Wherein,
The gas vent and the fractionating column of the corresponding fast gas-solid separator of the level-one downflow fluidized bed
Connection；
The corresponding fast gas-solid separator of the level-one downflow fluidized bed, for described after detaching
Gas mixture is conveyed to the fractionating column；
The fractionating column, for in the gas mixture gaseous component and liquid phase component detach, and respectively
The gas phase component after output separation and the liquid phase component.
Optionally,
The downflow fluidized bed includes：Reactor body, cylinder of turning back, gas feed mouth and feeding-in solid body mouth；Its
In,
The reactor body is straight barrel type；
The reactor body is turned back described in being set in cylinder, the feeding mouth of the reactor body and the cylinder company of turning back
It is logical；
The top of the cylinder of turning back be it is bullet-shaped orType；
When the top of the cylinder of turning back is bullet-shaped, the gas feed mouth and the feeding-in solid body mouth are respectively set
In a both sides of turning back；
When the top of the cylinder of turning back isWhen type, the gas feed mouth is arranged described
The centre of type, the feeding-in solid body mouth are set to the side of the cylinder of turning back；
The gas of gas feed mouth fast gas-solid separator corresponding with next stage downflow fluidized bed goes out
Mouth connection；
The feeding-in solid body mouth the solid of fast gas-solid separator corresponding with upper level downflow fluidized bed expects
Mouth connection；
It is upward in the case where outside promotes wind action by the catalyst for cylinder of turning back described in feeding-in solid body mouth entrance
Movement, mixes with the gas mixture entered by the gas feed mouth at the top of the cylinder of turning back, mixed
The catalyst and the gas mixture are entered by the feeding mouth of the reactor body in the reactor body, in institute
It states and carries out catalytic cracking/cracking reaction in reactor body；
Optionally,
The fast gas-solid separator includes：Circular separator main body and gas eduction tube；Wherein,
The opening upwards of the gas-solid mixing phase entrance are set to the side of the circular separator main body outer wall, institute
Stating solid material outlet, Open Side Down, is set to the other side of the circular separator main body outer wall；
One end of the gas eduction tube is arranged in the separator main body, and the other end of the gas eduction tube is institute
State gas vent；
The separator main body receives the gas mixture and the catalyst by the gas-solid mixing phase entrance,
It controls the gas mixture and the catalyst is rotated in circular annular space, make described in the catalyst entrance
Gu material outlet, the gas mixture enter the gas eduction tube, point of the gas mixture and the catalyst is completed
From.
Second aspect, an embodiment of the present invention provides a kind of multi-stage countercurrent catalysis provided using any of the above-described embodiment to split
The method that change/cracking system carries out catalytic cracking/cracking, including：
Oil gas raw material and catalyst are received using most bottom grade downflow fluidized bed, carries out catalytic cracking/cracking reaction,
Gas mixture is formed, and the catalyst and the gas mixture are conveyed to corresponding fast gas-solid separator；
The oil gas is received using every level-one downflow fluidized bed in addition to the grade downflow fluidized bed of most bottom
Mixture and catalyst, carry out catalytic cracking/cracking reaction, and by after reaction gas mixture and catalyst transport to correspond to
The fast gas-solid separator；
The gas mixture and catalyst that receive are detached using each fast gas-solid separator, and led to
The feed inlet that the gas mixture is delivered to upper level downflow fluidized bed by the gas vent of itself is crossed, itself is passed through
The outlet of solid material by the catalyst transport to the feed inlet of next stage downflow fluidized bed.
Optionally,
Further comprise：
Using the most bottom corresponding fast gas-solid separator of grade downflow fluidized bed by the catalyst transport
To stripper；
The gas mixture in the catalyst is stripped using the stripper, and by the catalysis after stripping
Agent is conveyed to the regenerator；
The catalyst is regenerated using the regenerator；
Catalyst transport after being regenerated regenerator using conveying hoisting pipe gives level-one downflow fluidized bed.
Optionally,
Further comprise：
Using the corresponding fast gas-solid separator of level-one downflow fluidized bed by the air-fuel mixture after separation
Object is conveyed to fractionating column；
Using the fractionating column in the gas mixture gaseous component and liquid phase component detach, and respectively it is defeated
Go out the gaseous component after separation and the liquid phase component.
Optionally,
It is described that the gas mixture and catalyst that receive are detached using each fast gas-solid separator,
Including：
The gas mixture and the catalysis are received using the gas-solid mixing phase entrance of the fast gas-solid separator
Agent；
The gas mixture is controlled using the separator main body of the fast gas-solid separator and the catalyst exists
It is rotated in circular annular space, so that the catalyst enters the solid material outlet, the gas mixture enters institute
The gas eduction tube for stating fast gas-solid separator completes the separation of the gas mixture and the catalyst.
Optionally,
The catalyst includes：The molecular sieve that grain size is 25 μm~750 μm；
Optionally,
The temperature of the catalytic cracking/cracking reaction is：550~650 DEG C.
Optionally,
When the catalytic cracking/cracking system includes three-level downflow fluidized bed,
Temperature in level-one down-flow fluidized bed using ECT fluidized-bed reactor is：450~550 DEG C；
Temperature in two level down-flow fluidized bed using ECT fluidized-bed reactor is：500~600 DEG C；
Most bottom grade downflow fluidized bed in temperature be：550~650 DEG C；
Optionally,
The molecular sieve includes：The auxiliary agent based on host agent and ZSM-5 based on Y type molecular sieve；The host agent with
The mass ratio of the auxiliary agent is：1:1~10:1.
An embodiment of the present invention provides a kind of multi-stage countercurrent catalytic cracking/cracking system and methods, downflow fluidized per level-one
The feed inlet of bed reactor is arranged on the top of downflow fluidized bed, and discharge port setting is in bottom end, downstreams at different levels as a result,
Oil gas raw material (most bottom grade downflow fluidized bed) or gas mixture and catalyst in fluidized bed reactor in reaction, from
The feed inlet on downflow fluidized bed top moves to the discharge port of bottom end, which is to be not easy to make along gravitational motion process
The gas-solid back-mixing of olefiant gas mixture or oil gas raw material and catalyst so that the distribution of catalyst reactor is more uniform, has
Conducive to the residence time of effective control catalyst in the reactor, to be conducive to improve the selectivity of reaction.
In addition, it is correspondingly arranged on fast gas-solid separator per level-one downflow fluidized bed, it is downflow fluidized per level-one
Bed reactor after catalytic cracking/cracking reaction, by after reaction gas mixture and catalyst transport give corresponding gas-solid
Fast separation device.Fast gas-solid separator can carry out quick separating to gas mixture and catalyst, to effectively avoid
Excessive catalytic cracking/cracking reaction, i.e., effectively avoid the reaction time of gas mixture long, to be conducive to improve catalysis
The yield of cracking/cracking reaction intermediate product.
In addition, per level-one downflow fluidized bed the solid material outlet of corresponding fast gas-solid separator with it is corresponding under
The feed inlet of level-one downflow fluidized bed is connected to, and the gas vent of each fast gas-solid separator with it is corresponding
The feed inlet of upper level downflow fluidized bed is connected to.This make gas mixture by most bottom grade downflow fluidized bed by
Grade to corresponding upper level downflow fluidized bed convey, while catalyst from level-one downflow fluidized bed step by step to right
The next stage downflow fluidized bed conveying answered so that gas mixture and catalyst carry out counter current contacting, are conducive to enhance
Mass-and heat-transfer motive force between gas mixture and catalyst, and the enhancing of mass transfer force can guarantee catalytic cracking/cracking
The quick progress of reaction, meanwhile, the enhancing of driving force of heat transfer can guarantee that the temperature in downflow fluidized bed is uniform, also favorably
In the quick progress of reaction, avoid the reaction time long, to further be conducive to improve production among catalytic cracking/cracking reaction
The yield of object.
Description of the drawings
In order to more clearly explain the embodiment of the invention or the technical proposal in the existing technology, to embodiment or will show below
There is attached drawing needed in technology description to be briefly described, it should be apparent that, the accompanying drawings in the following description is the present invention
Some embodiments for those of ordinary skill in the art without creative efforts, can also basis
These attached drawings obtain other attached drawings.
Fig. 1 is a kind of structural schematic diagram of multi-stage countercurrent catalytic cracking/cracking system provided by one embodiment of the present invention；
Fig. 2 is a kind of structural representation for multi-stage countercurrent catalytic cracking/cracking system that another embodiment of the present invention provides
Figure；
Fig. 3 is the regenerator in a kind of multi-stage countercurrent catalytic cracking/cracking system provided by one embodiment of the present invention
Structural schematic diagram；
Fig. 4 is a kind of multi-stage countercurrent catalytic cracking/cracking system including fractionating column provided by one embodiment of the present invention
Structural schematic diagram；
Fig. 5 is that the gas-solid in a kind of multi-stage countercurrent catalytic cracking/cracking system provided by one embodiment of the present invention is quick
The structural schematic diagram of separator；
Fig. 6 (a) is the downstream in a kind of multi-stage countercurrent catalytic cracking/cracking system provided by one embodiment of the present invention
The structural schematic diagram of fluidized bed reactor；
Fig. 6 (b) is the downlink in a kind of multi-stage countercurrent catalytic cracking/cracking system that another embodiment of the present invention provides
The structural schematic diagram of fluidized-bed reactor；
Fig. 7 is the downstream in a kind of multi-stage countercurrent catalytic cracking/cracking system that another embodiment of the invention provides
The structural schematic diagram of fluidized bed reactor；
Fig. 8 is a kind of flow chart of catalytic cracking/cleavage method provided by one embodiment of the present invention；
Fig. 9 is a kind of structural schematic diagram of two-stage countercurrent catalytic cracking/cracking system provided by one embodiment of the present invention；
Figure 10 is a kind of structural representation for two-stage countercurrent catalytic cracking/cracking system that another embodiment of the present invention provides
Figure；
Figure 11 is a kind of structural representation of three-level counter-current catalytic cracking/cracking system provided by one embodiment of the present invention
Figure.
Specific implementation mode
In order to make the object, technical scheme and advantages of the embodiment of the invention clearer, below in conjunction with the embodiment of the present invention
In attached drawing, technical scheme in the embodiment of the invention is clearly and completely described, it is clear that described embodiment is
A part of the embodiment of the present invention, instead of all the embodiments, based on the embodiments of the present invention, those of ordinary skill in the art
The every other embodiment obtained without making creative work, shall fall within the protection scope of the present invention.
As shown in Figure 1, an embodiment of the present invention provides a kind of multi-stage countercurrent catalytic cracking/cracking/cracking systems, including：
At least two-stage downflow fluidized bed 101 and at least two fast gas-solid separators 102 being distributed in ladder；Wherein,
The downflow fluidized bed 101 and the fast gas-solid separator 102 correspond, per level-one described under
The discharge port of row fluidized-bed reactor 101 is connected to the gas-solid mixing phase entrance of the corresponding fast gas-solid separator 102；
The gas vent of the corresponding fast gas-solid separator 102 per downflow fluidized bed 101 described in level-one
It is connected to the feed inlet of corresponding upper level downflow fluidized bed 101；
The solid material outlet of the corresponding fast gas-solid separator 102 per downflow fluidized bed 101 described in level-one
It is connected to the feed inlet of corresponding next stage downflow fluidized bed 101；
It is anti-to carry out catalytic cracking/cracking for receiving oil gas raw material and catalyst for most bottom grade downflow fluidized bed
It answers, forms gas mixture, and the catalyst and the gas mixture are conveyed to the corresponding gas-solid quick separating
Device 102；
In addition to the grade downflow fluidized bed of the most bottom, downflow fluidized bed 101 described in every level-one, for connecing
Gas mixture and catalyst are received, carries out catalytic cracking/cracking reaction, and by the gas mixture and catalyst transport after reaction
To the corresponding fast gas-solid separator 102；
Each described fast gas-solid separator 102, for receiving gas mixture and catalyst divide
From, and the gas mixture is conveyed by the gas vent of itself, described in the solid material outlet conveying by itself
Catalyst.
In the above-described embodiments, using stairstepping distribution at least two-stage downflow fluidized bed carry out catalytic cracking/
Cracking reaction carries out catalytic cracking/cracking reaction wherein most bottom grade downflow fluidized bed receives oil gas raw material and catalyst
After generate gas mixture, except most bottom grade downflow fluidized bed in addition to every level-one downflow fluidized bed reception oil gas
Mixture and catalyst, after carrying out catalytic cracking/cracking reaction, the gas mixture after output-response and catalyst.
Since downflow fluidized bed has the property of similar laminar flow, in the catalytic cracking/cracking reaction system,
Using downflow fluidized bed so that the system is content with very little high severe degree condition, such as high temperature and big finish ratio etc..Per level-one
The feed inlet of downflow fluidized bed is arranged on the top of downflow fluidized bed, and discharge port is arranged in bottom end, as a result, respectively
Oil gas raw material (most bottom grade downflow fluidized bed) or gas mixture and catalyst in grade downflow fluidized bed exist
When reaction, the discharge port of bottom end is moved to from the feed inlet on downflow fluidized bed top, gas mixture and catalyst are simultaneously
Stream moves downward, which is along gravitational motion process, and inverse gravity system compared to the prior art does not easily cause air-fuel mixture
The gas-solid back-mixing of object or oil gas raw material and catalyst so that the distribution of catalyst reactor is more uniform, is conducive to effectively control
The residence time of catalyst processed in the reactor, to be conducive to improve the selectivity of reaction.
In addition, it is correspondingly arranged on fast gas-solid separator per level-one downflow fluidized bed, it is downflow fluidized per level-one
Bed reactor after catalytic cracking/cracking reaction, by after reaction gas mixture and catalyst transport give corresponding gas-solid
Fast separation device.Fast gas-solid separator can carry out quick separating to gas mixture and catalyst so that air-fuel mixture
The time of contact of object and catalyst is very short, effectively avoids the reaction time of gas mixture long, to effectively avoid excessively
Catalytic cracking/cracking reaction, and then be conducive to improve catalytic cracking/cracking reaction intermediate product (gasoline and kerosene etc.) production
Rate.
It is noted that per level-one downflow fluidized bed the solid material outlet of corresponding fast gas-solid separator with
The feed inlet of corresponding next stage downflow fluidized bed is connected to, and the gas vent of each fast gas-solid separator
It is connected to the feed inlet of corresponding upper level downflow fluidized bed.This so that gas mixture is downflow fluidized bed by most bottom grade
Reactor is conveyed to corresponding upper level downflow fluidized bed step by step, while catalyst is by level-one downflow fluidized bed
It being conveyed step by step to corresponding next stage downflow fluidized bed so that gas mixture and catalyst carry out counter current contacting, this
So that in other every level-one downflow fluidized beds in addition to level-one downflow fluidized bed, oil gas raw material (most bottom
Grade downflow fluidized bed) and gas mixture contacted with the catalyst of part carbon distribution, avoid oil gas raw material or oil gas
Mixture directly contacted with most fresh catalyst and in the initial period rapid deactivation of reaction so that entire catalytic cracking/split
The transmission motive force of solution system is uniformly distributed.Meanwhile the gas mixture in level-one downflow fluidized bed with it is most fresh
Catalyst contacts, that is, the gas mixture for being reacted to final stage is in contact with most fresh catalyst, is conducive to enhance oil gas
Mass-and heat-transfer motive force between mixture and catalyst, and the enhancing of mass transfer force can guarantee catalytic cracking/cracking reaction
Quick progress, meanwhile, the enhancing of driving force of heat transfer can guarantee that the temperature in downflow fluidized bed is uniform, be also beneficial to anti-
The quick progress answered, avoids the reaction time long, to further be conducive to improve catalytic cracking/cracking reaction intermediate product
Yield.It is understood that the sequence of downflow fluidized bed at different levels is top-down according to catalyst in the present embodiment
What the direction of motion was ranked up, i.e., level-one downflow fluidized bed is highest downflow fluidized bed.
In conclusion multi-stage countercurrent catalytic cracking/cracking/cracking system provided in an embodiment of the present invention, using downstream
The form that fluidized bed reactor is combined with gas-solid gas-solid separating device fast gas-solid separator so that vapor-phase reactant (crude oil or
Gas mixture) and the time of contact of solid-phase reactant (catalyst) it is very short, be very suitable for high severe degree (high oil and big finish
Than) catalytic cracking/cracking reaction.
As shown in Fig. 2, in one embodiment of the invention, which can be into one
Step includes：Regenerator 201, conveying hoisting pipe 202 and stripper 203；Wherein,
The catalyst granules entrance of the stripper 203 quick air corresponding with most bottom grade downflow fluidized bed
The solid material outlet of solid fast separating device；
The solid material outlet of the particle entrance of the regenerator 201 and the stripper 203；
One end of the conveying hoisting pipe 202 is connect with the feed inlet of level-one downflow fluidized bed, the other end and institute
State the particle outlet connection of regenerator 201；
The corresponding fast gas-solid separator of most bottom grade downflow fluidized bed, for urging described in isolating
Agent is conveyed to the stripper 203；
The stripper 203, for being stripped to the gas mixture in the catalyst, and the solid material for passing through itself
The regenerator is given the catalyst transport after stripping in outlet；
The regenerator 201, for being regenerated to the catalyst；
The conveying hoisting pipe 202, for the catalyst transport after regenerating the regenerator 201 to the level-one downlink
Fluidized-bed reactor.
Although catalyst is not involved in catalytic cracking/cracking reaction, but the coke generated in reaction process is easily adhered and is urging
In agent so that catalyst degradation or loss of catalytic activity.In order to maintain the catalytic activity of catalyst, most bottom grade downflow fluidized bed
The corresponding fast gas-solid separator of reactor is by the catalyst transport isolated to stripper, and stripper is to being adhered to catalyst
On gas mixture stripped, for example, by using the gas mixture on steam separating catalyst surface, then stripper is by vapour
Thus catalyst transport after carrying is conducive to yield of light oil to regenerator.Then regenerator utilizes the regeneration from bottom reception
Gas regenerates catalyst, that is, removes the coke adhered on catalyst, restore the catalytic activity of catalyst.For example, utilizing
High temperature dry air regenerates the catalyst such as molecular sieve.Then, regenerator carries the catalyst transport after regeneration to conveying
Riser, conveying hoisting pipe give the catalyst transport after regeneration to level-one downflow fluidized bed, thus not only maintain catalysis
The catalytic activity of agent also achieves recycling for catalyst.Also, the catalyst transport after regenerating is downflow fluidized bed to level-one
Reactor so that most fresh catalyst is in contact with the gas mixture for reacting final stage, be conducive to enhance catalytic cracking/
The depth of cracking reaction.
It is understood that at the initial stage for preparing catalytic cracking/cracking reaction, it is downflow fluidized that catalyst is added to level-one
In bed reactor or regenerator.During catalytic cracking/cracking reaction, downflow fluidized beds at different levels and regeneration
There is no strict sequence between device, i.e., during catalytic cracking/cracking reaction, downflow fluidized beds at different levels with again
Raw device is constantly in operating status.
Further it will be understood that for level-one downflow fluidized bed, there is no upper level is downflow fluidized bed
Reactor, for most bottom grade downflow fluidized bed for, in the absence of level-one downflow fluidized bed, under two-stage
For row fluidized-bed reactor, most bottom grade downflow fluidized bed is two level downflow fluidized bed.
Specifically, as shown in figure 3, regenerator 201 can be turbulent fluidized bed 301, turbulent fluidized bed 301 is internally provided with
One cyclone separator 302, wherein
The two side lower end of the turbulent fluidized bed 301 is respectively arranged with inlet port and outlet port, the feed inlet setting
In the top of the discharge port；
The cyclone separator 302 is arranged inside the turbulent fluidized bed 301；
One end of the conveying hoisting pipe 202 is connected with the discharge port of the turbulent fluidized bed 301, the conveying hoisting pipe
202 other end is connected with the level-one downflow fluidized bed；
The corresponding fast gas-solid separator of most bottom grade downflow fluidized bed, for by the catalyst from institute
The feed inlet for stating turbulent fluidized bed 301 is delivered in the turbulent fluidized bed 301；
The turbulent fluidized bed 301, for using from the regeneration gas of bottom reception by the catalyst existing for inside
It is delivered in the cyclone separator 302；The catalyst that the cyclone separator 302 is discharged is arranged by the discharge port
Go out to the conveying hoisting pipe 202；
The cyclone separator 302, the centrifugal force for being generated using itself, to the catalyst existing for inside and institute
It states regeneration gas to be detached, and the catalyst after separation is expelled to the turbulent fluidized bed 301 from the dipleg of bottom end.
Herein, the most bottom corresponding fast gas-solid separator of grade downflow fluidized bed by the catalyst after separation from
The feed inlet of turbulent fluidized bed side wall lower ends is delivered in turbulent fluidized bed, and catalyst can form flowing inside turbulent fluidized bed
Bed.After regeneration gas enters turbulent fluidized bed from the bottom of turbulent fluidized bed, it can be formed from the bottom to top by catalyst
Flowing bed.By with the contact of high temperature regeneration gas, catalyst surface adherency coke can react generate carbon dioxide and
Then regenerator is discharged in the gases such as vapor together with regeneration gas, thus remove the coke of catalyst surface adherency, restore to urge
The catalytic activity of agent.
It is noted that turbulent fluidized bed is as continuous stir reactor, the catalyst of most bottom grade downflow fluidized bed conveying
Once entering turbulent fluidized bed from feed inlet, is then uniformly mixed with its internal existing flowing bed, that is, flow urging in bed
Agent does not enter into the difference of priority.In addition, the feed inlet on the downside of turbulent fluidized bed side wall is arranged in the top of discharge port so that
Catalyst has that certain altitude is poor during flowing to discharge port from feed inlet, to ensure that it is enough that regeneration gas and catalyst have
Time of contact, fully to be regenerated to catalyst.
In regenerative process, partial catalyst may be blown to the middle and upper part of turbulent fluidized bed by regeneration gas, this part is urged
Agent will enter cyclone separator with regeneration gas, and after being detached by cyclone separator, catalyst passes through cyclone separator bottom
Dipleg drop back into the bottom of turbulent fluidized bed, regeneration gas is then expelled to turbulent fluidized bed from the riser on cyclone separator top
Top is discharged from the top of turbulent fluidized bed, thus avoids regeneration gas in flow process from the bottom to top, by partially catalyzed
Agent carries out turbulent fluidized bed, to ensure the internal circulating load of solid particle.
In addition, the temperature in downflow fluidized beds at different levels in the catalytic cracking/cracking system is adjustable, specifically
Ground can be adjusted in the heating mantle for corresponding to downflow fluidized bed outer wall into trip temperature so that catalytic cracking/cracking by being arranged
The temperature of reaction maintains within the scope of 550~650 DEG C, to ensure being normally carried out for catalytic cracking/cracking reaction.Ordinary circumstance
Under, the temperature of rudimentary downflow fluidized bed is higher, and the reaction temperature in advanced downflow fluidized bed is relatively low, this
So that with the progress of catalytic cracking/cracking reaction, gas mixture steps up, residing for downflow fluidized bed reactions at different levels
Temperature in device continuously decreases, and is thus conducive to the overreaction for avoiding gas mixture, improves high producing light olefins and aromatic hydrocarbons
The yield of equal intermediate products.For example, when catalytic cracking/cracking system includes three-level downflow fluidized bed, under level-one
Temperature in row bed fluidized-bed reactor is：450~550 DEG C, the temperature in two level down-flow fluidized bed using ECT fluidized-bed reactor is：500~
600 DEG C, most bottom grade downflow fluidized bed in temperature be：550~650 DEG C.
In conclusion multi-stage countercurrent catalytic cracking/cracking system provided in an embodiment of the present invention, in downflow fluidized bed reaction
On the basis of utensil has gas-solid to be uniformly distributed and inhibits gas-solid back-mixing property, multistage gas-solid contracurrent system is formed, it is each to increase
The average mass transfer force of grade downflow fluidized bed, and different reaction atmospheres can be provided at different levels, it is light to be conducive to high yield
Matter alkene and aromatic hydrocarbons are very suitable for catalytic cracking/cracking reaction of high severe degree (high oil and big finish ratio).
As shown in figure 4, in one embodiment of the invention, the catalytic cracking/cracking reaction system can further comprise：Fractionation
Tower 401；Wherein,
The gas vent and the fractionating column of the corresponding fast gas-solid separator of the level-one downflow fluidized bed
401 connections；
The corresponding fast gas-solid separator of the level-one downflow fluidized bed, for described after detaching
Gas mixture is conveyed to the fractionating column 401；
The fractionating column 401, for in the gas mixture gaseous component and liquid phase component detach, and point
The gaseous component after Shu Chu not detaching and the liquid phase component.
In the gas mixture that the corresponding fast gas-solid separator of level-one downflow fluidized bed is isolated, there is catalysis
The reaction intermediate of cracking/cracking, such as gasoline and kerosene etc., these reaction intermediates are the liquid phase in gas mixture
Component.In addition, there is also the gaseous components such as carbon monoxide and vapor in gas mixture.To catalytic cracking/pyrolysis product
When being utilized, the liquid phase components such as gasoline and kerosene are the higher product of added value, therefore level-one downflow fluidized bed pair
After the gas mixture that the fast gas-solid separator answered is isolated, need further to detach the gas mixture, with
By in gas mixture liquid phase component and gaseous component separate.As shown in figure 4, after gas mixture is fractionated into tower, it can
Isolate the components such as propylene, aromatic hydrocarbons, light diesel fuel and recycle oil and slurry oil.
Herein, the gas mixture is detached using fractionating column, fractionating column can receive external vapor decile
Gas is evaporated, when the fractionation gas received is contacted with gas mixture, the gaseous components such as carbon monoxide in gas mixture
It will diffuse into fractionation gas, fractionating column is discharged with fractionation gas in the gaseous component then spread, and liquid phase component is then from fractionation
Another outlet of tower is discharged, and to realize the separation of gas mixture gaseous component and liquid phase component, is conducive to gas mixture
Efficient utilization.
As shown in figure 5, in one embodiment of the invention, the fast gas-solid separator 102 may further include：Circle
Cyclic annular separator main body 1021 and gas eduction tube 1022；Wherein,
The opening upwards of the gas-solid mixing phase entrance are set to the one of 1021 outer wall of the circular separator main body
Side, Open Side Down for the solid material outlet, is set to the other side of 1021 outer wall of the circular separator main body；
One end of the gas eduction tube 1022 is arranged in the separator main body 1021, the gas eduction tube 1022
The other end be the gas vent；
The separator main body 1021 receives the gas mixture and the catalysis by the gas-solid mixing phase entrance
Agent, controls the gas mixture and the catalyst is rotated in circular annular space, and the catalyst is made to enter
The solid material outlet, the gas mixture enter the gas eduction tube 1022, complete the gas mixture and described urge
The separation of agent.
In order to reach good separating effect, the diameter D of circular separator main body and corresponding downflow fluidized bed reaction
The ratio D/Dr of the diameter Dr of device is 2.5~3.5.In addition, the cross section of gas-solid mixing phase entrance is rectangle, the long L1 of rectangle is
0.35~0.6D, wide W1 are 0.8~1.2Dr.It is mutually cut into circular ring shape separator main body the side of rectangle gas-solid mixing phase entrance
One vertical protective plate, the other side opposite with vertical protective plate are mutually cut with circular separator main body, and mutually the angle α at the place of cutting is
50 °~70 °.Gas eduction tube is one section and is co-axially mounted with circular separator main body, and is inserted into circular separator master
The opening straight tube in internal portion, open end are 0.1~0.35D with the baffle distance W3 of circular separator main body.In gas
Gu mixed phase entrance mutually cuts place with circular separator main body, inlet guide baffles are equipped with, are with the angle beta residing for vertical line
10 °~25 °.The end of flow apron is 0.07~0.25D with the distance between vertical protective plate W2.Gu expecting the cross section of outlet
Also it is rectangle, another vertical protective plate is mutually cut into one side with circular separator main body, and height H3 is 0.8~1.2D.Solid
Material outlet is equipped with arc cutting plate, radius D/2 with circular separator main body the tangent.Arc cutting plate divides with circular
The vertical range H2 of shell from device main body is 0.05~0.15D, the angle γ with the center vertical line of circular separator main body
For 5 and circular point.Gu the other both sides of material outlet are arc-shaped baffle, arc radius R1 and R2 are respectively 0.2~0.3D
With 0.4~0.6D.
After the gas-solid mixture that gas mixture and catalyst form leaves corresponding downflow fluidized bed, from
When the gas-solid mixing phase entrance of fast gas-solid separator enters fast gas-solid separator, since inlet guide baffles are to gas-solid
The guide functions of mixture so that for catalyst in gas-solid mixing phase inlet tool there are one the trend moved to side wall, gas-solid is mixed
It closes object to enter after circular separation main body, the annulus between the shell and gas eduction tube positioned at circular separator main body
It rotates in shape annular space.Due to the wall attachment effect of the difference and solid particle of gas mixture and catalyst inertia force,
Catalyst after the movement of 1/4 circular arc, is gathered in away from a close boundary layer of side wall in circular annular space.This
When cutting plate using solid particle side wall clustering phenomena realize catalyst and gas mixture efficient quick separating.By cutting
After cutting, gas continues to rotate in circular annular space from the top of cutting plate, after rotary motion in 1~3 week,
Corresponding upper level downflow fluidized bed is expelled to by gas eduction tube.And catalyst then falls to solid material outlet, passes through
Gu material outlet flows into corresponding next stage downflow fluidized bed.
In addition, in order to further increase separating effect, gas eduction tube is eccentrically mounted in circular separator main body, this
The gap before catalyst cutting can be reduced so that catalyst is further assembled to side wall, while increasing the gap after cutting, reduces
Gas mixture is when continuing to rotate to the entrainment of catalyst.
Measured through experiment, which has good separating effect, separation rate up to 97% or more,
And the residence time of catalyst in 100ms hereinafter, the residence time of gas mixture in 2s hereinafter, when can effectively avoid stop
Between it is long caused by excessively catalytic cracking/cracking reaction.
In one embodiment of the invention, the downflow fluidized bed includes：Reactor body, cylinder of turning back, gas into
Material mouth and feeding-in solid body mouth；Wherein,
The reactor body is straight barrel type；
The reactor body is turned back described in being set in cylinder, the feeding mouth of the reactor body and the cylinder company of turning back
It is logical；
The top of the cylinder of turning back be it is bullet-shaped orType；
When the top of the cylinder of turning back is bullet-shaped, the gas feed mouth and the feeding-in solid body mouth are respectively set
In a both sides of turning back；
When the top of the cylinder of turning back isWhen type, the gas feed mouth is arranged describedThe centre of type, the feeding-in solid body mouth are set to the side of the cylinder of turning back；
The gas of gas feed mouth fast gas-solid separator corresponding with next stage downflow fluidized bed goes out
Mouth connection；
The feeding-in solid body mouth the solid of fast gas-solid separator corresponding with upper level downflow fluidized bed expects
Mouth connection；
It is upward in the case where outside promotes wind action by the catalyst for cylinder of turning back described in feeding-in solid body mouth entrance
Movement, mixes with the gas mixture entered by the gas feed mouth at the top of the cylinder of turning back, mixed
The catalyst and the gas mixture are entered by the feeding mouth of the reactor body in the reactor body, in institute
It states and carries out catalytic cracking/cracking reaction in reactor body.
When overhead of turning back is bullet-shaped, shown in structural schematic diagram such as Fig. 6 (a) of downflow fluidized bed, when
Overhead of turning back isWhen type, the structural schematic diagram of downflow fluidized bed is as shown in Figure 7.In practical application
When, generally air-separating plant can be used to provide loosening gas for this system, such as provide nitrogen as loosening gas.This strand of nitrogen
Be blown into from downflow fluidized bed bottom, i.e., nitrogen the flow direction of downflow fluidized bed be from bottom to top, then this
Stock nitrogen can be used as the promotion wind in downflow fluidized bed.When being bullet-shaped at the top of cylinder of turning back, catalyst and oil gas
Mixture enters cylinder of turning back after catalyst enters cylinder of turning back from the both sides for cylinder of turning back respectively and is moved upwards under the action of nitrogen,
Meanwhile gas mixture is due to gas characteristic, also to a top movements of turning back so that gas mixture and catalyst are in sub warhead
Mixing at the top of the cylinder of turning back of type.It is at the top of cylinder of turning backWhen type, catalyst is also upward in the case where promoting wind action
Movement can be mixed with from the gas mixture that a top enters of turning back.Then, mixed catalyst and gas mixture are another
And enter reactor body, catalytic cracking/cracking reaction occurs when being carried out along gravitational motion inside reactor body.As a result,
By the cooperation of turn back cylinder and reactor body, ensure that gas-solid uniformly enters reactor body, is conducive to improve reaction uniformly
Property.
It is noted that the feeding mouth of reactor body and turn back the distance between cylinder top and a bottom straight tube of turning back
Diameter ratio be 0.5~3, for turning back and be bullet-shaped at the top of cylinder, as shown in Fig. 6 (b), m:N=0.5~3:1.It can be with
Understand, is at the top of cylinder of turning backWhen type, the feeding mouth of reactor body and between turning back at the top of cylinder away from
It is still 0.5~3 from the diameter ratio with cylinder of turning back.
In addition, central axes institute of the gas feed mouth (generally atomizer) of downflow fluidized bed with reactor body
At angle be 0~90~, i.e., gas feed mouth is arranged at the top or side of downflow fluidized bed, and downstream
The feeding-in solid body mouth of fluidized bed reactor is generally located on the side of downflow fluidized bed.
It is understood that most bottom grade downflow fluidized bed may be alternatively provided as reactor body and turn back what cylinder was combined
Form ensures that oil gas raw material and catalyst uniformly enter reactor body in order to the mixing of oil gas raw material and catalyst.
As shown in figure 8, an embodiment of the present invention provides a kind of catalytic cracking/cracking provided using any of the above-described embodiment
The method that system carries out catalytic cracking/cracking, this method may comprise steps of：
Step 801：Receive oil gas raw material and catalyst using most bottom grade downflow fluidized bed, carry out catalytic cracking/
Cracking reaction forms gas mixture, and the catalyst and the gas mixture is conveyed to corresponding gas-solid and quickly divided
From device；
Step 802：It is received using every level-one downflow fluidized bed in addition to the grade downflow fluidized bed of most bottom
The gas mixture and catalyst, carry out catalytic cracking/cracking reaction, and by after reaction gas mixture and catalyst it is defeated
Give the corresponding fast gas-solid separator；
Step 803：The gas mixture and catalyst that receive are carried out using each fast gas-solid separator
It detaches, and the gas mixture is delivered to the charging of upper level downflow fluidized bed by the gas vent of itself
Mouthful, it is exported the catalyst transport to the feed inlet of next stage downflow fluidized bed by the solid material of itself.
In one embodiment of the invention, this method may further include：
Using the most bottom corresponding fast gas-solid separator of grade downflow fluidized bed by the catalyst transport
To stripper；
The gas mixture in the catalyst is stripped using the stripper, and by the catalysis after stripping
Agent is conveyed to the regenerator；
The catalyst is regenerated using the regenerator；
Catalyst transport after being regenerated regenerator using conveying hoisting pipe gives level-one downflow fluidized bed.
In one embodiment of the invention, this method may further include：
Using the corresponding fast gas-solid separator of level-one downflow fluidized bed by the air-fuel mixture after separation
Object is conveyed to fractionating column；
Using the fractionating column in the gas mixture gaseous component and liquid phase component detach, and respectively it is defeated
Go out the gaseous component after separation and the liquid phase component.
In one embodiment of the invention, the specific implementation mode of step 803 may include：
The gas mixture and the catalysis are received using the gas-solid mixing phase entrance of the fast gas-solid separator
Agent；
The gas mixture is controlled using the separator main body of the fast gas-solid separator and the catalyst exists
It is rotated in circular annular space, so that the catalyst enters the solid material outlet, the gas mixture enters institute
The gas eduction tube for stating fast gas-solid separator completes the separation of the gas mixture and the catalyst.
In one embodiment of the invention, the catalyst includes：The molecular sieve that grain size is 75 μm~750 μm, the molecule
Sieve includes：The auxiliary agent based on host agent and ZSM-5 based on Y type molecular sieve；The mass ratio of the host agent and the auxiliary agent
For：1:1~10:1.Since the molecular sieve of appropriate particle size has super large specific surface so that molecular sieve and gas mixture or
The transmission motive force of oil gas raw material greatly enhances, to ensure the quick progress of reaction.
Below by several specific embodiments to being carried out using catalytic cracking provided in an embodiment of the present invention/cracking system
The method of catalytic cracking/cracking reaction is described in detail.
Embodiment 1：Catalytic cracking/cracking reaction is carried out using multi-stage countercurrent catalytic cracking shown in Fig. 9/cracking system,
Detailed process is as follows：
In the present embodiment 1, multi-stage countercurrent catalytic cracking/cracking system has grade (two level) the downflow fluidized bed reaction of most bottom
Device 901 and its corresponding most bottom grade (two level) fast gas-solid separator 902, also level-one downflow fluidized bed 903
And its corresponding level-one fast gas-solid separator 904.
In initial reaction stage, level-one downflow fluidized bed 903 receives catalyst, and catalyst is quickly divided by level-one gas-solid
Solid material outlet from device 904 is delivered to the feed inlet of two level downflow fluidized bed 901.Then catalyst and two level downlink
The oil gas raw material contact that fluidized-bed reactor 901 receives, carries out catalytic cracking/cracking reaction, generates gas mixture.
Then, the gas mixture with catalyst of generation are mixed by the gas-solid of two level fast gas-solid separator 902
Entrance enters two level fast gas-solid separator 902, and after the separation of two level fast gas-solid separator 902, gas mixture is logical
It crosses gas vent and is promoted to level-one downflow fluidized bed 903, and catalyst is then exported by solid material and is discharged.
It is then received into the gas mixture in level-one downflow fluidized bed 903 with level-one downflow fluidized bed
Catalyst carry out further catalytic cracking/cracking reaction, it is fast that the gas mixture after reaction with catalyst enters level-one gas-solid
Fast separator 904, after level-one fast gas-solid separator 904 detaches gas mixture and catalyst, air-fuel mixture
Object is discharged by gas vent, and catalyst then enters two level downflow fluidized bed 901 by the outlet of solid material, is catalyzed under two level
The oil gas raw material that row fluidized-bed reactor 901 receives carries out catalytic cracking/cracking reaction.
Embodiment 2：It is anti-that catalytic cracking/cracking is carried out using multi-stage countercurrent catalytic cracking as shown in Figure 10/cracking system
It answers, detailed process is as follows：
In the present embodiment 2, catalytic cracking/cracking system have most bottom grade (two level) downflow fluidized bed 901 with
And its corresponding most bottom grade (two level) fast gas-solid separator 902, also level-one downflow fluidized bed 903 and its is right
Level-one fast gas-solid separator 904 and regenerator 1001, conveying hoisting pipe 1002 and the stripper 1003 answered.
The reaction process of the catalytic cracking/cracking is similar to the reaction process in embodiment 1, the difference is that：It is following
In ring reaction process, two level fast gas-solid separator 902 is by the catalyst transport isolated to stripper 1003, stripper
After 1003 pairs of gas mixtures for being adsorbed on catalyst surface strip, by the catalyst transport after stripping to regenerator
1001, after regenerator regenerates catalyst existing for inside, the catalyst after regeneration is carried by conveying hoisting pipe 1002
Level-one downflow fluidized bed 903 is risen to, realizes recycling for catalyst so that level-one downflow fluidized bed 903
Without constantly receiving externally input catalyst.
Embodiment 3：Catalytic cracking/cracking reaction, tool are carried out using multistage catalytic cracking as shown in figure 11/cracking system
Body process is as follows：
In the present embodiment 3, catalytic cracking/cracking system have most bottom grade (three-level) downflow fluidized bed 1101 with
And its corresponding most bottom grade (three-level) fast gas-solid separator 1102, two level downflow fluidized bed 1103 and its correspondence
Two level fast gas-solid separator 1104, also level-one downflow fluidized bed 1105 and its corresponding level-one gas-solid be fast
Fast separator 1106 and regenerator 1107, conveying hoisting pipe 1108, stripper 1109 and fractionating column 1110.
In a cycle period：
Regenerator 1107 receives catalyst, and it is downflow fluidized bed by conveying hoisting pipe 1108 catalyst to be promoted to level-one
Reactor 1105, level-one downflow fluidized bed 1105 will be catalyzed by its corresponding level-one fast gas-solid separator 1106
Agent is delivered to two level downflow fluidized bed 1103, and two level downflow fluidized bed 1103 passes through its corresponding two level gas-solid
Fast separation device 1104 will be in catalyst transport to three-level downflow fluidized bed 1101.
Three-level downflow fluidized bed 1101 receives externally input oil gas raw material, and oil gas raw material exists existing for inside
Catalytic cracking/cracking reaction is carried out under the catalytic action of catalyst, generates gas mixture, and gas mixture and inside are deposited
Partial catalyst be conveyed to corresponding three-level fast gas-solid separator 1102, three-level fast gas-solid separator 1102 is right
Gas mixture and catalyst are detached, and by the catalyst transport after separation to stripper 1109, stripper 1109 is to inhaling
Be attached to catalyst surface gas mixture stripped after, by the catalyst transport after stripping to regenerator 1107, three-level gas
The gas mixture isolated is conveyed to two level downflow fluidized bed 1103 by solid fast separating device 1102 simultaneously.
After gas mixture carries out further catalytic cracking/cracking reaction in two level downflow fluidized bed 1103,
It is detached with catalyst by its 1103 corresponding two level fast gas-solid separator 1104 of two level downflow fluidized bed
Afterwards, it then is delivered in level-one downflow fluidized bed 1105.Meanwhile regenerator 1107 is to three-level fast gas-solid separator
After the catalyst of 1102 conveyings is regenerated, the catalyst after regeneration is promoted to level-one downstream using conveying hoisting pipe 1108
Fluidized bed reactor 1105.
Catalyst in level-one downflow fluidized bed 1105 is contacted with gas mixture so that gas mixture
Further catalytic cracking/cracking reaction is carried out, the gas mixture and catalyst after reaction enter level-one gas-solid quick separating dress
1106 are set, the gas mixture isolated is delivered to fractionating column 1110 by level-one fast gas-solid separator 1106, while will be divided
The catalyst transport separated out is to two level downflow fluidized bed 1103.Fractionating column 1110 is to the gaseous component in gas mixture
It is detached with liquid phase component, and the gaseous component and liquid phase component after output separation respectively.
As can be seen from the above-described embodiment, oil gas raw material is entered by most bottom grade downflow fluidized bed, is carried out catalysis and is split
Gas mixture is generated after change/cracking reaction, then gas mixture carries out further by two level downflow fluidized bed
Catalytic cracking/cracking reaction ... in level-one (superlative degree) downflow fluidized bed until react, and by level-one downstream
Fluidized bed reactor exports.Catalyst is entered by level-one downflow fluidized bed, by secondary advanced downflow fluidized bed reaction
Device ... is until enter most bottom grade downflow fluidized bed, and be conveyed to regenerator again by most bottom grade downflow fluidized bed
Raw, the catalyst after regeneration is transported to level-one (superlative degree) downflow fluidized bed again.In the process, gas mixture
Realize that counter current contacting, mass-and heat-transfer motive force bigger are conducive to the quick progress of catalytic cracking/cracking reaction with catalyst.
Also, it is both provided with corresponding fast gas-solid separator per the discharge port of level-one downflow fluidized bed, often
One fast gas-solid separator can carry out quick separating to gas mixture and catalyst, to effectively avoid excessive catalysis
Cracking/cracking reaction effectively avoids the reaction time of gas mixture long.
Embodiment 4
The feedstock oil that 60% wax oil and 40% residual oil are formed is used as oil gas raw material, catalyst include 75% molecular sieve and
25%ZSM-5, by multi-stage countercurrent catalytic cracking that oil gas raw material and any of the above-described embodiment of the catalyst input present invention provide/split
In addition same oil gas raw material is carried out catalytic cracking/cracking reaction, the reaction condition of two systems by solution system in riser
It is as shown in table 1 with reaction product, wherein A1 and A2 characterizes multi-stage countercurrent catalytic cracking/cracking system provided in an embodiment of the present invention
Reaction in system, B characterize the reaction in riser.From table 1 it follows that multi-stage countercurrent catalysis provided in an embodiment of the present invention
The high producing light olefins of cracking/cracking system and aromatic hydrocarbons.
Table 1
To sum up, each embodiment of the present invention at least has the following effects that：
1, in embodiments of the present invention, at least two-stage downflow fluidized bed being distributed using stairstepping is carried out catalysis and split
Change/cracking reaction, since downflow fluidized bed has the property of similar laminar flow, in downflow fluidized beds at different levels
Oil gas raw material or gas mixture and catalyst move to bottom end in reaction from the feed inlet on downflow fluidized bed top
Discharge port, which is along gravitational motion process, to not easily cause the gas of gas mixture or oil gas raw material and catalyst
Gu back-mixing so that the distribution of catalyst reactor is more uniform, is conducive to effectively control the stop of catalyst in the reactor
Time, to be conducive to improve the selectivity of reaction.
2, in embodiments of the present invention, it is correspondingly arranged on fast gas-solid separator per level-one downflow fluidized bed,
Per level-one downflow fluidized bed after catalytic cracking/cracking reaction, by after reaction gas mixture and catalyst it is defeated
Give corresponding fast gas-solid separator.Fast gas-solid separator can quickly divide gas mixture and catalyst
From, to effectively avoid excessive catalytic cracking/cracking reaction, i.e., effectively avoid the reaction time of gas mixture long, from
And be conducive to improve the yield of catalytic cracking/cracking reaction intermediate product.
3, in embodiments of the present invention, per the solid material of the corresponding fast gas-solid separator of level-one downflow fluidized bed
It exports and is connected to the feed inlet of corresponding next stage downflow fluidized bed, and the gas of each fast gas-solid separator
Body is exported to be connected to the feed inlet of corresponding upper level downflow fluidized bed.This makes gas mixture by level-one downstream
Fluidized bed reactor is conveyed to corresponding upper level downflow fluidized bed step by step, while catalyst is by highest downflow fluidized bed
Reactor is conveyed to corresponding next stage downflow fluidized bed step by step so that gas mixture and catalyst carry out adverse current and connect
It touches, is conducive to enhance the mass-and heat-transfer motive force between gas mixture and catalyst, and the enhancing of mass transfer force can guarantee
The quick progress of catalytic cracking/cracking reaction, meanwhile, the enhancing of driving force of heat transfer can guarantee the temperature in downflow fluidized bed
Degree is uniform, is also beneficial to the quick progress of reaction, avoids the reaction time long, to be further conducive to improve catalytic cracking/
The yield of cracking reaction intermediate product.
4, in embodiments of the present invention, the corresponding fast gas-solid separator of most bottom grade downflow fluidized bed will detach
The catalyst transport gone out is to regenerator, after regenerator regenerates catalyst, using conveying hoisting pipe by the catalysis after regeneration
Agent is delivered to highest downflow fluidized bed, thus not only maintains the catalytic activity of catalyst, also achieves catalyst
Recycle.Also, the catalyst transport after regenerating gives level-one downflow fluidized bed so that most fresh catalyst with
The gas mixture of reaction final stage is in contact, and is conducive to the depth for enhancing catalytic cracking/cracking reaction.
5, in embodiments of the present invention, the corresponding fast gas-solid separator of level-one downflow fluidized bed will be isolated
Gas mixture be conveyed to fractionating column, fractionating column by gas mixture gaseous component and liquid phase component detach, and
Gaseous component and liquid phase component after output separation respectively, is convenient for the follow-up use of light component and heavy constituent, to be conducive to oil
The efficient utilization of gas mixture.
6, in embodiments of the present invention, it is provided with reactor body in downflow fluidized bed and cylinder of turning back, enters
The catalyst of cylinder of turning back is moved upwards in the case where promoting wind action, is mixed at the top of cylinder of turning back with gas mixture, mixed
Catalyst and gas mixture enter reactor body together, thereby guarantee that gas-solid uniformly enters reactor body, are conducive to
Improve reaction uniformity.
7, in embodiments of the present invention, in downflow fluidized bed there is gas-solid to be uniformly distributed and inhibit gas-solid back-mixing
On the basis of matter, multistage gas-solid contracurrent system is formed, to increase the average mass transfer force of downflow fluidized beds at different levels,
And different reaction atmospheres can be provided at different levels, be conducive to high producing light olefins and aromatic hydrocarbons, it is (high oily and big to be very suitable for high severe degree
Finish ratio) catalytic cracking/cracking reaction.
It should be noted that herein, such as first and second etc relational terms are used merely to an entity
Or operation is distinguished with another entity or operation, is existed without necessarily requiring or implying between these entities or operation
Any actual relationship or order.Moreover, the terms "include", "comprise" or its any other variant be intended to it is non-
It is exclusive to include, so that the process, method, article or equipment including a series of elements includes not only those elements,
But also include other elements that are not explicitly listed, or further include solid by this process, method, article or equipment
Some elements.In the absence of more restrictions, the element limited by sentence " including one ", is not arranged
Except there is also other identical factors in the process, method, article or apparatus that includes the element.
Finally, it should be noted that：The foregoing is merely presently preferred embodiments of the present invention, is merely to illustrate the skill of the present invention
Art scheme, is not intended to limit the scope of the present invention.Any modification for being made all within the spirits and principles of the present invention,
Equivalent replacement, improvement etc., are included within the scope of protection of the present invention.
Claims (10)
1. a kind of multi-stage countercurrent catalytic cracking/cracking system, which is characterized in that including：At least two-stage downlink being distributed in ladder
Fluidized-bed reactor and at least two fast gas-solid separators；Wherein,
The downflow fluidized bed and the fast gas-solid separator correspond, downflow fluidized bed anti-described in every level-one
The discharge port of device is answered to be connected to the gas-solid mixing phase entrance of the corresponding fast gas-solid separator；
Gas vent per the corresponding fast gas-solid separator of downflow fluidized bed described in level-one with it is corresponding on
The feed inlet of level-one downflow fluidized bed is connected to；
Solid material outlet per the corresponding fast gas-solid separator of downflow fluidized bed described in level-one with it is corresponding under
The feed inlet of level-one downflow fluidized bed is connected to；
Most bottom grade downflow fluidized bed carries out catalytic cracking/cracking reaction, shape for receiving oil gas raw material and catalyst
Olefiant gas mixture, and the catalyst and the gas mixture are conveyed to the corresponding fast gas-solid separator；
In addition to the grade downflow fluidized bed of the most bottom, downflow fluidized bed described in every level-one, for receiving oil gas
Mixture and catalyst, carry out catalytic cracking/cracking reaction, and by after reaction gas mixture and catalyst transport to correspond to
The fast gas-solid separator；
Each described fast gas-solid separator, for receiving gas mixture and catalyst detach, and lead to
It crosses the gas vent of itself and conveys the gas mixture, the catalyst is conveyed by the solid material outlet of itself.
2. multi-stage countercurrent catalytic cracking/cracking system according to claim 1, which is characterized in that
Further comprise：Stripper, regenerator and conveying hoisting pipe；Wherein,
The quick gas-solid corresponding with most bottom grade downflow fluidized bed of the catalyst granules entrance of the stripper is quick
The solid material outlet of separator；
The solid material outlet of the particle entrance of the regenerator and the stripper；
One end of the conveying hoisting pipe is connect with the feed inlet of level-one downflow fluidized bed, the other end and the regenerator
Particle outlet connection；
The corresponding fast gas-solid separator of most bottom grade downflow fluidized bed, the catalyst for will isolate
It is conveyed to the stripper；
The stripper, for being stripped to the gas mixture in the catalyst, and being exported by the solid material of itself will
The catalyst transport after stripping gives the regenerator；
The regenerator, for being regenerated to the catalyst；
The conveying hoisting pipe, for the catalyst transport after regenerating the regenerator to the downflow fluidized bed reaction of the level-one
Device.
3. multi-stage countercurrent catalytic cracking/cracking system according to claim 1 or 2, which is characterized in that
Further comprise：Fractionating column；Wherein,
The gas vent of the corresponding fast gas-solid separator of the level-one downflow fluidized bed is connected to the fractionating column；
The corresponding fast gas-solid separator of the level-one downflow fluidized bed, for the oil gas after detaching
Mixture is conveyed to the fractionating column；
The fractionating column, for in the gas mixture gaseous component and liquid phase component detach, and export respectively
The gas phase component after separation and the liquid phase component.
4. multi-stage countercurrent catalytic cracking/cracking system according to claim 1, which is characterized in that
The downflow fluidized bed includes：Reactor body, cylinder of turning back, gas feed mouth and feeding-in solid body mouth；Wherein,
The reactor body is straight barrel type；
The reactor body is turned back described in being set in cylinder, and the feeding mouth of the reactor body is connected to the cylinder of turning back；
The top of the cylinder of turning back be it is bullet-shaped orType；
When the top of the cylinder of turning back is bullet-shaped, the gas feed mouth and the feeding-in solid body mouth are respectively arranged at institute
State a both sides of turning back；
When the top of the cylinder of turning back isWhen type, the gas feed mouth is arranged describedType
Centre, the feeding-in solid body mouth are set to the side of the cylinder of turning back；
The gas vent of gas feed mouth fast gas-solid separator corresponding with next stage downflow fluidized bed connects
It is logical；
The solid material outlet of feeding-in solid body mouth fast gas-solid separator corresponding with upper level downflow fluidized bed connects
It is logical；
It is moved upwards by the catalyst for cylinder of turning back described in feeding-in solid body mouth entrance in the case where outside promotes wind action,
It is mixed at the top of the cylinder of turning back with the gas mixture entered by the gas feed mouth, it is mixed described to urge
Agent and the gas mixture are entered by the feeding mouth of the reactor body in the reactor body, in the reaction
Catalytic cracking/cracking reaction is carried out in device main body；
And/or
The fast gas-solid separator includes：Circular separator main body and gas eduction tube；Wherein,
The opening upwards of the gas-solid mixing phase entrance are set to the side of the circular separator main body outer wall, described solid
Open Side Down for material outlet, is set to the other side of the circular separator main body outer wall；
One end of the gas eduction tube is arranged in the separator main body, and the other end of the gas eduction tube is the gas
Body exports；
The separator main body receives the gas mixture and the catalyst, control by the gas-solid mixing phase entrance
The gas mixture and the catalyst are rotated in circular annular space, and the catalyst is made to enter the solid material
Outlet, the gas mixture enter the gas eduction tube, complete the separation of the gas mixture and the catalyst.
5. a kind of split using any multi-stage countercurrent catalytic cracking/cracking system carries out catalytic cracking/of Claims 1-4 4
The method of solution, which is characterized in that including：
Oil gas raw material and catalyst are received using most bottom grade downflow fluidized bed, catalytic cracking/cracking reaction is carried out, is formed
Gas mixture, and the catalyst and the gas mixture are conveyed to corresponding fast gas-solid separator；
The air-fuel mixture is received using every level-one downflow fluidized bed in addition to the grade downflow fluidized bed of most bottom
Object and catalyst, carry out catalytic cracking/cracking reaction, and by after reaction gas mixture and catalyst transport give corresponding institute
State fast gas-solid separator；
The gas mixture and catalyst that receive are detached using each fast gas-solid separator, and by certainly
The gas mixture is delivered to the feed inlet of upper level downflow fluidized bed by the gas vent of body, passes through consolidating for itself
Material is exported the catalyst transport to the feed inlet of next stage downflow fluidized bed.
6. according to the method described in claim 5, it is characterized in that,
Further comprise：
Using the corresponding fast gas-solid separator of most bottom grade downflow fluidized bed by the catalyst transport to vapour
Carry device；
The gas mixture in the catalyst is stripped using the stripper, and the catalyst after stripping is defeated
Give the regenerator；
The catalyst is regenerated using the regenerator；
Catalyst transport after being regenerated regenerator using conveying hoisting pipe gives level-one downflow fluidized bed.
7. according to the method described in claim 5, it is characterized in that,
Further comprise：
It is using level-one downflow fluidized bed corresponding fast gas-solid separator that the gas mixture after separation is defeated
Give fractionating column；
Using the fractionating column in the gas mixture gaseous component and liquid phase component detach, and respectively output point
The gaseous component from after and the liquid phase component.
8. according to the method described in claim 5, it is characterized in that,
It is described that the gas mixture and catalyst that receive are detached using each fast gas-solid separator, packet
It includes：
The gas mixture and the catalyst are received using the gas-solid mixing phase entrance of the fast gas-solid separator；
The gas mixture and the catalyst are controlled in annulus using the separator main body of the fast gas-solid separator
It is rotated in shape annular space, so that the catalyst enters the solid material outlet, the gas mixture enters the gas
The gas eduction tube of solid fast separating device completes the separation of the gas mixture and the catalyst.
9. according to the method described in claim 5, it is characterized in that,
The catalyst includes：The molecular sieve that grain size is 25 μm~750 μm；
And/or
The temperature of the catalytic cracking/cracking reaction is：550~650 DEG C.
10. according to the method described in claim 9, it is characterized in that,
When the catalytic cracking/cracking system includes three-level downflow fluidized bed,
Temperature in level-one down-flow fluidized bed using ECT fluidized-bed reactor is：450~550 DEG C；
Temperature in two level down-flow fluidized bed using ECT fluidized-bed reactor is：500~600 DEG C；
Most bottom grade downflow fluidized bed in temperature be：550~650 DEG C；
And/or
The molecular sieve includes：The auxiliary agent based on host agent and ZSM-5 based on Y type molecular sieve；The host agent with it is described
The mass ratio of auxiliary agent is：1:1~10:1.
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