CN105885930A - Multifunctional residual oil catalytic cracking method and device - Google Patents

Abstract

The invention discloses a multifunctional residual oil catalytic cracking method and belongs to the technical field of petrochemical engineering and resource utilization. The method comprises the steps of regenerant and residual oil feeding, residual oil and regenerant mixing, vaporization, cracking and conversion. The method is characterized in that a high-activity low-temperature catalyst is introduced to the middle of a main reactor to achieve catalyst activity improvement and temperature reduction of the rear portion, and then hydrogen transfer, isomerization and aromatization of the rear portion are promoted; furthermore, the catalyst to oil ratio of the front portion and the temperature of the feeding stage are increased, so that initial cracking and vaporization of residual oil are promoted and high-temperature short-contact time cracking is achieved; an auxiliary reactor is arranged to guide a regenerant from a regenerator to be lifted by gasoline, so that cracking conversion reaction is conducted, and a high-activity spent catalyst which is 300-550 DEG C is conveyed to the middle of the main reactor. The invention further provides a residual oil catalytic cracking device comprising the main reactor and the auxiliary reactor for realizing the method. By the adoption of the method and device, residual oil conversion capacity can be improved remarkably, gasoline quality can be improved, and the yield of propylene, gasoline and light aromatics is high.

Description

A kind of multi-functional method for catalytic cracking residue and device

Technical field

The invention belongs to petrochemical industry, technical field of resource utilization, particularly to a kind of multi-functional method for catalytic cracking residue and dress Put.

Background technology

Along with the overseas crude oil day by day of petroleum resources is more and more heavier, catalytically cracked material is more and more heavier.Catalytic cracking process is weight Matter oil occurs gas-solid catalysis cracking reaction to generate light oil process on a catalyst.Catalytic cracking unit heavy raw oil is after atomization Enter bottom riser reactor, contact with high temperature regeneration agent and first carry out that heavy raw oil is original cracking, vaporize, send out the most again Angry solid catalytic cracking reaction, reaction oil gas and spent agent flow out from riser reactor outlet, reaction oil gas after gas solid separation Discharging reactor, spent agent goes regenerator to regenerate.Owing to catalytic cracking primary response is the endothermic reaction and has a large amount of coke to generate (coke Be deposited on catalyst surface), thus in riser reactor along with oil gas flow up temperature, catalyst activity gradually reduces, The oil ratio of reactor is determined by reactor thermal balance.Generally there are 2 problems in RFCC riser reactor at present: 1, Oil ratio is on the low side does not reaches optimization requirement, and catalytic reaction process catalyst activity is on the low side, more than heavy oil nozzle is catalyzed at 1/3 length Agent activity only has the 1/2 of initial activity, and at 1/2 length, catalyst activity is less than the 1/3 of initial activity, 1/2 length after riser Inside carrying out under low catalyst activity, substantial deviation optimizes reaction condition.2, higher than outlet temperature bottom riser reactor 20～30 DEG C, requirement can be met during wax oil raw material, but heavy raw oil boiling point increases substantially, make major part mink cell focus vaporization , do not exist with non-vaporization gasoline form, cause device coking yield to raise, even make riser reactor, settler coking.Closely The heavy oil catalytically cracking equipment that phase has have employed regenerative agent cooling measure, applies this technical measures rear catalyst circulating load to increase, carries High oil ratio, course of reaction catalyst activity, but in the case of outlet temperature is constant, riser bottom temp reduces further, then Raw agent temperature and riser bottom temp reduce simultaneously to heavy raw oil (especially poor residuum) original cracking, vaporize unfavorable, Dealing with improperly when processing poor residuum to cause coking yield to raise on the contrary.Additionally petrochemical enterprise also have processing coked waxy oil, The demands such as producing more propylene, fecund gasoline and raising quality of gasoline.

Summary of the invention

It is an object of the invention to provide a kind of multi-functional method for catalytic cracking residue, make the catalyst activity raising of reactor rear portion, temperature Degree reduces and promotes rear portion hydrogen migration, isomerization, aromatisation conversion reaction, and improves reactor front portion cracking zone oil ratio and charging Section mixing temperature.Improve poor residuum conversion capability, improve quality of gasoline, and also can with processing coked waxy oil, producing more propylene, Fecund gasoline.

The present invention solves the method that its technical problem used: include that regenerative agent, residual oil enter, residual oil mixes with regenerative agent, Vaporization, cracking and after convert, it is characterized in that: in the middle part of main reactor, fill into high activity low temperature catalyst, make rear portion catalyst live Property improve, temperature reduce, promote rear portion hydrogen migration, isomerization, aromatization；And improve anterior oil ratio and feed zone temperature Degree, promotes residual oil original cracking and vaporization realizes high temperature short contact cracking；Auxiliary reactor is set from regenerator or cooler or treatment with external measures Hot device draws regenerative agent, promotes through gasoline, light cycle oil, C4～C6 alkene, cracking, conversion reaction by 300～550 DEG C occur High activity spent agent is transported in the middle part of main reactor；Fast bed mixing section is set at main reactor rear portion, makes main side effect device to be generated Agent and air-fuel mixture uniformly carry out conversion reaction；Improve crude conversion ability, improve quality of gasoline, producing more propylene, fecund gasoline And light aromatic hydrocarbons.

Further, it is also possible to sharp separation facility is set in auxiliary reactor outlet, 300～550 DEG C of high activities of separation and recovery are treated Raw agent directly or is transported in the middle part of main reactor after cooling.

Further, it is also possible to wax tailings adsorption section and wax tailings charging are set in the middle part of main reactor.

A kind of multi-functional residue fluid catalytic cracking unit, including regenerator, external warmer, main regenerative agent pipe, main pre-riser, master Riser, heavy oil nozzle, fast bed, secondary regenerative agent pipe, secondary pre-riser, secondary riser, nozzle；Main regenerative agent pipe upper end Being connected with regenerator, lower end is connected with main pre-riser, and main riser bottom is provided with heavy oil nozzle, under upper end is connected with fast bed End is connected with main pre-riser；Secondary regenerative agent pipe upper end and regenerator or cooler or external warmer are connected, lower end and pair pre-lift Device connects, and secondary riser is provided with gasoline, dry gas nozzle, and lower end is connected with secondary pre-riser upper end, and upper end folds and main riser Upper end or fast bed lower end connect.

Further, it is also possible in secondary riser bottom, light cycle oil nozzle is set, it is also possible to expansion is set in secondary riser bottom straight Footpath conversion zone and C4～C6 alkene nozzle.

Further, it is also possible on secondary riser top, secondary fast bed is set, it is also possible at secondary pre-riser, heat removing tube is set.

Further, it is also possible to arranging secondary fast point, secondary stripping section or secondary storing section, secondary spent agent pipe, secondary riser upper end is fast with pair Point connecting, secondary fast point of lower end be connected with secondary stripping section or secondary storing section, secondary spent agent pipe upper end with under pair stripping section or pair storing section Portion connects, and lower end is connected with main riser upper end or fast bed lower end.

Further, it is also possible at secondary stripping section or secondary storing section, heat removing tube is set.

Further, it is also possible to wax tailings nozzle is set on main riser top, it is also possible to heat removing tube is set at fast bed.

Innovative point of the present invention and good effect:

Innovative point of the present invention is: fill into high activity low temperature catalyst in the middle part of main reactor, makes rear portion catalyst activity raising, temperature Degree reduces, and promotes rear portion hydrogen migration, isomerization, aromatization；And improve anterior oil ratio and feed zone temperature, promote slag Oil is original cracking and vaporization realizes high temperature short contact cracking；Auxiliary reactor is set and draws regeneration from regenerator or cooler or external warmer Agent, promotes through gasoline, light cycle oil, C4～C6 alkene, cracking, conversion reaction by be generated for 300～550 DEG C of high activities occurs Agent is transported in the middle part of main reactor；Fast bed mixing section is set at main reactor rear portion, makes main side effect device spent agent and oil gas mix Close and uniformly carry out conversion reaction.

Good effect of the present invention is: 1, significantly improves poor residuum conversion capability, improve quality of gasoline.2, coking wax can be processed Oil, it is to avoid nitride is to catalyst adverse effect and settler coking problem.3, producing more propylene, fecund gasoline and light aromatic hydrocarbons.

Accompanying drawing explanation

Fig. 1 is a kind of multi-functional method for catalytic cracking residue and device schematic diagram.

1-outlet, 2-fast bed, 3-allotter, 4-connecting tube, the main riser of 5-, 6-residual oil nozzle, 6A-recycle oil nozzle, The main pre-riser of 7-, 8-main regenerative agent pipe, 9-main regeneration guiding valve, 10-pair riser, 11-petrol jet, 13-pair lifter, 14-pair regenerative agent pipe, 15-pair regeneration guiding valve, 16-dry gas ozzle, 17-heat removing tube, 20-thermal regenerant pipe, 21A-cooler, 23-regenerator.

Fig. 2 is another kind of multi-functional method for catalytic cracking residue and device schematic diagram.

1-outlet, 2-fast bed, 3-allotter, 4-connecting tube, the main riser of 5-, 5A-adsorption section, 6-residual oil nozzle, 6A- Recycle oil nozzle, 6B-wax tailings nozzle, the main pre-riser of 7-, 8-main regenerative agent pipe, 9-main regeneration guiding valve, 10-pair promotes Pipe, 11-petrol jet, the light component nozzle of 12-diesel oil, 13-pair lifter, 14-pair regenerative agent pipe, 15-pair regeneration guiding valve, 16- Dry gas ozzle, 17-heat removing tube, 20-thermal regenerant pipe, 21-external warmer, 22-low temperature agent recurrent canal, 23-regenerator.

Fig. 3 is another kind of multi-functional method for catalytic cracking residue and device schematic diagram.

1-outlet, 2-fast bed, 3-allotter, 4-connecting tube, the main riser of 5-, 5A-adsorption section, 6-residual oil nozzle, 6A- Recycle oil nozzle, 6B-wax tailings nozzle, the main pre-riser of 7-, 8-main regenerative agent pipe, 9-main regeneration guiding valve, 10-pair promotes Pipe, 11-petrol jet, the light component nozzle of 12-diesel oil, 13-pair lifter, 14-pair regenerative agent pipe, 15-pair regeneration guiding valve, 16- Dry gas ozzle, 17-heat removing tube, 18-conversion zone, 19-C4～C6 alkene nozzle, 20-thermal regenerant pipe, 21-external warmer, 22-low temperature agent recurrent canal, 23-regenerator.

Fig. 4 is another kind of multi-functional method for catalytic cracking residue and device schematic diagram.

1-outlet, 2-fast bed, 3-allotter, 4A-pair spent agent pipe, the main riser of 5-, 6-residual oil nozzle, 6A-freshening Oil burner nozzle, the main pre-riser of 7-, 8-main regenerative agent pipe, 9-main regeneration guiding valve, 10-pair riser, 11-petrol jet, 12- The light component nozzle of diesel oil, 13-pair lifter, 14-pair regenerative agent pipe, 15-pair regeneration guiding valve, 16-dry gas ozzle, 17-heat removing tube, 23-regenerator, 24-settler, secondary fast point of 25-, 26-pair stripping section or secondary storing section.

Fig. 5 is another kind of multi-functional method for catalytic cracking residue and device schematic diagram.

1-outlet, 2-fast bed, 3-allotter, 4A-pair spent agent pipe, the main riser of 5-, 5A-adsorption section, 6-residual oil sprays Mouth, 6A-recycle oil nozzle, 6B-wax tailings nozzle, the main pre-riser of 7-, 8-main regenerative agent pipe, 9-main regeneration guiding valve, 10- Secondary riser, 11-petrol jet, the light component nozzle of 12-diesel oil, 13-pair lifter, 14-pair regenerative agent pipe, the regeneration of 15-pair is sliding Valve, 16-dry gas ozzle, 17-heat removing tube, 18-conversion zone, 19-C4～C6 alkene nozzle, 23-regenerator, 25A-pair eddy flow Device, 25B-pair seal closure, 26-pair stripping section or secondary storing section.

Detailed description of the invention

Seeing that Fig. 1, main riser 5 bottom are provided with residual oil nozzle 6 and recycle oil nozzle 6A, lower end is with main pre-riser 7 upper end even Connecing, upper end is connected with fast bed 2 lower end；Being provided with allotter 3 in fast bed 2, its upper end is connected with outlet 1 lower end.Main Regenerative agent pipe 8 bottom is provided with main regeneration guiding valve 9, and its lower end is connected with main pre-riser 7, and upper end is connected with regenerator 23.Secondary Riser 10 bottom is provided with petrol jet 11, and upper end is connected with fast bed 2 bottom through connecting tube 4, lower end and secondary lifter 13 Upper end connects, and secondary lifter 13 bottom is provided with dry gas ozzle 16.Being provided with heat removing tube 17 in cooler 21A, top is by heat again Raw agent pipe 20 is connected with regenerator 23, and bottom is connected with secondary lifter 13 by secondary regenerative agent pipe 14, secondary regeneration guiding valve 15.

Seeing that Fig. 2, main riser 5 bottom are provided with residual oil nozzle 6 and recycle oil nozzle 6A, lower end is with main pre-riser 7 upper end even Connecing, upper end is connected with adsorption section 5A lower end；Adsorption section 5A bottom is provided with wax tailings nozzle 6B, upper end and fast bed 2 lower end Connect；Being provided with allotter 3 in fast bed 2, upper end is connected with outlet 1 lower end.Main regenerative agent pipe 8 bottom is provided with main regeneration Guiding valve 9, lower end is connected with main pre-riser 7, and upper end is connected with regenerator 23.Secondary riser 10 be provided with petrol jet 11, The light component nozzle of diesel oil 12, upper end is connected with fast bed 2 bottom through connecting tube 4, and lower end is connected with secondary lifter 13 upper end, Secondary lifter 13 bottom is provided with dry gas ozzle 16.Being provided with heat removing tube 17 in external warmer 21, thermal regenerant pipe 20 is passed through on top Being connected with regenerator 23, bottom is connected with secondary lifter 13 by secondary regenerative agent pipe 14, secondary regeneration guiding valve 15, passes through simultaneously Low temperature agent recurrent canal 22 is connected with regenerator 23.

Seeing that Fig. 3, main riser 5 bottom are provided with residual oil nozzle 6 and recycle oil nozzle 6A, lower end is with main pre-riser 7 upper end even Connecing, its upper end is connected with adsorption section 5A lower end.Adsorption section 5A bottom is provided with wax tailings nozzle 6B, adsorption section 5A upper end with Fast bed 2 lower end connects；Being provided with allotter 3 in fast bed 2, its upper end is connected with outlet 1 lower end.Main regenerative agent pipe 8 Bottom is provided with main regeneration guiding valve 9, and lower end is connected with main pre-riser 7, and upper end is connected with regenerator 23.Secondary riser 10 sets Having the light component nozzle of petrol jet 11, diesel oil 12, upper end is connected with fast bed 2 bottom through connecting tube 4, lower end and conversion zone 18 upper ends connect.Conversion zone 18 is provided with C4～C6 alkene nozzle 19, and lower end is connected with secondary lifter 13 upper end, secondary lifter 13 bottoms are provided with dry gas ozzle 16.Being provided with heat removing tube 17 in external warmer 21, thermal regenerant pipe 20 and regenerator are passed through in top 23 connect, and bottom is connected with secondary lifter 13 by secondary regenerative agent pipe 14, secondary regeneration guiding valve 15, is returned by low temperature agent simultaneously Pipe 22 is connected with regenerator 23.

Seeing that Fig. 4, main riser 5 bottom are provided with residual oil nozzle 6 and recycle oil nozzle 6A, lower end is with main pre-riser 7 upper end even Connecing, upper end is connected with fast bed 2 lower end.Being provided with allotter 3 in fast bed 2, its upper end is connected with outlet 1 lower end.Main Regenerative agent pipe 8 bottom is provided with main regeneration guiding valve 9, and lower end is connected upper end with main pre-riser 7 and is connected with regenerator 23.Secondary lifting Pipe 10 bottom is provided with petrol jet 11 or the light component nozzle of diesel oil 12, and upper end folds divides 25 to be connected with pair soon；Lower end carries with pair Rising device 13 upper end to connect, secondary lifter 13 bottom is provided with dry gas ozzle 16；Secondary regenerative agent pipe 14 bottom is provided with secondary regeneration guiding valve 15, lower end is connected upper end with secondary lifter 13 and is connected with regenerator 23.Settler 24 lower end and secondary stripping section or secondary storing section 26 (inside is provided with heat removing tube 17) upper end connects；Secondary spent agent pipe 4A upper end is connected with secondary stripping section or secondary storing section 26, lower end It is connected with bottom fast bed 2.

Seeing that Fig. 5, main riser 5 bottom are provided with residual oil nozzle 6 and recycle oil nozzle 6A, lower end is with main pre-riser 7 upper end even Connecing, its upper end is connected with adsorption section 5A lower end, and adsorption section 5A bottom is provided with wax tailings nozzle 6B, adsorption section 5A upper end with Fast bed 2 lower end connects；Being provided with allotter 3 in fast bed 2, its upper end is connected with outlet 1 lower end.Main regenerative agent pipe 8 Bottom is provided with main regeneration guiding valve 9, and lower end is connected upper end with main pre-riser 7 and is connected with regenerator 23.Secondary riser 10 bottom Being provided with petrol jet 11 or the light component nozzle of diesel oil 12, upper end reaches the internal and secondary cyclone 25A of secondary seal closure 25B and is connected, Secondary seal closure 25B lower end is connected with secondary stripping section or secondary storing section 26 (inside is provided with heat removing tube 17) upper end；Secondary spent agent pipe 4A Upper end is connected with secondary stripping section or secondary storing section 26, and lower end is connected bottom fast bed 2.Conversion zone 18 is provided with C4～C6 alkene Nozzle 19, upper end is connected with secondary riser 10 lower end, and lower end is connected with secondary lifter 13 upper end, and secondary lifter 13 bottom sets There is dry gas ozzle 16.Secondary regenerative agent pipe 14 bottom is provided with secondary regeneration guiding valve 15, and lower end is connected upper end and regeneration with secondary lifter 13 Device 23 connects.

Seeing Fig. 1,680～730 DEG C of high temperature regeneration agent are drawn from regenerator 23 and are entered cooler 21A through thermal regenerant pipe 20, with Heat removing tube 17 heat-exchange temperature drops to 300～680 DEG C, enters secondary lifter 13 through secondary regenerative agent pipe 14, secondary regeneration guiding valve 15. Entering dry gas medium at dry gas ozzle 16, regenerative agent is promoted to secondary riser 10 bottom, external high olefin gasolines sprays through gasoline Enter after mouth 11 atomization, mix, vaporize and occur Olefin decrease conversion reaction with regenerative agent, control reaction temperature 300～450 DEG C, Reaction gas and high activated catalyst flow up, and flow out from secondary riser 10 upper end and enter fast bed 2 bottom through connecting tube 4. 680～730 DEG C of high temperature regeneration agent enter main pre-riser 7 through main regenerative agent pipe 8, main regeneration guiding valve 9, are promoted to main riser 5 Bottom, residual oil enters after residual oil nozzle 6 is atomized, and recycle oil enters after recycle oil nozzle 6A is atomized, and mixes with high temperature regeneration agent Close original cracking, vaporization, catalytic cracking reaction, control reaction temperature 510～530 DEG C, make mink cell focus be cracked into light-end products, Generate dry gas simultaneously and coke, reaction oil gas and catalyst flow up and flow out from main riser 5 upper end, with secondary riser 10 The mixing of 300～450 DEG C of high activated catalysts, control after mixing temperature 470～515 DEG C, after mixing oil gas and catalyst continue to Upper influencing meridian allotter 3 enters fast bed 2, and in fast bed 2, mix homogeneously promotes that hydrogen migration, isomerization, aromatisation etc. are anti- Should, final reaction oil gas and catalyst flow out from fast bed 2 upper end discharges through outlet 1.The program has the advantage that 1, Improve slag oil cracking section oil ratio, feed zone temperature, improve crude conversion ability, reduce green coke, raising product yield；2, carry Gao Quan factory quality of gasoline.

Seeing Fig. 2,680～730 DEG C of high temperature regeneration agent are drawn from regenerator 23 and are entered external warmer 21 through thermal regenerant pipe 20, Dropping to 500～680 DEG C with heat removing tube 17 heat-exchange temperature, a part enters secondary lifting through secondary regenerative agent pipe 14, secondary regeneration guiding valve 15 Device 13, another part returns regenerator 23 through low temperature agent recurrent canal 22.Dry gas medium is entered, by regenerative agent at dry gas ozzle 16 Being promoted to secondary riser 10 bottom, the light component of diesel oil enters after diesel oil light component nozzle 12 is atomized, and mixes with regenerative agent, vapour Change, control reaction temperature 450～550 DEG C and light for diesel oil component is cracked into gasoline, reaction gas and catalyst flows up into middle part. High olefin gasolines enters after petrol jet 11 is atomized, and controls reaction temperature 350～450 DEG C and carries out Olefin decrease conversion reaction, so Rear reaction gas and high activated catalyst continue up flowing and enter fast bed 2 bottom from the outflow of secondary riser 10 upper end through connecting tube 4. 680～730 DEG C of high temperature regeneration agent enter main pre-riser 7, the main lifting of boosted entrance through main regenerative agent pipe 8, main regeneration guiding valve 9 Pipe 5 bottom, residual oil enters after residual oil nozzle 6 is atomized, and recycle oil enters after recycle oil nozzle 6A is atomized, with high temperature regeneration Agent mixing is original cracking, vaporization, catalytic cracking reaction, control reaction temperature 510～530 DEG C, make mink cell focus be cracked into lightweight and produce Product, generate dry gas simultaneously and coke, reaction oil gas and low activity spent agent travel up to adsorption section 5A.Wax tailings is through coking Wax oil nozzle 6B atomization after enter, in adsorption section 5A high temperature low activity spent agent make wax tailings be heated vaporization and to nitride Adsorbing, then reaction oil gas and low activity spent agent continue up and flow into bottom fast bed 2, with secondary riser 10 The mixing of 350～450 DEG C of high activated catalysts, control mixing temperature 470～515 DEG C, mixed oil and gas and catalyst continue up stream Influencing meridian allotter 3 enters fast bed 2 bottom, and in fast bed 2, mix homogeneously carries out cracking to wax tailings fraction, and promotes Hydrogen migration, isomerization, aromatisation etc. are reacted, and last oil gas and spent agent flow out from fast bed 2 upper end discharges through outlet 1. The program has the advantage that 1, improves slag oil cracking section oil ratio, feed zone temperature, improves crude conversion ability, reduces life Burnt, raising product yield；2, improve wax tailings conversion capability, reduce nitride to the murder by poisoning of catalyst, avoid settler to tie Jiao, reduces green coke, improves product yield；3, improve gasoline yield, improve quality of gasoline.

Seeing Fig. 3,680～730 DEG C of high temperature regeneration agent are drawn from regenerator 23 and are entered external warmer 21 through thermal regenerant pipe 20, Dropping to 600～680 DEG C with heat removing tube 17 heat-exchange temperature, a part enters secondary lifting through secondary regenerative agent pipe 14, secondary regeneration guiding valve 15 Device 13, another part returns regenerator 23 through low temperature agent recurrent canal 22.Dry gas medium is entered, by regenerative agent at dry gas ozzle 16 Being promoted to conversion zone 18, C4～C6 alkene enters through C4～C6 alkene nozzle, with regenerative agent mixed-controlled reaction temperature 550～620 DEG C C4～C6 alkene converts and produces propylene, and reaction gas and catalyst mixture flow up into secondary riser 10 bottom.Light group of diesel oil Lease making diesel oil light component nozzle 12 atomization after enter, mix with regenerative agent, vaporize, control reaction temperature 450～550 DEG C by bavin The light component of oil is cracked into gasoline, reaction gas and catalyst and flows up into middle part.High olefin gasolines is after petrol jet 11 is atomized Entering, control reaction temperature 350～450 DEG C and carry out Olefin decrease conversion reaction, then reaction gas and high activated catalyst continue up Flow to flow out from secondary riser 10 upper end and enter fast bed 2 bottom through connecting tube 4.680～730 DEG C of high temperature regeneration agent are through main regeneration Agent pipe 8, main regeneration guiding valve 9 enter main pre-riser 7, and boosted entrance main riser 5 bottom, residual oil is through residual oil nozzle 6 mist Entering after change, recycle oil enters after recycle oil nozzle 6A is atomized, mix with high temperature regeneration agent original cracking, vaporize, be catalyzed and split Change reaction, control reaction temperature 510～530 DEG C, make mink cell focus be cracked into light-end products, generate dry gas and coke, reaction simultaneously Oil gas and low activity spent agent travel up to adsorption section 5A.Wax tailings enters after wax tailings nozzle 6B is atomized, and is inhaling Contacting with high temperature low activity spent agent in attached section of 5A, wax tailings is heated and vaporizes and adsorb nitride, then reaction oil gas And low activity spent agent continues up and flows into bottom fast bed 2, urge with 350～450 DEG C of high activities of secondary riser 10 Agent mixes, control mixing temperature 470～515 DEG C, and mixed oil and gas and catalyst continue up the allocated device 3 of flowing and enter quickly Bed 2 bottoms, in fast bed 2, mix homogeneously carries out cracking to wax tailings fraction, and promotes hydrogen migration, isomerization, aromatization The reactions such as change, last oil gas and spent agent flow out from fast bed 2 upper end discharges through outlet 1.Have the advantage that 1, improve Slag oil cracking section oil ratio, feed zone temperature, improve crude conversion ability, reduce green coke, raising product yield；2, Jiao is improved Change wax oil conversion capability, reduce nitride to the murder by poisoning of catalyst, avoid settler coking；3, quality of gasoline is improved；4, many Produce propylene, gasoline.

Seeing Fig. 4,680～730 DEG C of high temperature regeneration agent draw to enter through secondary regenerative agent pipe 14, secondary regeneration guiding valve 15 from regenerator 23 Enter secondary lifter 13.Enter dry gas medium at dry gas ozzle 16 and high temperature regeneration agent is promoted to secondary riser 10 bottom, high alkene Gasoline enters (or/and the light component of diesel oil enters after diesel oil light component nozzle 12 is atomized) after petrol jet 11 is atomized, with high temperature Regenerative agent mixes, vaporizes and occur cracking reaction, control reaction temperature 400～550 DEG C, makes the light component of part diesel oil be converted into vapour Oil (or/and high olefin gasolines changes into propylene), reaction gas and catalyst flow up, and exit into from secondary riser 10 upper end Secondary fast point 25, dividing soon in pair and carry out primary centrifuge separation in 25, the secondary spent agent separated falls into secondary stripping section or the pair of lower section Storing section 26, secondary spent agent makes temperature be reduced to 350～450 DEG C with heat removing tube 17 heat-shift therein, by secondary spent agent Pipe 4A is transported to bottom fast bed 2.680～730 DEG C of high temperature regeneration agent enter main pre-through main regenerative agent pipe 8, main regeneration guiding valve 9 Lifter 7, is promoted to main riser 5 bottom, and residual oil enters after residual oil nozzle 6 is atomized, and recycle oil is through recycle oil nozzle 6A Enter after atomization, mix original cracking, vaporization, catalytic cracking reaction with high temperature regeneration agent, control reaction temperature 510～530 DEG C, Make mink cell focus be cracked into light-end products, generate dry gas simultaneously and coke, reaction oil gas and spent agent flow up from main riser 5 Upper end is flowed out, and mixes with 350～450 DEG C of high activated catalysts of secondary riser 10, makes the activity raising of mixed catalyst, And control temperature 470～515 DEG C after mixing, after mixing, oil gas and spent agent continue up the allocated device 3 of flowing and enter fast bed 2, Spent agent mix homogeneously completes the reactions such as hydrogen migration, isomerization, aromatisation, and final reaction oil gas and spent agent are from fast bed 2 Upper end is flowed out and is discharged through outlet 1.The program has the advantage that 1, improves slag oil cracking section oil ratio, feed zone temperature, Improve crude conversion ability, reduce green coke, raising product yield；2, quality of gasoline is improved；3, producing more propylene, gasoline.

Seeing Fig. 5,680～730 DEG C of high temperature regeneration agent draw to enter through secondary regenerative agent pipe 14, secondary regeneration guiding valve 15 from regenerator 23 Enter secondary lifter 13.Enter dry gas medium at dry gas ozzle 16 and high temperature regeneration agent is promoted to conversion zone 18, C4～C6 alkene warp C4～C6 alkene nozzle enters, and mix and control reaction temperature 550～620 DEG C with high temperature regeneration agent, C4～C6 alkene converts gives birth to Producing propylene, reaction gas and catalyst mixture flow up into secondary riser 10 bottom.High olefin gasolines is through petrol jet 11 mist (or/and the light component of diesel oil enters after diesel oil light component nozzle 12 is atomized) is entered after change, mix with 550～620 DEG C of regenerative agents, Vaporize and occur cracking reaction, control reaction temperature 400～550 DEG C, make the light component of part diesel oil be converted into gasoline, high alkene vapour Oil changes into propylene, reaction gas and catalyst and continues up flowing, exits into secondary cyclone 25A from secondary riser 10 upper end, Carrying out primary centrifuge separation inside secondary seal closure 25B, the secondary spent agent separated falls into the secondary stripping section of lower section or secondary storing Section 26, secondary spent agent makes temperature be reduced to 350～450 DEG C with heat removing tube 17 heat-shift therein, by secondary spent agent pipe 4A is transported to bottom fast bed 2.680～730 DEG C of high temperature regeneration agent enter master carry in advance through main regenerative agent pipe 8, main regeneration guiding valves 9 Rising device 7, boosted entrance main riser 5 bottom, residual oil enters after residual oil nozzle 6 is atomized, and recycle oil is through recycle oil nozzle Enter after 6A atomization, mix original cracking, vaporization, catalytic cracking reaction with high temperature regeneration agent, control reaction temperature 510～530 DEG C, Make mink cell focus be cracked into light-end products, generate dry gas simultaneously and coke, reaction oil gas and low activity spent agent travel up to absorption Section 5A.Wax tailings enters after wax tailings nozzle 6B is atomized, and contacts with high temperature low activity spent agent in adsorption section 5A, Wax tailings is heated and vaporizes and adsorb nitride, and then reaction oil gas and spent agent continue up and flow into fast bed 2 Bottom, mixes with 350～450 DEG C of high activated catalysts of secondary riser 10, makes the activity raising of mixed catalyst, and controls Temperature 470～515 DEG C after system mixing, oil gas and mixed catalyst continue up the allocated device 3 of flowing and enter fast bed 2 bottom, Wax tailings fraction is carried out by catalyst mix homogeneously cracking, and promotes the reactions such as hydrogen migration, isomerization, aromatisation, finally Oil gas and spent agent flow out from fast bed 2 upper end discharges through outlet 1.Have the advantage that 1, improve slag oil cracking section agent oil Ratio, feed zone temperature, improve crude conversion ability, reduce green coke, raising product yield；2, improve wax tailings conversion capability, Reduce nitride to the murder by poisoning of catalyst, avoid settler coking；3, quality of gasoline is improved；4, producing more propylene, gasoline.

Claims (9)

1. a multi-functional method for catalytic cracking residue, enters including regenerative agent, residual oil, residual oil mixes with regenerative agent, vaporizes, Cracking and after convert, it is characterized in that: in the middle part of main reactor, fill into high activity low temperature catalyst, make rear portion catalyst activity improve, Temperature reduces, and promotes rear portion hydrogen migration, isomerization, aromatization；And improve anterior oil ratio and feed zone temperature, promote Residual oil is original cracking and vaporization realizes high temperature short contact cracking；Auxiliary reactor is set and draws regenerative agent, warp from regenerator or external warmer Gasoline, light cycle oil, C4～C6 alkene promote, and cracking, conversion reaction occur and is carried by 300～550 DEG C of high activity spent agents In the middle part of main reactor；Fast bed mixing section is set at main reactor rear portion, makes main side effect device spent agent and air-fuel mixture uniform Carry out conversion reaction；Improve crude conversion ability, improve quality of gasoline, producing more propylene, fecund gasoline and light aromatic hydrocarbons.

Method the most according to claim 1, is characterized in that: can also arrange sharp separation facility in auxiliary reactor outlet, 300～550 DEG C of high activity spent agents of separation and recovery directly or are transported in the middle part of main reactor after cooling.

Method the most according to claim 1, is characterized in that: can with arrange in the middle part of main reactor wax tailings adsorption section and Wax tailings feeds.

4. a multi-functional residue fluid catalytic cracking unit, including regenerator, external warmer, main regenerative agent pipe, main pre-riser, Main riser, heavy oil nozzle, fast bed, secondary regenerative agent pipe, secondary pre-riser, secondary riser, nozzle；On main regenerative agent pipe End is connected with regenerator, and lower end is connected with main pre-riser, and main riser bottom is provided with heavy oil nozzle, and upper end is connected with fast bed Lower end is connected with main pre-riser；Secondary regenerative agent pipe upper end is connected with regenerator or external warmer, and lower end is connected with secondary pre-riser, Secondary riser is provided with gasoline, dry gas nozzle, and lower end is connected with secondary pre-riser upper end, and upper end folds and main riser upper end or fast Speed bed lower end connects.

Multi-functional residue fluid catalytic cracking unit the most according to claim 4, is characterized in that: can also be in secondary riser bottom Light cycle oil nozzle is set, it is also possible to arrange enlarged diameter conversion zone and C4～C6 alkene nozzle in secondary riser bottom.

Multi-functional residue fluid catalytic cracking unit the most according to claim 4, is characterized in that: can also be on secondary riser top Secondary fast bed is set, it is also possible to arrange heat removing tube at secondary pre-riser.

Multi-functional residue fluid catalytic cracking unit the most according to claim 4, is characterized in that: can also arrange secondary fast point, pair Stripping section or secondary storing section, secondary spent agent pipe, secondary riser upper end divides soon with pair and is connected, secondary fast point of lower end and pair stripping section or pair The linking of storing section, secondary spent agent pipe upper end is connected with secondary stripping section or secondary storing pars infrasegmentalis, lower end and main riser upper end or quick Bed lower end connects.

Multi-functional residue fluid catalytic cracking unit the most according to claim 7, is characterized in that: can also be in secondary stripping section or pair Storing section arranges heat removing tube.

Multi-functional residue fluid catalytic cracking unit the most according to claim 4, is characterized in that: can also be on main riser top Wax tailings nozzle is set, it is also possible to arrange heat removing tube at fast bed.