CN102399579A - Catalytic cracking method - Google Patents
Catalytic cracking method Download PDFInfo
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- CN102399579A CN102399579A CN2011103111479A CN201110311147A CN102399579A CN 102399579 A CN102399579 A CN 102399579A CN 2011103111479 A CN2011103111479 A CN 2011103111479A CN 201110311147 A CN201110311147 A CN 201110311147A CN 102399579 A CN102399579 A CN 102399579A
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- 238000000034 method Methods 0.000 title claims abstract description 25
- 238000004523 catalytic cracking Methods 0.000 title abstract description 5
- 238000006243 chemical reaction Methods 0.000 claims abstract description 201
- 239000003054 catalyst Substances 0.000 claims abstract description 95
- 238000005336 cracking Methods 0.000 claims abstract description 23
- 239000003502 gasoline Substances 0.000 claims abstract description 23
- 230000003197 catalytic effect Effects 0.000 claims abstract description 5
- 239000002994 raw material Substances 0.000 claims description 12
- 230000008929 regeneration Effects 0.000 claims description 12
- 238000011069 regeneration method Methods 0.000 claims description 12
- 230000035484 reaction time Effects 0.000 claims description 7
- 229930195733 hydrocarbon Natural products 0.000 claims description 5
- 150000002430 hydrocarbons Chemical class 0.000 claims description 5
- 239000003208 petroleum Substances 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 2
- 238000000926 separation method Methods 0.000 claims description 2
- 150000001336 alkenes Chemical class 0.000 abstract description 7
- 230000000694 effects Effects 0.000 abstract description 7
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 238000004939 coking Methods 0.000 abstract description 2
- 238000006011 modification reaction Methods 0.000 abstract 2
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 abstract 1
- 239000000376 reactant Substances 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 32
- 239000007789 gas Substances 0.000 description 29
- 238000005516 engineering process Methods 0.000 description 8
- 230000008569 process Effects 0.000 description 4
- 239000000463 material Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 238000003889 chemical engineering Methods 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 2
- 238000006317 isomerization reaction Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 2
- 239000003209 petroleum derivative Substances 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 238000010517 secondary reaction Methods 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 230000001256 tonic effect Effects 0.000 description 2
- 238000006276 transfer reaction Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000002010 green coke Substances 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 239000011541 reaction mixture Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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Abstract
The invention discloses a catalytic cracking method, and belongs to the technical field of petrochemical engineering. A main reactor and an auxiliary reactor are adopted in the method, wherein the main reactor comprises a lower lift pipe reaction zone and an upper diameter expanded second reaction zone; in the main reactor, the reaction raw oil is in contact with a regenerated catalyst in the lift pipe reaction zone to produce cracking reaction, a part of catalyst is separated from the generated oil gas and catalyst reactant flow at the outlet of the lift pipe reaction zone, and the oil gas and the rest catalyst rise together and undergo gasoline modification reaction in the diameter expanded second reaction zone; and a part of catalyst to be generated in the auxiliary reactor is supplied to the second reaction zone to participate in the gasoline modification reaction. In the method, a part of catalyst inactivated due to coking is separated at the outlet of the lift pipe reaction zone of the main reactor, so that the catalytic activity and the reaction selectivity of the whole main reactor are reinforced; and control on the flow and the activity of the catalyst of the second reaction zone is integrally realized, and the production target of producing more gasoline with low olefins and high octane value is realized.
Description
Technical field
The present invention relates to the petrochemical technology field, particularly relate to a kind of petroleum hydrocarbon raw material catalyst cracking method and device.
Background technology
CCU is topmost gasoline production device, and world's overwhelming majority motor spirit is from CCU, and riser reactor is adopted in conventional catalytic cracking.
The diameter of existing riser reactor is uniform; Carrying out along with catalyzed reaction; More small molecules generate, and molecule expands flow velocity is vertically upward sharply increased, and are unfavorable for improving the carrying out of the alkene secondary reaction that quality product distributes; The Perfected process that addresses this problem is to carry out hole enlargement in the middle and upper part of the riser reaction zone of homogeneous diameter, makes alkene have the longer time to participate in secondary reaction.
CN99105903.4 discloses a kind of riser reactor that is used for fluidized catalytic conversion; Vertically be followed successively by co-axial each other pre lift zone, first reaction zone, enlarged-diameter from bottom to up second reaction zone, reduced outlet area, be connected with one section level pipe at the outlet area end.In this technology; First reaction zone of bottom is a pyrolysis reaction zone, and temperature of reaction is higher, and residence time of material is shorter; And the temperature of reaction of second reaction zone on top reduces; Residence time of material is longer, and material carries out alkylated reaction and hydrogen transfer reactions, improves the content of isoparaffin in the gasoline composition; CN01102240.X discloses a kind of catalysis conversion method of producing low-alkene gasoline and high-yield diesel oil; The regenerated catalyst of raw oil and heat is contacted the cracking reaction of generation macromole at first reaction zone of reactor drum, and the oil gas of generation goes upward to second reaction zone with the band Pd/carbon catalyst and carries out cracking reaction, hydrogen transfer reactions and isomerization reaction; Second reaction zone is thicker than first reaction zone in the engineering design, and its effect is flow velocity and the temperature of reaction that reduces oil gas and catalyzer.
Above-mentioned technology is the MIP technology of Research Institute of Petro-Chemical Engineering's exploitation, and the full scale plant operation result shows that this Technology can significantly reduce olefin content in gasoline, and product liquid is received to be increased, the coke selectivity grow, and dry gas and slurry oil productive rate descend.
But because the enlarged-diameter of riser tube second reaction zone, the second reaction zone fluid velocity sharply reduces, and need replenish the part catalyzer to regulate, to keep the air speed that needs to second reaction zone.For addressing the above problem; In existing design; Research Institute of Petro-Chemical Engineering adopts on the engineering construction of MIP technology and mends into reclaimable catalyst to second reaction zone from settling vessel; Its concrete device design has detailed introduction in " industrial application of the catalytic cracking process of voluminous isoparaffin " literary composition of " refining of petroleum and chemical industry " 2003 the 34th volumes o. 11th 1-6 page or leaf: adopt MIP technology that the refinery 1.4Mt/a of high bridge petrochemical industry branch office CCU is transformed; Riser tube integral replacing, riser tube bottom have increased an extension diameter section as second reaction zone as first reaction zone at the riser tube middle part; Wherein settling vessel integral body is raised 2m; At settling vessel stripping stage upper cone section overflow downcomer is set; Overflow downcomer is provided with on the sedimentation wall extracts mouth out, is communicated with through the pipeline to be generated and second reaction zone bottom of circulating, thereby the part reclaimable catalyst in the settling vessel is introduced second reaction zone.
Keep the problem of air speed with regard to having solved second reaction zone like this, but existing MIP second reaction zone is a reclaimable catalyst, additional catalyzer also is a spent agent, and activity is very low, and katalysis has been very limited; Although so Shi Ke institute requires make-up catalyst (the normal restriction air speed 15 ~ 20 that requires), design also has the tonic measure, tonic not basically in a lot of device operations; The value that air speed also requires far above exploitation side, temperature of reaction can not reduce a lot, and the result can cause green coke to increase, and the thermopositive reaction that gasoline upgrading exists also is suppressed.
Summary of the invention
On the basis of above-mentioned catalyst cracking method, the object of the present invention is to provide a kind of petroleum hydrocarbon raw material catalyst cracking method and device, to adapt to the needs that market changes flexibly, realize the target of fortifying catalytic cracking process production clean gasoline.
The technical scheme that the present invention adopts is following:
A kind of catalyst cracking method is provided with main reactor and auxiliary reactor, and main reactor comprises the riser reaction zone of bottom and second reaction zone that upper diameter enlarges; In the main reactor; Reaction raw materials oil contacts with regenerated catalyst in riser reaction zone cracking reaction takes place; Oil gas that generates and catalyst reaction logistics are isolated a part of catalyzer in the riser reaction zone outlet; Oil gas and residual catalyst are up together, carry out the gasoline upgrading reaction at second reaction zone of enlarged-diameter, it is characterized in that:
⑴ participate in the gasoline upgrading reaction to the reclaimable catalyst that second reaction zone replenishes a part of auxiliary reactor; The reclaimable catalyst that replenishes is perhaps drawn from the auxiliary reactor middle part, perhaps behind auxiliary reactor outlet separation and stripping, draws, and the catalyst temperature that replenishes is below 550 ℃; Said second reaction zone is a fast fluidized bed, and the gas phase flow velocity is 1.2-5.0m/s;
⑵ be provided with grid distributor in the riser reaction zone and second reaction interval, and grid distributor is provided with opening or passage; Be provided with the catalyzer splitter in the riser reaction zone outlet, the coaxial catalyst stripping section that is provided with in the riser reaction zone outside, second reaction zone is arranged on the stripping stage top;
⑶ participate in the main reactor catalyst for reaction and divide two-way to get into the main reaction part; First via catalyzer is directly from the regenerated catalyst of revivifier or through the regenerated catalyst after the cooling; Regenerated catalyst is introduced into the pre lift zone of riser reaction zone raw oil nozzle bottom; With the reaction raw materials contact reacts, reaction is isolated a part of catalyzer after accomplishing in the catalyzer splitter, and catalyzer of not shunted and reaction oil gas upwards get into second reaction zone through grid distributor together; The second road catalyzer is said additional reclaimable catalyst, and the second tunnel catalyst make-up gets into second reaction zone, and carries out the upgrading reaction after above-mentioned catalyzer and reaction oil gas logistics mix.
Further, the shared stripping stage of the reclaimable catalyst of two reaction zones of main reactor reactive moieties, the catalyzer behind the stripping gets into revivifier regeneration through standpipe.
Further, the reacted reclaimable catalyst of second reaction zone partly returns in second reaction zone, and the part reclaimable catalyst is circulated at second reaction zone, increases the catalyzer agent-oil ratio of second reaction zone or reduces reaction velocity.
Further, the 0-80% of the reclaimable catalyst after the said riser reaction zone cracking reaction gets into second reaction zone and participates in the upgrading reaction.
Further, the riser reaction zone reaction conditions does, 500 ℃-620 ℃ of temperature of reaction, and reaction times 0.2-1.6s, oil gas mean flow rate are 5.0 ~ 26m/s; The second reaction zone reaction conditions does, 450 ℃-510 ℃ of temperature of reaction, and reaction times 2.0-5.0s, oil gas mean flow rate are 1.2-4.0m/s, preferred 3.0-3.5m/s.
Further, auxiliary reactor is a riser reactor, and reaction raw materials is C
4One or more of the lighter hydrocarbons that component, catalytic gasoline, coker gasoline, petroleum naphtha are such; The shared settling vessel of auxiliary reactor and main reactor.
Further, the 1.5-4.9 that said second reaction zone diameter is the riser reaction zone diameter times, preferred 2.0-3.5 doubly.
In the inventive method, the reclaimable catalyst of employing auxiliary reactor carries out the displacement of the second reaction zone catalyzer, replenishes, and auxiliary reactor is realized C simultaneously
4Dual-use function Deng hydrocarbon raw material cracking and catalyst transport; The reaction raw materials of auxiliary reactor can also can install from other for the light constituent in the main reactor cracked product of the present invention.
The present invention provides a kind of CCU simultaneously, comprises main reactor, auxiliary reactor, settling vessel, stripping stage, revivifier and catalyst make-up pipeline, it is characterized in that:
⑴ main reactor is provided with second reaction zone of riser reaction zone, enlarged-diameter from bottom to top, and the riser reaction zone outlet is provided with the catalyzer splitter; The coaxial riser reaction zone outside that is arranged at of stripping stage, second reaction zone is arranged on the stripping stage top;
⑵ main reactor, the shared settling vessel of auxiliary reactor and stripping stage are provided with the catalyzer return line between settling vessel, stripping stage, guiding valve is set on the return line;
⑶ be provided with grid distributor in the riser reaction zone and second reaction interval, and grid distributor is provided with a plurality of openings or passage;
⑷ auxiliary reactor is a riser reactor; The center is provided with the reclaimable catalyst outlet; Said catalyst make-up pipeline upper end is communicated with the catalyzer outlet, and the lower end is communicated with second reaction zone, is used for replenishing to second reaction zone reclaimable catalyst of auxiliary reactor.
Further, the 1.5-4.9 that said second reaction zone diameter is the riser reaction zone diameter times, preferred 2.0-3.5 doubly.
Further, the shared oil gas vent of auxiliary reactor and main reactor or the auxiliary reactor oil gas vent is set separately.
Among the present invention, through control get into the amount of the riser reaction zone reclaimable catalyst of second reaction zone, the amount of the reclaimable catalyst of the auxiliary reactor that replenishes to second reaction zone controls the air speed and the catalyst activity of second reaction zone.
In the scheme of the present invention, the auxiliary reactor raw material is light, and catalyst deactivation is slow; At the catalyzer of main reactor riser reaction zone outlet cutting out partial because of the coking inactivation; Replenish the reclaimable catalyst of the greater activity of auxiliary reactor at second reaction zone, can be according to activity of such catalysts appropriate change reaction conditions in engineering construction, as: suitably improve air speed; Reduce temperature of reaction (reducing by 10 ℃ at least), reduce the oil gas reaction times; Perhaps suitably improve the structure of main reactor, as: adopt grid distributor to reduce the catalyzer back-mixing.
Adopt technical scheme of the present invention, have following beneficial effect at least:
⑴ be highly active reclaimable catalyst owing to what replenish to second reaction zone; Catalytic activity and reaction preference in the whole main reactor have been strengthened generally; Effectively suppressed thermal response, can make slurry oil reduction 1.0-2.0% in the reactor product, the total liquid receipts of reaction increase more than 1.0%;
⑵ the reclaimable catalyst of riser reaction zone carried out the catalyzer shunting earlier before getting into second reaction zone; Thereby control gets into the reclaimable catalyst and the reclaimable catalyst ratio of replenishing entering second reaction zone of second reaction zone; Realize control on the whole, realize the productive target of the low alkene stop bracket gasoline of fecund the second reaction zone catalyst flow and catalyst activity;
⑶ adopt with the suitable hole enlargement of second reaction zone, to the additional high activated catalyst of second reaction zone, measures such as shunting earlier, mixing before catalyzer gets into second reaction zone; Strengthened the isomerization reaction of second reaction zone; Realize the target of the low alkene stop bracket gasoline of fecund, reduced the sulphur content in the gasoline simultaneously.
Description of drawings
Fig. 1 is a catalyst cracking method apparatus structure synoptic diagram of the present invention.
Numbering explanation among the figure: 11 riser reaction zone; 12 second reaction zones; 13,51 feed nozzles; 14 grid distributors; 15 catalyst make-up pipelines; 16 pre lift zones; 18 catalyzer splitters; 20 settling vessels; 21 catalyzer return lines; 22 stripping stages; 23,25 oil gas vents; 24 regeneration standpipes; 30 revivifiers; 31 exhanst gas outlets; 32,33 regeneration standpipes; 34 heat collectors; 50 service hoisting pipe reactors; 52 catalyzer outlets.
Embodiment
Specify technical scheme of the present invention below in conjunction with accompanying drawing, but protection scope of the present invention includes, but are not limited to this:
Fig. 1 is a catalyst cracking method apparatus structure synoptic diagram of the present invention, and CCU comprises main reactor, service hoisting pipe reactor 50, settling vessel 20, stripping stage 22, revivifier 30 and catalyst make-up pipeline 15; Main reactor, service hoisting pipe reactor 50 shared settling vessels 20 are provided with oil gas vent 23 and 25 respectively separately; Main reactor comprises pre lift zone 16, riser reaction zone 11, catalyzer splitter 18, grid distributor 14 and second reaction zone 12 that is provided with from bottom to top; Second reaction zone, 12 diameters are 1.5-4.9 times of riser reaction zone 11 diameters, and grid distributor 14 is provided with a plurality of openings; Stripping stage 22 coaxial riser reaction zone 11 outsides that are arranged at, second reaction zone 12 is arranged on stripping stage 22 tops, with riser reaction zone 11 shared stripping stages 22; Be communicated with through catalyzer return line 21 between settling vessel 20 and the stripping stage 22, return line 21 is provided with guiding valve; Service hoisting pipe reactor 50 middle parts are provided with reclaimable catalyst outlet 52, and catalyst make-up pipeline 15 upper ends are communicated with catalyzer outlet 50, and the lower end is communicated with second reaction zone 12; Main reactor, service hoisting pipe reactor 50 are respectively arranged with feed nozzle 13 and 51; Be provided with regeneration standpipe 24 between stripping stage 22 and the revivifier 30, main reactor, service hoisting pipe reactor 50 and 30 of revivifiers are respectively equipped with regeneration standpipe 32 and 33; Revivifier 30 is provided with exhanst gas outlet 31 and heat collector 34; All corresponding gas distributor is set in stripping stage 22, the grid distributor 14 according to requirement of engineering.
The technical process of this catalyst cracking method is following:
In the main reactor; Regenerated catalyst from revivifier 30 gets in the pre lift zone 16 of main reactor along regeneration standpipe 32; In the lifting that promotes in advance steam entering riser reaction zone 11 down, with the raw oil contact reacts that sprays into from feed nozzle 13 of preheating, reaction mixture upwards flows in the splitter 18 along main reactor; Isolated catalyzer directly gets in the stripping stage 22 downwards; All the other catalyzer and reaction oil gas contact mixing with the reclaimable catalyst of the service hoisting pipe reactor of introducing through catalyst make-up pipeline 15 50 in grid distributor 14 evenly upwards gets into second reaction zone 12, carry out the gasoline upgrading reaction; Reaction finishes, and oil gas gets into settling vessel 20 with catalyzer to be separated, and oil gas gets into fractionating system through oil gas vent 23, and catalyzer then carries out stripping after regeneration standpipe 24 returns revivifier 30 regeneration along catalyzer return line 21 entering stripping stages 22;
In the service hoisting pipe reactor; Regenerated catalyst from revivifier 30 gets into service hoisting pipe reactor 50 bottoms along regeneration standpipe 33; The light hydrocarbon feedstocks that sprays into from feed nozzle 51 oil contact reacts with preheating; At service hoisting pipe reactor 50 middle parts, a part of reclaimable catalyst is drawn through catalyst make-up pipeline 15 through catalyzer outlet 52 and is replenished participation upgrading reaction in second reaction zone 12 that gets into main reactor, and all the other catalyzer and reaction oil gas continue along reactor drum 50 up reactions; Reaction finishes; Oil gas gets into settling vessel 20 with catalyzer to be separated, and oil gas gets into fractionating system through oil gas vent 25, and catalyzer then carries out stripping after regeneration standpipe 24 returns revivifier 30 regeneration along catalyzer return line 21 entering stripping stages 22.
Embodiment:
1,000,000 tons of/year gasoline upgrading CCUs of certain refinery comprise main reactor and subsidiary riser, the shared settling vessel of two reactor drums; Main reactor pre lift zone diameter 1.1m, height 5m, riser reaction zone diameter 1.4m; High 20.4m, the second reaction zone diameter 4.0m, high 19.5m; Stripping stage and the coaxial setting of riser reaction zone, diameter 4.2m highly is 8.9m; Subsidiary riser diameter 0.8m, subsidiary riser is provided with oil gas vent separately, and oil gas separates with main reactor oil gas and carries out subsequent disposal; The reclaimable catalyst of riser reaction zone has 22% to get into second reaction zone, and the reclaimable catalyst carbon content of second reaction zone is controlled at 0.5%; 520 ℃ of riser reaction zone temperature of reaction, reaction times 0.6s; 490 ℃ of the second reaction zone temperature of reaction, reaction times 3.2s; The reclaimable catalyst that adds to second reaction zone accounts for 65% of the second reaction zone total catalyst internal circulating load; Spray into the part quenched water in the second reaction zone bottom.
In the present embodiment, main reactor adopts distillate to mix refining 12% vacuum residuum; Subsidiary riser adopts C
4The lighter hydrocarbons charging, 63% is the main reactor product fraction, rest part installs from other.
The result shows, adopts identical reaction raw materials and reaction conditions, compares with existing heavy oil list riser reactor, and olefin(e) centent is reduced to below 26% in the main reactor product gasoline, and MON increases by 1.2, and sulphur content reduces.
It should be noted last that: above explanation is only unrestricted in order to explanation the present invention; Although the present invention is specified with reference to preferred embodiments; Those of ordinary skill in the art is to be understood that; Can make amendment or be equal to replacement the present invention, and not break away from the spirit and scope of the present invention, it all should be encompassed in the middle of the claim scope of the present invention.
Claims (7)
1. a catalyst cracking method is provided with main reactor and auxiliary reactor, and main reactor comprises the riser reaction zone of bottom and second reaction zone that upper diameter enlarges; In the main reactor; Reaction raw materials oil contacts with regenerated catalyst in riser reaction zone cracking reaction takes place; Oil gas that generates and catalyst reaction logistics are isolated a part of catalyzer in the riser reaction zone outlet; Oil gas and residual catalyst are up together, carry out the gasoline upgrading reaction at second reaction zone of enlarged-diameter, it is characterized in that:
⑴ participate in the gasoline upgrading reaction to the reclaimable catalyst that second reaction zone replenishes a part of auxiliary reactor; The reclaimable catalyst that replenishes is perhaps drawn from the auxiliary reactor middle part, perhaps behind auxiliary reactor outlet separation and stripping, draws, and the catalyst temperature that replenishes is below 550 ℃; Said second reaction zone is a fast fluidized bed, and the gas phase flow velocity is 1.2-5.0m/s;
⑵ be provided with grid distributor in the riser reaction zone and second reaction interval, and grid distributor is provided with opening or passage; Be provided with the catalyzer splitter in the riser reaction zone outlet, the coaxial catalyst stripping section that is provided with in the riser reaction zone outside, second reaction zone is arranged on the stripping stage top;
⑶ participate in the main reactor catalyst for reaction and divide two-way to get into the main reaction part; First via catalyzer is directly from the regenerated catalyst of revivifier or through the regenerated catalyst after the cooling; Regenerated catalyst is introduced into the pre lift zone of riser reaction zone raw oil nozzle bottom; With the reaction raw materials contact reacts, reaction is isolated a part of catalyzer after accomplishing in the catalyzer splitter, and catalyzer of not shunted and reaction oil gas upwards get into second reaction zone through grid distributor together; The second road catalyzer is said additional reclaimable catalyst, and the second tunnel catalyst make-up gets into second reaction zone, and carries out the upgrading reaction after above-mentioned catalyzer and reaction oil gas logistics mix.
2. catalyst cracking method according to claim 1 is characterized in that: the shared stripping stage of the reclaimable catalyst of two reaction zones of main reactor reactive moieties, the catalyzer behind the stripping gets into revivifier regeneration through standpipe.
3. catalyst cracking method according to claim 1; It is characterized in that: the reacted reclaimable catalyst of second reaction zone partly returns in second reaction zone; The part reclaimable catalyst is circulated at second reaction zone, increase the catalyzer agent-oil ratio of second reaction zone or reduce reaction velocity.
4. catalyst cracking method according to claim 1 is characterized in that: the 0-80% of the reclaimable catalyst after the said riser reaction zone cracking reaction gets into second reaction zone and participates in the upgrading reaction.
5. catalyst cracking method according to claim 1 is characterized in that: the riser reaction zone reaction conditions does, 500 ℃-620 ℃ of temperature of reaction, and reaction times 0.2-1.6s, oil gas mean flow rate are 5.0 ~ 26m/s; The second reaction zone reaction conditions does, 450 ℃-510 ℃ of temperature of reaction, and reaction times 2.0-5.0s, oil gas mean flow rate are 1.2-4.0m/s, preferred 3.0-3.5m/s.
6. catalyst cracking method according to claim 1 is characterized in that: auxiliary reactor is a riser reactor, and reaction raw materials is C
4One or more of the lighter hydrocarbons that component, catalytic gasoline, coker gasoline, petroleum naphtha are such; The shared settling vessel of auxiliary reactor and main reactor.
7. realize the described catalyst cracking method of claim 1, it is characterized in that: the 1.5-4.9 that said second reaction zone diameter is the riser reaction zone diameter times, preferred 2.0-3.5 doubly.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110240932A (en) * | 2018-05-29 | 2019-09-17 | 石宝珍 | A kind of petroleum hydrocarbon multi-stage fluidized catalytic reaction method and reactor |
| CN113926390A (en) * | 2020-07-13 | 2022-01-14 | 中国石油化工股份有限公司 | Catalytic conversion reactor, catalytic conversion device and method for preparing propylene by catalytic cracking of heavy oil |
| CN113926396A (en) * | 2020-07-13 | 2022-01-14 | 中国石油化工股份有限公司 | Heavy oil catalytic conversion reactor and method for preparing propylene by heavy oil catalytic cracking |
| WO2024139528A1 (en) * | 2022-12-30 | 2024-07-04 | 中国石油天然气股份有限公司 | Heavy oil catalysis device and method |
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| CN201901660U (en) * | 2010-12-02 | 2011-07-20 | 石宝珍 | Catalytic cracking unit |
| CN201962247U (en) * | 2011-01-27 | 2011-09-07 | 青岛京润石化设计研究院有限公司 | Catalytic cracking device |
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2011
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| EP1046696A2 (en) * | 1999-04-23 | 2000-10-25 | China Petrochemical Corporation | A catalytic conversion process for producing isobutane and isoparaffin-enriched gasoline |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110240932A (en) * | 2018-05-29 | 2019-09-17 | 石宝珍 | A kind of petroleum hydrocarbon multi-stage fluidized catalytic reaction method and reactor |
| US11578274B2 (en) | 2018-05-29 | 2023-02-14 | Qingdao Jingrun Petrochemical Design Institute Co., Ltd. | Multi-stage fluidized catalytic reaction process of petroleum hydrocarbons and an apparatus thereof |
| CN113926390A (en) * | 2020-07-13 | 2022-01-14 | 中国石油化工股份有限公司 | Catalytic conversion reactor, catalytic conversion device and method for preparing propylene by catalytic cracking of heavy oil |
| CN113926396A (en) * | 2020-07-13 | 2022-01-14 | 中国石油化工股份有限公司 | Heavy oil catalytic conversion reactor and method for preparing propylene by heavy oil catalytic cracking |
| CN113926390B (en) * | 2020-07-13 | 2022-12-13 | 中国石油化工股份有限公司 | Catalytic conversion reactor, catalytic conversion device and method for preparing propylene by catalytic cracking of heavy oil |
| CN113926396B (en) * | 2020-07-13 | 2022-12-13 | 中国石油化工股份有限公司 | Heavy oil catalytic conversion reactor and method for preparing propylene by heavy oil catalytic cracking |
| WO2024139528A1 (en) * | 2022-12-30 | 2024-07-04 | 中国石油天然气股份有限公司 | Heavy oil catalysis device and method |
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