CN207016721U - Catalytic cracking unit and petroleum refining equipment - Google Patents
Catalytic cracking unit and petroleum refining equipment Download PDFInfo
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- CN207016721U CN207016721U CN201720089059.1U CN201720089059U CN207016721U CN 207016721 U CN207016721 U CN 207016721U CN 201720089059 U CN201720089059 U CN 201720089059U CN 207016721 U CN207016721 U CN 207016721U
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- Prior art keywords
- regenerator
- catalyst
- catalytic cracking
- riser reactor
- cracking unit
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- 238000004523 catalytic cracking Methods 0.000 title claims abstract description 33
- 238000005504 petroleum refining Methods 0.000 title claims abstract description 9
- 239000003054 catalyst Substances 0.000 claims abstract description 82
- 238000011069 regeneration method Methods 0.000 claims abstract description 19
- 230000008929 regeneration Effects 0.000 claims abstract description 15
- 239000002994 raw material Substances 0.000 claims description 13
- 230000000694 effects Effects 0.000 abstract description 14
- 239000000571 coke Substances 0.000 abstract description 11
- 238000006555 catalytic reaction Methods 0.000 abstract description 10
- 239000003502 gasoline Substances 0.000 abstract description 9
- 238000005516 engineering process Methods 0.000 abstract description 6
- 230000009467 reduction Effects 0.000 abstract description 3
- 230000004044 response Effects 0.000 abstract description 3
- 239000003921 oil Substances 0.000 description 34
- 239000007789 gas Substances 0.000 description 16
- 238000000034 method Methods 0.000 description 16
- 238000006243 chemical reaction Methods 0.000 description 15
- 239000003795 chemical substances by application Substances 0.000 description 14
- 239000002245 particle Substances 0.000 description 8
- 238000005336 cracking Methods 0.000 description 7
- 238000009826 distribution Methods 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 238000011084 recovery Methods 0.000 description 5
- 238000013461 design Methods 0.000 description 4
- QQONPFPTGQHPMA-UHFFFAOYSA-N Propene Chemical compound CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 230000001172 regenerating effect Effects 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 239000002283 diesel fuel Substances 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 241000772415 Neovison vison Species 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000007809 chemical reaction catalyst Substances 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000003079 shale oil Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Catalytic cracking technology field is the utility model is related to, more particularly, to a kind of catalytic cracking unit and petroleum refining equipment, and in particular to a kind of catalytic cracking unit for optimizing reaction-regeneration system.The catalytic cracking unit includes：Riser reactor, settler, regenerator and catalyst heat exchange device；The top of riser reactor connects with settler, and bottom connects with catalyst heat exchange device；The stripping section of settler is connected by regeneration standpipe with regenerator；Regenerator is connected by standpipe, the first airduct with catalyst heat exchange device respectively；Catalyst heat exchange device and regenerator are respectively connected with the second airduct of the main wind of supply system.Compared with prior art, the utility model can take into account catalyst activity and temperature plateau controls two aspects, therefore can realize following purpose：Oil ratio is improved, thermal response is reduced, catalytic reaction increases, coke and dry gas yied reduction, gasoline yield increase, and the device can realize commercial Application completely.
Description
Technical field
Catalytic cracking technology field is the utility model is related to, more particularly, to a kind of catalytic cracking unit and petroleum refining
A kind of equipment, and in particular to catalytic cracking unit for optimizing reaction-regeneration system.
Background technology
Catalytic cracking unit is one of secondary operation device important in oil refining process, and its workflow is in heat and catalysis
Make mink cell focus that cracking reaction occur in the presence of agent, be changed into the process of cracked gas, gasoline and diesel oil etc.；Generated in course of reaction
Coke laydown on catalyst, catalyst is lost activity, catalyst can be regenerated by being blown into air burning-off coke, and circulation makes
With.The regenerated catalyst of heat can provide reaction institute calorific requirement.In above-mentioned technique, pursuit be high value fuel product receipts
Rate and quality, while the yield of accessory substance dry gas and coke is reduced, improve heat recovery rate.And this target is realized, often lead to
Cross the change of heat recovery mode after catalyst regenerates.In recent years, each research institution conducts in-depth research to this both at home and abroad,
The technology of exploitation mainly has following items：
IsoCat techniques disclosed in US 6059958, it is characterized in the catalyst cooled down through external warmer being divided into two strands,
One returns to regenerator bed, and another stock enters riser and reacted with feedstock oil after being mixed with the regenerated catalyst of heat.Obviously, mix
Close temperature of the temperature less than conventional regenerated catalyst of regenerated catalyst.IsoCat techniques can reduce coke and dry gas production
Rate, and two strands of catalyst of IsoCat techniques are regenerated catalyst, and the activity of intermixture is higher, is more beneficial for catalytic reaction.
But the temperature of technique lifting bottom of the tube mixed catalyst is more difficult to get steady control.
" X designs " disclosed in US 5451313, Uop Inc.'s this new design in nineteen ninety-five utility model, the purpose is to
Oil ratio is improved, improves product distribution.It is characterized in being provided with a catalyst blender between reactor and regenerator, it is to be generated
Agent mixes with regenerative agent in blender, and part intermixture flows into riser and raw material haptoreaction, and remaining intermixture flows into
Regenerator is regenerated.The benefit of this structure is that the temperature of intermixture into riser is lower than what regenerator came, makes catalyst
Internal circulating load increase, oil ratio improve, so thermal response reduction, catalytic reaction increase, coke and dry gas yied reduce, gasoline yield
Increase.But the design shortcoming is exactly that the spent agent activity in mixed catalyst is very low, causes the active relatively low of intermixture, is unfavorable for
The cracking of feedstock oil.
Regenerator sloped tube catalyst cooling technology disclosed in CN 1288933, this method are exactly directly in regenerator sloped tube peripheral hardware
A cooling water jecket is put, the regenerated catalyst temperature for entering riser reactor is lowered by cooling water.It is although this
Method has obtained good effect on pilot-plant, is remarkably decreased dry gas and coke yield, but given in industrial practice
The control of reaction temperature brings very big difficulty, that is to say, that this method seems simple, and it is larger to put into practice difficulty.
A kind of catalyst cracking method and device disclosed in CN 1710029, this method, which uses double lifting leg and sets up gasoline, sinks
Device and secondary fractionating column are dropped, while relative temperature relatively low gasoline rising pipe reclaimable catalyst in part is introduced into raw material oil riser and urged
Agent pre-lift blender, feedstock oil riser is entered after being mixed with high temperature regeneration agent, had so both reduced raw material oil riser
Finish Contact Temperature, take full advantage of the residual activity of gasoline rising pipe reclaimable catalyst again, improve raw material oil riser and urge
Change the oil ratio and product selectivity of cracking, reduce dry gas and coke yield, improve propene yield and Propylene Selectivity.The technique
Although being disadvantageous in that gasoline spent agent residual activity is higher, still there is certain difference compared with regenerated catalyst activity
Away from.
Catalytic cracking unit disclosed in above-mentioned patent can not take into account at following 2 points：One, guarantee is recycled into riser
The all regenerated catalysts of catalyst, without reclaimable catalyst, to ensure the activity of reaction catalyst used；Two, recovery
The temperature of mixed catalyst is steadily controlled after heat.
Utility model content
The purpose of this utility model is to provide a kind of catalytic cracking unit, urged with solving mixing present in prior art
Agent activity is low, can not steadily control the technical problems such as the temperature of catalyst.
In order to solve the above technical problems, in a first aspect, catalytic cracking unit provided by the utility model, it includes：Lifting
Pipe reactor, settler, regenerator and catalyst heat exchange device；The top of the riser reactor connects with the settler,
The bottom of the riser reactor connects with the catalyst heat exchange device；The stripping section of the settler by regeneration standpipe with
The regenerator connection；The regenerator is connected by standpipe, the first airduct with the catalyst heat exchange device respectively；It is described
Catalyst heat exchange device and the regenerator are respectively connected with the second airduct of the main wind of supply system.
Further, described catalytic cracking unit also includes external warmer, and the external warmer connects with the regenerator
It is logical.
Further, the external warmer is connected by the Ith inclined tube, the IIth inclined tube with the regenerator respectively.
Further, the catalyst heat exchange device is connected by the bottom of the first regenerator sloped tube and the riser reactor
It is logical.
Further, the regenerator is connected by the second regenerator sloped tube with the middle part of the riser reactor.
Further, second regenerator sloped tube by multiple branch pipes respectively with connecting in the middle part of the riser reactor
Connect, and the multiple branch pipe is distributed in the different height of the riser reactor.
Further, positioned at the branch pipe of the riser reactor bottom and being connected for the riser reactor
Position is located at 0.5-10m above the raw material oil inlet of the riser reactor.
Further, the connected position interval 4-10m of the two neighboring branch pipe and the riser reactor.
Further, it is equipped with valve on the branch pipe, first regenerator sloped tube and second regenerator sloped tube.
In order to solve the above technical problems, second aspect, the utility model also provides a kind of petroleum refining equipment, and it includes institute
The catalytic cracking unit stated.
Using above-mentioned technical proposal, empirical tests, for same raw material, and same catalyst is used, split with Conventional catalytic
Makeup, which is put, to be compared, and the utility model can at least realize following beneficial effect：
(1) device dry gas and coke gross production rate decline 0.5-1.5 percentage points, and liquefied gas, gasoline and the total liquid of diesel oil are received
Rate improves more than 1.0 percentage points.
(2) riser reactor oil ratio can be improved to more than 10.
(3) gasoline olefin volume content can reduce 5-15 percentage points.
(4) it is catalyzed SO in flue gasxContent reduces by more than 30%.
Brief description of the drawings
, below will be right in order to illustrate more clearly of the utility model embodiment or technical scheme of the prior art
The required accompanying drawing used is briefly described in embodiment or description of the prior art, it should be apparent that, describe below
In accompanying drawing be some embodiments of the present utility model, for those of ordinary skill in the art, do not paying creativeness
On the premise of work, other accompanying drawings can also be obtained according to these accompanying drawings.
Fig. 1 is the structural representation for the catalytic cracking unit that the utility model embodiment one provides；
Fig. 2 is the structural representation for the catalytic cracking unit that the utility model embodiment two provides；
Fig. 3 is the first structural representation of the catalytic cracking unit of the utility model embodiment three；
Fig. 4 is second of structural representation of the catalytic cracking unit of the utility model embodiment three.
Reference：
1-reaction oil gas outlet；2-settler；3-riser reactor；4-regenerator；5-branch pipe；6- second
Regenerator sloped tube；7-raw material oil inlet；8-the first regenerator sloped tube；9-the second airduct；10-catalyst heat exchange device；11-regeneration
Standpipe；12-the first airduct；13-the II inclined tube；14-external warmer；15-the I inclined tube；16-regeneration standpipe；17-sedimentation
The stripping section of device.
Embodiment
The technical solution of the utility model is clearly and completely described below in conjunction with accompanying drawing, it is clear that described
Embodiment is the utility model part of the embodiment, rather than whole embodiments.Based on the embodiment in the utility model, sheet
The every other embodiment that field those of ordinary skill is obtained under the premise of creative work is not made, belongs to this practicality
Novel protected scope.
, it is necessary to explanation in description of the present utility model, term " " center ", " on ", " under ", it is "left", "right", " perpendicular
Directly ", the orientation of the instruction such as " level ", " interior ", " outer " or position relationship are based on orientation shown in the drawings or position relationship, are only
Described for the ease of description the utility model and simplifying, rather than instruction or imply signified device or element must have it is specific
Orientation, with specific azimuth configuration and operation, therefore it is not intended that to limitation of the present utility model.In addition, term " the
One ", " second ", " the 3rd " are only used for describing purpose, and it is not intended that instruction or hint relative importance.
, it is necessary to which explanation, unless otherwise clearly defined and limited, term " are pacified in description of the present utility model
Dress ", " connected ", " connection " should be interpreted broadly, for example, it may be fixedly connected or be detachably connected, or integratedly
Connection；Can be mechanical connection or electrical connection；Can be joined directly together, can also be indirectly connected by intermediary,
It can be the connection of two element internals.For the ordinary skill in the art, above-mentioned art can be understood with concrete condition
Concrete meaning of the language in the utility model.
Embodiment one
As shown in figure 1, the present embodiment one provides a kind of catalytic cracking unit, it includes：Riser reactor 3, settler
2nd, regenerator 4 and catalyst heat exchange device 10；The top of riser reactor 3 connects with settler 2, the bottom of riser reactor 3
Portion connects with catalyst heat exchange device 10；The stripping section 17 of settler is connected by regeneration standpipe 16 with regenerator 4；Regenerator 4 divides
Do not connected by standpipe 11, the first airduct 12 with catalyst heat exchange device 10；Catalyst heat exchange device 10 and regenerator 4 are all connected with
There is the second airduct 9 of the main wind of supply system.
The operation principle of catalytic cracking unit that the present embodiment one provides is：
Feedstock oil enters the bottom of riser reactor 3 from raw material oil inlet 7, with the catalysis from catalyst heat exchange device 10
Agent contacts, and completes the heating, vaporization and reaction of raw material.Reacted oil gas is with reclaimable catalyst on the top of riser reactor 3
Portion is rapidly separated through thick rotation, and the gas isolated enters settler 2, after being separated off the catalyst fines of carrying wherein, instead
Answer the reacted oil gas vent pipe 1 of oil gas to leave settler 2, realize and separate into fractionating column.Reclaimable catalyst enters through thick spin material leg
Enter the stripping section 17 of settler, herein with stripped vapor counter current contacting, with oil gas entrained in stripping catalyst.After stripping
The main wind of system and the first airduct 12 that reclaimable catalyst is introduced through regeneration standpipe 16 into regenerator 4 with the second airduct 9 are introduced
Catalyst heat exchange device 10 in hot blast contact burnt, realize completely regeneration.High temperature regeneration agent after regeneration is vertical through regenerating
Pipe 11 enters catalyst heat exchange device 10, the main wind contact heat-exchanging of system introduced with the second airduct 9, after fully heat exchange, on the one hand
Main air temperature rise after heat exchange, then burnt by the first airduct 12 into regenerator 4, another aspect regenerated catalyst temperature
Degree reduces, then enters bottom and the feedstock oil haptoreaction of riser reactor 3 by the first regenerator sloped tube 8, contacts finish
Temperature reduces, and feedstock oil heat cracking reaction degree weakens, and dry gas and coke yield decline to a great extent, and total liquid yield significantly improves.
It is to react the cyclic process with regeneration above.
Compared with prior art, above-mentioned catalytic cracking unit is additionally arranged catalysis between regenerator 4 and riser reactor 3
Agent heat exchanger 10, so as to by cracking reaction-sedimentation-regeneration-exchange heat this series of process circulation, realize circulation life
Produce to increase the purpose of oil ratio.
First, heat transfer process is carried out in single equipment-catalyst heat exchange device 10, and high temperature regeneration is catalyzed
Agent be with the air contact of flowing exchange heat, realize regenerated catalyst cooling and recovery waste heat purpose, thus avoid with it is to be generated
The problem of catalyst contact heat-exchanging causes catalyst activity to reduce.
Second, wind speed and air quantity in catalyst heat exchange device 10 can be controlled by the first airduct 12 and the second airduct 9,
So as to reach the purpose of catalyst temperature in steady control heat exchanger.
3rd, the temperature of burning in regenerator 4 can also be by controlling the air quantity of the first airduct 12 and the second airduct 9 to realize
Steady control.
4th, in above-mentioned production process, catalyst internal circulating load significantly improves, i.e., oil ratio increases, because containing in catalyst
There is certain metal oxide, the catalyst internal circulating load of raising, therefore can be bright equivalent to can play a part of more sulfur transfer additives
It is aobvious to reduce SO in catalysis flue gasxContent.
As can be seen here, compared with prior art, the utility model can take into account catalyst activity and temperature plateau controls two
Aspect, therefore oil ratio further improves during production, thermal response reduction, catalytic reaction increase, coke and dry gas yied reduce, vapour
Oily yield increase, and commercial Application can be realized completely.In addition, said apparatus is applied to reduced crude, decompression residuum, straight run
The raw materials such as wax oil, wax tailings, deasphalted oil, hydrogenation tail oil, recycle oil, slurry oil, crude oil, shale oil, artificial oil, coal tar
Deep processing.
Embodiment two
As shown in Fig. 2 the technical scheme disclosed in the present embodiment two includes the technical scheme disclosed in embodiment one, it is real
The protection content that the content that example one is protected falls within the present embodiment two is applied, it is no longer repeated for identical part.
Specifically, the catalytic cracking unit that the present embodiment two provides also includes external warmer 14, external warmer 14 and regeneration
Device 4 connects.
Preferably, external warmer 14 is connected by the Ith inclined tube 15, the IIth inclined tube 13 with regenerator 4 respectively.
The present embodiment two is set up the waste heat released when external warmer 14 can regenerate catalyst and recycled,
It can also be acted synergistically with catalyst heat exchange device 10 to control the rate of recovery of heat.
Embodiment three
As shown in Figure 3, Figure 4, the technical scheme disclosed in the present embodiment three is including disclosed in embodiment one, embodiment two
Technical scheme, the content that embodiment one, embodiment two are protected falls within the protection content of the present embodiment three, identical part
It is no longer repeated.Specifically, the present embodiment three is for obtained by above-described embodiment one, embodiment two specifically refinement.
In the present embodiment three, catalyst heat exchange device 10 is connected by the bottom of the first regenerator sloped tube 8 and riser reactor 3
It is logical.Regenerator 4 is connected by the second regenerator sloped tube 6 with the middle part of riser reactor 3.
Under normal circumstances, catalytic cracking reaction aggregate performance is the endothermic reaction, and with the increase of riser height, reaction is not
Disconnected to carry out, the temperature of catalyst can continuous decrease.The feed jet mixing section above nozzle, jet phase (representing mist of oil) and particle phase
It is uniform that the distributional pattern of (representing catalyst) is unfavorable for two alternate contacts very much, the big position of jet phase concentration, particle phase it is dense
Degree it is small, do not match that, particle phase matched with the concentration distribution of jet phase it is bad, be influence finish two-phase well can not uniformly connect
The main reason for touching.And above-mentioned decision design increases by the second regenerator sloped tube 6 in the interlude of riser reactor 3, so as to will again
For raw catalyst transport to the less interlude of particle phase Relative distribution, the regenerated catalyst now filled into can properly increase particle phase
The less region of concentration, makes jet phase match with particle phase concentration, realizes that finish two-phase uniformly contacts, and suppresses particle phase concentration
The heat cracking reaction that smaller area occurs, promotes the progress of catalytic reaction.
Further, since regenerated catalyst carries heat, therefore it can be anti-to fill into regenerated catalyst in the other regions of riser
Additional heat is answered, while improves catalyst average activity in riser, ensures that catalytic reaction is persistently carried out, is able to product distribution
Optimization.
Preferably, the second regenerator sloped tube 6 is connected by middle part of multiple branch pipes 5 respectively with riser reactor 3, and more
Individual branch pipe 5 is distributed in the different height of riser reactor 3.
Regenerated catalyst is branched to the diverse location of the interlude of riser reactor 3 by multiple branch pipes 5, to make to carry
The reaction temperature profile of riser reactors 3 everywhere is uniform, and close to riser reactor 3, isothermal reaction (lifts tube reaction everywhere
The axial temperature of device 3 is approximately equalised) perfect condition, so as to improve product quality and yield.
For existing production technology, the axial temperature of riser reactor 3 is preferably 450-560 DEG C, preferably 460-
550 DEG C, preferably 470-540 DEG C；Reaction time is generally 0.5-5 seconds, preferably 1.0-4.5 seconds, best 1.5-4.0 seconds；Agent
Oily ratio generally 3-20, preferably preferably 5-18,7-15；Reaction absolute pressure is generally 0.15-0.45MPa, preferably
0.20-0.42MPa, preferably 0.22-0.40MPa.
After setting multiple branch pipes 5, the main air quantity of heat exchange for entering catalyst heat exchange device 10 typically constitutes from the 20%- of all main air quantity
100% (volume ratio), preferably 30%-90% (volume ratio), preferably 40%-85% (volume ratio)；In catalyst heat exchange device
Regenerative agent temperature is generally 580-670 DEG C, preferably 600-660 DEG C, preferably 610-660 DEG C after 10 heat exchange.It is defeated by catalyst
The total catalyst internal circulating load that inclined tube, supervisor, branch pipe 5 are delivered to riser reactor 3 is sent as the global cycle amount of riser reactor 3
5-30% (weight ratio)；The regeneration temperature of regenerator 4 is 650-750 DEG C, and the phosphorus content of regenerated catalyst is 0.02-0.2% (weights
Measure ratio), micro-activity is generally 55-70.
The connected position of the branch pipe 5 and riser reactor 3 that are preferably located at the bottom of riser reactor 3, which is located at, to be carried
The top 0.5-10m of raw material oil inlet 7 of riser reactors 3.Above raw material oil inlet 7 at 0.5-10m, particle phase and jet phase
Concentration distribution matching it is substantially poor, therefore here set first meaning of branch pipe 5 it is bigger.
Further, the connected position interval 4-10m of two neighboring branch pipe 5 and riser reactor 3.This interval is set
Length, it is ensured that the axial temperature of riser reactor 3 is in optimal scope (470-540 DEG C).
In addition, being directed to the existing specification of riser reactor 3, branch pipe 5 can be set 1-5 roots, be preferably provided with 5.
In addition, controlling the flow and air quantity of catalyst for convenience, valve can be set on each branch pipe 5, airduct, inclined tube
Door, for instance, it is preferred that all branch pipes 5 are provided with valve, it is preferable that the second regenerator sloped tube 6 is provided with valve, it is preferable that the first regeneration
Inclined tube 8 is provided with valve.
Example IV
The present embodiment four provides a kind of petroleum refining equipment, and it is included in embodiment one, embodiment two or embodiment three
Catalytic cracking unit.
It is not described in detail as the concrete structure of the catalytic cracking unit in the present embodiment three, the present embodiment four is not only
This body structure of the catalytic cracking unit is protected, but also protects the petroleum refining equipment of the catalytic cracking unit.As for this
The concrete composition of petroleum refining equipment can continue to use equipment of the prior art, according to being actually needed flexible selection.
Finally it should be noted that：Various embodiments above is only to illustrate the technical solution of the utility model, rather than it is limited
System；Although the utility model is described in detail with reference to foregoing embodiments, one of ordinary skill in the art should
Understand：It can still modify to the technical scheme described in foregoing embodiments, either to which part or whole
Technical characteristic carries out equivalent substitution；And these modifications or replacement, the essence of appropriate technical solution is departed from this practicality newly
The scope of each embodiment technical scheme of type.
Claims (5)
- A kind of 1. catalytic cracking unit, it is characterised in that including：Riser reactor, settler, regenerator, external warmer and Catalyst heat exchange device；The top of the riser reactor connects with the settler, and the catalyst heat exchange device passes through first Regenerator sloped tube connects with the bottom of the riser reactor；The stripping section of the settler passes through regeneration standpipe and the regeneration Device connects；The regenerator is connected by standpipe, the first airduct with the catalyst heat exchange device respectively；The catalyst changes Hot device and the regenerator are respectively connected with the second airduct of the main wind of supply system；The external warmer passes through the Ith inclined tube, respectively II inclined tube connects with the regenerator；The regenerator is by the second regenerator sloped tube with connecting in the middle part of the riser reactor It is logical；Second regenerator sloped tube is connected by middle part of multiple branch pipes respectively with the riser reactor, and the multiple Branch pipe is distributed in the different height of the riser reactor.
- 2. catalytic cracking unit according to claim 1, it is characterised in that positioned at the riser reactor bottom The connected position of the branch pipe and the riser reactor is located at 0.5- above the raw material oil inlet of the riser reactor 10m。
- 3. catalytic cracking unit according to claim 1, it is characterised in that the two neighboring branch pipe and the riser The connected position interval 4-10m of reactor.
- 4. catalytic cracking unit according to claim 1, it is characterised in that the branch pipe, first regenerator sloped tube and Valve is equipped with second regenerator sloped tube.
- 5. a kind of petroleum refining equipment, it is characterised in that including the catalytic cracking unit any one of claim 1-4.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720089059.1U CN207016721U (en) | 2017-01-20 | 2017-01-20 | Catalytic cracking unit and petroleum refining equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720089059.1U CN207016721U (en) | 2017-01-20 | 2017-01-20 | Catalytic cracking unit and petroleum refining equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN207016721U true CN207016721U (en) | 2018-02-16 |
Family
ID=61460305
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201720089059.1U Expired - Fee Related CN207016721U (en) | 2017-01-20 | 2017-01-20 | Catalytic cracking unit and petroleum refining equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN207016721U (en) |
-
2017
- 2017-01-20 CN CN201720089059.1U patent/CN207016721U/en not_active Expired - Fee Related
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