CN2360148Y - Catalytic cracking lifting tube reactor - Google Patents
Catalytic cracking lifting tube reactor Download PDFInfo
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- CN2360148Y CN2360148Y CN 97216545 CN97216545U CN2360148Y CN 2360148 Y CN2360148 Y CN 2360148Y CN 97216545 CN97216545 CN 97216545 CN 97216545 U CN97216545 U CN 97216545U CN 2360148 Y CN2360148 Y CN 2360148Y
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- carrier pipe
- tube
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Abstract
The utility model relates to a catalytic cracking lifting tube reactor, and a pre-lifting area arranged on the bottom of the catalytic cracking lifting tube reactor can be improved to be an enlarging pipe. Owning to the different setting positions of an inner conveying pipe and a gas lifting pipe and the different connection forms of the enlarging pipe and the gas lifting pipe in the enlarging pipe, two novel catalytic cracking lifting tube reactors can be achieved, and contact conditions of catalyst improvement and raw oil improvement all can by achieved by the two catalytic cracking lifting tube reactors. The utility model has the advantages of yield and quality increase of objective products, operating flexibility increase of equipment and energy consumption reduction.
Description
The utility model belongs to the petroleum refining field, and the riser reactor that relates in particular to catalytic cracking unit improves.
Well-known catalytic cracking unit is of paramount importance secondary operations means in the petroleum refining industry, and the reactor-regenerator system of this device is one of topmost equipment in the catalytic cracking reaction process, in decades, continuous change along with raw material and processing technology, its technological process and process equipment also constantly improve, and course of reaction also develops into riser cracking by bed cracking gradually.Riser reactor can be divided into three operating mode districts: the pre-lifting zone in bottom (I), reaction zone (II) and outlet quick Disengagement zone (III) (seeing accompanying drawing 1), enter wherein through regenerator sloped tube at the catalyst of the pre-lifting zone in riser bottom from regenerator, under the effect of pre-lift gas, when rising and the oily vapour haptoreaction of nozzle ejection along riser, separate fast in the riser exit, isolated oily vapour enters fractionating system, catalyst then enters regenerator and regenerates behind stripping, burn the carbon distribution of catalyst surface, then, enter riser by regenerator sloped tube again, finish the cyclic process of a catalyst.The employed riser reactor of domestic industry device is two kinds of straight barrel type and bottom undergauges mostly at present.Because the no cushion space in the riser reactor of these two kinds of versions bottom, and promoting steam in advance directly upwards blows, the regenerator sloped tube feed opening is checked effect, regenerator sloped tube catalyst blanking resistance is strengthened, thereby the blanking shakiness produces pressure oscillation when causing catalyst to enter riser reactor, influences quiet run.This also is that catalyst recycle intensity is little in present most commercial plant, the main cause that the oil ratio operating flexibility is low.Regenerated catalyst easily forms bias current through the side that inclined tube enters riser reactor simultaneously; And make population of catalyst particles have side velocity, in it makes progress lifting process, collide repeatedly, launch, form " S " type movement locus, behind certain altitude, could disappear with the riser wall.This has just aggravated the riser lower area, by the inhomogeneous situation of radial distribution that wall effect causes, from simulated test, can find out, and the radial density distribution of catalyst in the present commercial plant, the limit wall exceeds about 3 times than center density.In order to address these problems, industry adopts the way of the pre-riser height of lengthening to solve this contradiction, and existing industrial upgrading pipe reactor pre lift zone height is mostly in 2～4m scope, individual device even reach about 6m.But increase pre-hoisting depth can only reduce catalyst with the feedstock oil haptoreaction before " S " type track distribute; And to improving wall effect and pressure oscillation DeGrain.The pre-lifting linear speed of process units is mostly about 1m/s at present, sometimes in order to improve the catalyst circulation amount, linear speed is brought up to 2～3m/s, but increased inclined tube blanking resistance, so the raising that promotes linear speed in advance there is no positive effect to the increase of internal circulating load because of the raising of pre-hoisting velocity is corresponding.In sum, under present apparatus structure and operating condition, feedstock oil enters riser reactor and contacts with catalyst stream pockety, can produce cracking and coking, or cracking level is not enough, thereby influences purpose product yield and quality, and Zhuan Zhi operating flexibility is also little simultaneously.The patent of relevant catalytic cracking riser reactor lifting aspect in advance is more, is typical for United States Patent (USP) U.S.4,820,493 (as Fig. 5).Establish enlarged tube (4) in the riser reactor bottom, establish carrier pipe (14) in the pipe, promote steam in advance and enter carrier pipe (14) by pipe (3), catalyst enters enlarged tube (4) through regenerator sloped tube (10), and the top is an air chamber, and the bottom is a catalyst.Catalyst enters carrier pipe (20) center under enlarged tube (4) air chamber pressure effect.At a plurality of nozzles of carrier pipe periphery.Feedstock oil after nozzle atomization with riser in catalyst stream directly contact, produce cracking reaction, enlarged tube is provided with the steam regulating system in (4), controls the top air chamber pressure of enlarged tube (4) by the quantity of steam of regulating (44), thereby reaches the purpose of regulating enlarged tube (4) controlling level.To this structure,, catalyst can effectively be contacted with feedstock oil because catalyst directly sprays into riser (20) center from carrier pipe (14).In this patent, enlarged tube (4) is enclosed, and enlarged tube (4) is actually through pipe 14 two unit of connecting with riser (20), and agent, vapour can only enter riser (20) through pipe (14).Its shortcoming is: it is hopeless that (1) enters the gas (44) of enlarged tube (4) top air chamber, can only be through regenerator sloped tube up or enter riser with catalyst through carrier pipe (14), will directly influence flowing of inclined tube inner catalyst like this; And catalyst is pressed into carrier pipe by air chamber pressure, and this just needs higher air chamber pressure, and it can cause the regenerator sloped tube blanking to interrupt, thereby reduces the smooth operation of device greatly.(2) owing to do not establish fluidisation vapour in the enlarged tube (4), catalyst can form moving bed or dead bed in pipe, be unfavorable for the lifting of catalyst, thereby causes the catalyst circulation amount to descend, and influences efficient.(3) because being set, the material level regulating system makes complicated operationization.
The purpose of this utility model be the defective that exists at above-mentioned riser reactor for the blanking state that improves regenerator sloped tube and catalyst in the distribution of the section of carrying in advance, thereby improve catalyst and feedstock oil contact conditions in the riser, improve the yield and the quality of purpose product; Two kinds of new catalytic cracking riser reactors are provided, its hoisting power is greatly strengthened, improve the operating flexibility of device, and cut down the consumption of energy.
The utility model is that two schemes of a kind of design all are to improve and obtain two kinds of novel catalytic cracking riser reactors at the pre-lifting zone (I) in catalytic cracking riser reactor bottom, it is enlarged tube (20) (seeing accompanying drawing 1) that a scheme and b scheme are the pre-lifting zone (I) in riser reactor bottom, interior carrier pipe (25) is set in enlarged tube (20), lift gas pipe (23), fluidizing gas pipe (21), fluid distribution of gas endless tube (22), this is the common design of two different schemes, different position and lift gas pipes is arranged on diverse location in the enlarged tube (20) because interior carrier pipe (25) is arranged on, and enlarged tube (20) is different with the type of attachment of riser (27), all can reach common purpose and identical effect and formed two kinds of different schemes.First kind of scheme seen accompanying drawing 2 for (a), the riser reactor bottom is enlarged tube (20a), enlarged tube (20a) is connected with riser (27a), in enlarged tube (20a) carrier pipe (25a) being installed can be venturi type, can offer various forms of apertures on it, the arrival end (24a) of interior carrier pipe (25a) is seen accompanying drawing 4,25G has a, b, three kinds of forms of c, the port of export is seen accompanying drawing 4 for (26a), and 25R has d, e, f, four kinds of forms of g, the arrival end (24a) of (25a) of interior carrier pipe are positioned at regenerator sloped tube (29a) end bottom or top, and the port of export (26a) of interior carrier pipe (25a) is positioned under the feedstock oil nozzle (28a), the centre of carrier pipe (25a) arrival end (24a) in lift gas pipe (23a) inserts, fluidizing gas pipe (21a) and fluidizing gas distribution endless tube (22a) are set in the bottom of enlarged tube (25a), the aperture under the mind-set of many holes is arranged on the fluidizing gas distribution endless tube (22a), and the middle footpath (D of fluidizing gas distribution endless tube (22a)
3a) greater than the diameter (M) of interior carrier pipe (25a) arrival end (24a).Lift gas (1a) is in lift gas pipe (23a) enters interior carrier pipe (25a), interior carrier pipe (25a) is positioned at enlarged tube (20a) center, the lift gas medium can be steam, gasoline, feedstock oil, dry gas etc., and making lift gas with dry gas can heavy metal-passivated pollution to catalyst.The catalyst of the interior bed 3a of enlarged tube (20a) is provided by regenerated catalyst stream (31a), regenerated catalyst stream (31a) is to enter in the enlarged tube (20a) through guiding valve (30a) and regenerator sloped tube (29a), catalyst in the beds 3a is under the effect of lift gas (1a), periphery by the arrival end (24a) of interior carrier pipe (20a) enters in the interior carrier pipe (25a), enters riser (27a) from the port of export (26a) then; Interior carrier pipe (25a) is positioned at enlarged tube (20a) inside, interior carrier pipe (25a) port of export (26a) is apart from the height Z＜4000mm of feedstock oil nozzle (28a), it is principle that the length of interior carrier pipe (25a) stretches in the riser (27a) with it, guaranteeing promptly that it can stretch in the riser (27a) gets final product, and the linear gas velocity in the interior carrier pipe (25a) is 0.1～18m/s; Fluidizing gas (2a) enters fluidizing gas distribution endless tube (22a) through fluidizing gas pipe (21a), many downward aperture from the fluidizing gas distribution endless tube (22a) sprays into the catalyst that makes in the enlarged tube (20a) in the bed (3a) and is in fluidized state, the middle footpath D of distribution endless tube (22a)
3aDiameter (M) greater than interior carrier pipe (25a) arrival end (24a) is D
3a＞M, just can guarantee that fluidizing gas enters in the riser (27a) in the outside annular space of interior carrier pipe (20a), fluidizing gas distribution endless tube (22a) is L＞20mm apart from the distance of interior carrier pipe (25a) arrival end (24a), and the linear speed of fluidizing gas is at 0.01～5.0m/s.
Feedstock oil enters riser (27a) and carries out catalytic cracking reaction with the direct even contact of catalyst that riser (27a) middle and upper reaches are come after nozzle (28a) atomizing, product that reaction generates and catalyst together enter settler (35) (referring to accompanying drawing 1) through riser (27a) outlet (37a), at settler (35) inner catalyst after sedimentation, product enters primary cyclone (36a) and secondary cyclone (36B), and isolated product enters fractionating column; The catalyst that cyclonic separation is got off enters dense-phase bed (4), catalyst in the bed (4) contacts with stripped vapor (33), remove the cracked product that catalyst stream carries, in the stripping section baffled (34), catalyst behind the stripping leaves this device and enters in the regenerator of catalyst regenerates, and returns pre-lifting area under control then.
The utility model (a) technical scheme implementation procedure is seen accompanying drawing 2.
Regenerated catalyst stream (31a) enters in the enlarged tube (20a) from regenerator sloped tube (29a), and regenerated catalyst is regulated by guiding valve (30a), and the catalyst that enters enlarged tube (20a) has cushion space, both can reduce pressure oscillation, can eliminate its horizontal force action again." S " type movement locus that this has just eliminated straight barrel type riser reactor catalyst helps it and evenly distributes in riser.
The interior catalyst of enlarged tube (20a) enters interior carrier pipe (25a) and sprays into riser (27a) center along pipe (25a) rising through the mouth of pipe (26a) under the effect of pressure and pre-lift gas (1a).Because interior carrier pipe caliber (25a) is less than riser (27a) caliber, the catalyst stream that sprays into riser will be the radial pattern flow regime, flow to riser (27a) limit wall at catalyst, also do not form rare place, the close center of limit wall, feedstock oil nozzle (28a) is set.So just guaranteed that the nozzle region catalyst distribution is even, in this district's inner catalyst radial density distribution, high and low point only differs about 20%, thereby has effectively improved the pre lift zone wall effect to the radially harmful effect of Density Distribution.Feedstock oil nozzle (28a) sprays into the feedstock oil after the atomizing the catalyst stream that is evenly distributed on every side from riser (27a), and agent, oil contact are more become evenly, and reaction efficiency is improved.Interior carrier pipe (25a) is an autonomous system, because of it is imbedded in enlarged tube (20a) the catalyst dense bed (3a), keep certain bed height promptly to keep under certain catalyst transport Impetus Condition in enlarged tube (20a), the hoisting power of carrier pipe in can improving greatly.Under identical lifting linear speed condition, the intensity of circulation of interior carrier pipe (27a) inner catalyst is enhanced about more than once than the pre-lifting constructional device of straight barrel type.This explanation is under the identical preceding topic of device catalyst circulation amount, and the utility model structure can reduce pre-lift gas consumption than the straight barrel type structure, reaches energy-saving and cost-reducing purpose.Because carrier pipe promotes catalyst in adopting, carry linear speed in advance the influence of catalyst recycle intensity is significantly strengthened, the adjusting of agent, oil ratio is become flexibly, the operating flexibility of whole device is improved.
Fluidizing gas (2a) enters and makes bed (3a) inner catalyst be able to fluidisation in the enlarged tube (20a), can guarantee that at fluidized state lower bed layer (3a) regenerator sloped tube (29a) blanking is unimpeded, can make catalyst again under lift gas 1a effect, enter in the interior carrier pipe arrival end (24a) along periphery.
In enlarged tube (20a) bottom fluidizing gas endless tube (22a) is set, makes the catalyst in the enlarged tube (20a) be in fluidized state, the fluidisation linear speed is in 0.01～5m/s scope.Both can guarantee that the regenerator sloped tube blanking was unimpeded, and can keep certain bed height again, guarantee the hoisting power of carrier pipe (25a).Fluidizing gas (2a) enters from interior carrier pipe arrival end (24a) annular space on every side and promotes tube edge wall district in addition, helps catalyst in the riser reactor center flow, reduces the influence of wall effect.
The effect that the utility model (a) scheme reaches is as follows:
(1) enlarged tube (20a) is communicated with riser (27a), is easy to realize continuous quiet run.
(2) interior carrier pipe (25a) is an autonomous system, and pre-lift gas enters interior carrier pipe, can reduce regenerator sloped tube blanking resistance, and the pre-lift gas amount of available adjustment is controlled and promoted the reactor catalyst internal circulating load, improves the device operating flexibility.
(3) establish the fluidizing gas pipe in the enlarged tube (20a), make the catalyst in the enlarged tube be in fluidized state, both can reduce and fluctuate, guaranteed again regenerator sloped tube blanking is unimpeded, and can improve the hoisting power of interior carrier pipe (25a), reduces pre-lift gas consumption.
(4) fluidizing gas finally enters from periphery and promotes tube edge wall district, impels catalyst in the riser center flow, can reduce the influence of whole riser reactor wall effect, helps oil, the reaction of agent even contact.
(b) of the present utility model scheme is seen accompanying drawing 3, catalytic cracking riser reactor comprises the pre-lifting zone (I) in bottom, middle part catalyst and the direct haptoreaction of oil gas district (II) and top product and the quick Disengagement zone of catalyst (III), it is characterized in that riser reactor bottom (I) is enlarged tube (20b), and enlarged tube (20b) is by interior carrier pipe (25b) and riser (27b) polyphone, the top of enlarged tube (20b) is air chamber E, its underpart is the dense bed (3b) of catalyst, the arrival end (24b) of interior carrier pipe (25b) is seen accompanying drawing 4 (a--c), the port of export is seen accompanying drawing 4 (d--f), and the arrival end (24b) of interior carrier pipe (25b) is positioned on regenerator sloped tube (29b) port; Its distance H＞5mm, interior carrier pipe (25b) port of export (26b) stretches out outside the enlarged tube (20b) and is positioned at side under the feedstock oil nozzle (28b), lift gas pipe (23b) is positioned at the air chamber (E) on carrier pipe (25b) arrival end (24b), apart from interior carrier pipe arrival end distance L＞5mm, fluidizing gas pipe and fluidizing gas distribution endless tube (22b) are arranged in the enlarged tube (20b) of regenerator sloped tube (29b) below, fluidizing gas distribution endless tube (22b) is gone up the many apertures under the porose mind-set, and the fluidizing gas distribution rings is apart from regenerator sloped tube (29b) port distance L
b＞20mm.
Lift gas (1b) enters air chamber (E) from lift gas pipe (23b) and enters interior carrier pipe (25b) from interior carrier pipe (25b) arrival end (24b) periphery then, and at interior carrier pipe center formation low-pressure area, catalyst is entered in it along interior carrier pipe (25b) center, and catalyst sprays into riser (27b) center with gas after interior carrier pipe (25b) evenly mixes; The catalyst of dense bed (3b) is from regenerated catalyst stream (31b), catalyst stream (31b) enters in the enlarged tube (20b) through guiding valve (30b) and regenerator sloped tube (29b), the a plurality of apertures of fluidizing gas (2b) on fluidizing gas pipe (21b) and fluidizing gas distribution rings (22b) spray in the enlarged tube (20b), make the pre-fluidisation of catalyst in the catalyst dense bed (3b), catalyst presents good mobility under the gas effect.
The utility model (b) implementation procedure is as follows: referring to accompanying drawing 3.Regenerated catalyst enters enlarged tube (20b) from regenerator sloped tube (29b), both can reduce pressure oscillation, can overcome the effect of horizontal force again.Fluidizing gas (2b) makes the catalyst in the bed (3b) get fluidisation, guarantees that the regenerator sloped tube blanking is unimpeded.Fluidizing gas (2b) finally enters riser (27b) from interior carrier pipe (25b), can play the wind effect that promotes again.Lift gas (1b) in pipe (23b) enters carrier pipe and the enlarged tube annular space (B) inside carrier pipe pre-lifting gas is provided.Enlarged tube (25b) middle and upper part is an air chamber, and the bottom is a dense bed.Catalyst enters riser from interior carrier pipe under the effect of pressure and lift gas (1b), carrier pipe center in catalyst enters along interior carrier pipe (25b) inlet tube (24b) sprays into the riser center through port (26b) then.The setting of feedstock oil nozzle just can guarantee that the nozzle region catalyst distribution is even in position, and the wall effect of the section of carrying is eliminated substantially.Carrier pipe inlet (24b) catalyst circulation amount can be regulated by pre-lifting tolerance (1b) in enlarged tube (20b) material level was higher than.
The effect that the utility model (b) scheme reaches:
(1) carrier pipe played castering action in fluidizing gas (1b) finally entered, thereby reduced gas usage.
(2) lift gas (1b) enters interior carrier pipe from interior carrier pipe (24b) periphery that enters the mouth, produce low pressure at tube hub, make catalyst along rising on the center, the wall effect of carrier pipe in can effectively alleviating, thus it is even to help riser reactor catalyst radial distribution.
Accompanying drawing and explanation thereof.
Accompanying drawing 1 is the utility model catalytic cracking riser reactor schematic diagram.
Accompanying drawing 2 is the utility model (a) scheme schematic diagrames.
Accompanying drawing 3 is the utility model (b) scheme schematic diagrames.
1 1a 1b lift gas
2 2a 2b fluidizing gas
The dense bed of 3 3a 3b enlarged tube (20a and 20b) bottoms
20 20a 20b enlarged tube
21 21a 21b fluidizing gas inlet tubes
22 22a 22b fluidizing gas distribution endless tubes
23 23a 23b lift gas inlet tubes
The inlet tube of carrier pipe (25a and 25b) in the 24 24a 24b
Carrier pipe in the 25 25a 25b
The outlet of carrier pipe (25a and 25b) in the 26 26a 26b
27 27a 27b risers
28 28a 28b feedstock oil nozzles
29 29a 29b regenerator sloped tubes
30 30a 30b guiding valves
Catalyst after the 31 31a 31b regeneration
32 remove the recycling catalyst of regenerator
33 stripped vapors
34 plate washers
35 settlers
The 36A primary cyclone
The 36B secondary cyclone
The outlet of 37 risers (27)
The diameter of carrier pipe (25) in the A
Void space in the B between carrier pipe (25) and the riser (27) is an air chamber
C is the diameter of riser (27)
D
1AD
1B is a lift gas pipe diameter
D
2AD
2B is a fluidizing gas pipe diameter
D3aD3b is footpath in the distribution rings, and middle footpath is the diameter that the footpath adds pipe within the ring, and F is the diameter of enlarged tube (20)
N is interior carrier pipe (a 25) port of export diameter
Carrier pipe (25) arrival end diameter in the M
H
1Height for enlarged tube (20)
H
2Height for interior carrier pipe (25)
Z is the distance of feedstock oil nozzle (28) to interior carrier pipe (25) port of export (26)
H is the distance between regenerator sloped tube (29) and interior carrier pipe (25) arrival end (24)
La is the distance between fluidizing gas distribution endless tube 22a and the interior carrier pipe arrival end 24a
Lb is the distance of fluidizing gas distribution endless tube 22b and regenerator sloped tube (29b) port
E is the top of enlarged tube in the accompanying drawing 3 (20b), by the formed annular space air chamber of inwall of wall outside the carrier pipe (25b) and enlarged tube (20b)
I is the annular space that interior carrier pipe outer wall and riser inwall form
Accompanying drawing 4 is interior carrier pipe (25) form figure, and wherein 25G is a, b, three kinds of inlet forms of c, and 25R is d, e, four kinds of outlet forms of f, g
Accompanying drawing 5 is United States Patent (USP)s 4,820,493 riser schematic diagrames
3-in advance promote steam pipe 10-regenerator sloped tube
4-enlarged tube, 14-carrier pipe
Inwall 20-the riser of 6-enlarged tube
8-steam, 44-steam
| Embodiment classify riser reactor device parameter and technological parameter | The a scheme | The | ||
| Embodiment | ||||
| 1 | |
Embodiment 3 | Embodiment 4 | |
| F/H 1 mm | φ1800/ 4000 | φ1400/ 3100 | φ1600/ 4000 | φ1250/ 3000 |
| A/H 2 mm | φ1000/ 3800 | φ800/2800 | φ900/3000 | φ700/2800 |
| D 1 mm | φ159 | φ108 | φ159 | φ108 |
| D 2 mm | φ108 | φ89 | φ108 | φ89 |
| Z | 1800 | 1600 | 1800 | 1600 |
| H | 450 | 400 | 1000 | 800 |
| L b | 800 | 600 | ||
| D 3 mm | φ1400 | φ1100 | φ1200 | φ1000 |
| Interior carrier pipe lift gas linear speed m/s | 2.0 | 1.8 | 2.0 | 1.8 |
| Promote fluidizing gas linear speed m/s | 0.1 | 0.1 | 0.08 | 0.08 |
| Riser reactor treating capacity t/a | 140×10 4 | 80×10 4 | 120×10 4 | 60×10 4 |
| Riser reactor specification (diameter * height) | φ1300/43500 | φ1000/38000 | φ1150/4000 | φ900/3400 |
| Green coke W% | 8.25 | 7.5 | 8.3 | 8.15 |
| Riser inlet/outlet temperature ℃ | 520/510 | 520/510 | 495/485 | 510/500 |
| Riser inlet/outlet pressure MPa | 0.3/0.27 | 0.25/0.21 | 0.28/0.26 | 0.24/0.21 |
Claims (2)
1, a kind of catalytic cracking riser reactor comprises the pre-lifting zone (I) in bottom, middle part catalyst and the direct haptoreaction of oil gas district (II) and top product and the quick Disengagement zone of catalyst (III), it is characterized in that the riser reactor bottom is enlarged tube (20a), enlarged tube (20a) is connected with riser (27a); Carrier pipe (25a) in enlarged tube (20a), installing, the arrival end pattern of interior carrier pipe (25a) be 25G (a, b, c); And its port of export pattern be 25R (d, e, f, g); Offer the aperture of various types on the interior carrier pipe, the arrival end (24a) of interior carrier pipe (25a) is positioned under the regenerator sloped tube (29a), also can be positioned at (29a) top; And the interior carrier pipe port of export (26a) is positioned under the feedstock oil nozzle (28a), the centre of carrier pipe (25a) arrival end (24a) in pre-lift gas pipe (23a) inserts.Fluid flue (21a) and fluidizing gas distribution endless tube (22a) are set in the bottom of enlarged tube (25a), many downward apertures are arranged on the fluidizing gas distribution endless tube (22a).And the middle footpath (D of fluidizing gas distribution endless tube (22a)
3a) greater than the diameter (M) of interior carrier pipe (25a) arrival end (24a).
2, a kind of catalytic cracking riser reactor comprises the pre-lifting zone (I) in bottom, middle part catalyst and the direct haptoreaction of oil gas district (II) and top product and the quick Disengagement zone of catalyst (III), it is characterized in that riser reactor bottom (I) is enlarged tube (20b), and enlarged tube (20b) is logical with riser (27b) polyphone by interior carrier pipe (25b), the top of enlarged tube (20b) is air chamber (E), its underpart is dense bed (3b), the arrival end (24b) and the port of export (26b) of interior carrier pipe (25b) are 25G (a, b, c) and 25R (d, e, f, g), and the arrival end (24b) of interior carrier pipe (25b) be positioned at regenerator sloped tube (29b) inlet top; The port of export (26b) of interior carrier pipe (25b) stretches out outside the enlarged tube (26b) and is positioned at side under the feedstock oil nozzle (28b), lift gas pipe (23b) is positioned at the air chamber (E) on carrier pipe (25b) arrival end (24b), fluidizing gas pipe (21b) and fluidizing gas distribution endless tube (22b) are arranged in the enlarged tube (20b) of regenerator sloped tube (29b) below, and many downward apertures are arranged on the fluidizing gas distribution endless tube (22b).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 97216545 CN2360148Y (en) | 1997-05-13 | 1997-05-13 | Catalytic cracking lifting tube reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 97216545 CN2360148Y (en) | 1997-05-13 | 1997-05-13 | Catalytic cracking lifting tube reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN2360148Y true CN2360148Y (en) | 2000-01-26 |
Family
ID=33933417
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 97216545 Expired - Fee Related CN2360148Y (en) | 1997-05-13 | 1997-05-13 | Catalytic cracking lifting tube reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN2360148Y (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1329107C (en) * | 2004-01-09 | 2007-08-01 | 洛阳石化设备研究所 | Hydrocarbon material lift pipe reactor |
| CN105498647A (en) * | 2014-10-14 | 2016-04-20 | 中国石油化工股份有限公司 | Fluidized bed reactor, reaction apparatus and olefin preparation method and aromatic preparation method |
-
1997
- 1997-05-13 CN CN 97216545 patent/CN2360148Y/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1329107C (en) * | 2004-01-09 | 2007-08-01 | 洛阳石化设备研究所 | Hydrocarbon material lift pipe reactor |
| CN105498647A (en) * | 2014-10-14 | 2016-04-20 | 中国石油化工股份有限公司 | Fluidized bed reactor, reaction apparatus and olefin preparation method and aromatic preparation method |
| CN105498647B (en) * | 2014-10-14 | 2018-07-03 | 中国石油化工股份有限公司 | Fluidized-bed reactor, consersion unit and olefin preparation method and aromatic hydrocarbons preparation method |
| TWI661867B (en) * | 2014-10-14 | 2019-06-11 | 大陸商中國石油化工科技開發有限公司 | Fluidized bed reactor, reaction regeneration equipment, method for preparing olefin, and method for preparing aromatic hydrocarbon |
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