CN103540345A - Catalytic cracking method - Google Patents

Abstract

The invention discloses a catalytic cracking method. A downer reactor is respectively subjected to heavy oil catalytic cracking and light hydrocarbon catalytic modification, and a reactant enters a settler so as to be subjected to gas-solid separation; after being mixed and stripped, the spent catalyst is scorched and regenerated together with a part of regenerated catalyst through a riser regenerator, and a semi-regenerated catalyst enters a turbulent bed so as to be further regenerated; a part of regenerated catalyst enters a catalyst mixing tank after being cooled by an external cooler and is mixed with the other part of regenerated catalyst, and then, the regenerated catalyst returns to two reactors in two paths so as to be recycled; the reacted oil gas is subjected to fractional distillation. By using the catalytic cracking method, the distribution of catalytic cracked products can be improved, the yield of light oil can be increased, and the yields of cracked gas and cokes can be reduced.

Description

A kind of catalyst cracking method

Technical field

The present invention relates in the situation that not there is not hydrogen the catalytic cracking field of hydrocarbon ils, particularly a kind of catalyst cracking method.

Background technology

At present, although the device that petroleum chemical industry catalytic cracking process is used is varied, but the process form of its reaction-regeneration system is basically identical, most single riser reactor (or single riser tube combine with fast bed two section reactor) and turbulent bed revivifiers (or turbulent bed combine with fast bed two-part revivifier) of adopting.Catalyzer and stock oil are along the up reaction of riser tube after riser tube bottom contact mixing, and reactant flow enters settling vessel from riser tube top exit and carries out the separated of reaction oil gas and catalyzer; Isolated reclaimable catalyst enters revivifier coke burning regeneration after one section of conventional stripping of stripping stage; Regenerated catalyst returns to riser tube bottom cycle and uses.In above-mentioned conventional catalytic cracking unit, there is the shortcoming of following several respects: first, regenerated catalyst temperature cannot realize flexible control, regeneration temperature catalyzer is generally all higher than 650 ℃, in riser reactor, finish Contact Temperature is higher, the degree that higher finish Contact Temperature carries out heat cracking reaction is higher, and the degree of catalytic cracking reaction is lower, cause that dry gas and coke yield are higher, total liquid yield is lower (total liquid yield refers to liquefied gas yield, gasoline yield and diesel yield sum); Due to higher regenerated catalyst temperature, limited by device thermal equilibrium, make the agent-oil ratio of heavy oil riser reactor relatively little, be generally 5～8 (agent-oil ratio of riser reactor is the ratio of weight internal circulating load with the weight rate of heavy oil riser reactor charging of riser reactor inner catalyst), thereby the number of active center that the stock oil that makes unit weight touches is less, this has also suppressed the carrying out of catalytic cracking reaction.Second, owing to promoting the length of tubular reactor and determined the reaction times long (generally in 4s left and right) of raw material, the longer reaction times has also been aggravated the secondary reaction of raw material cracking resultant when improving raw material per pass conversion, make reacted gas (dry gas, liquefied gas yield sum) productive rate higher, vapour, diesel oil distillate yield are lower, catalytic diesel oil cetane value is lower simultaneously, is not suitable as vehicle fuel.The 3rd, owing to promoting tubular type catalyst reactor, against gravity field, move upward and cause landing and the back-mixing of coked catalyst, promoting tubular type reactor feedstocks nozzle top, the coked catalyst of landing and atomized feed and cracking resultant be contact reacts again, thereby worsened product distribution, reduced the product selectivity of catalyzer to raw material cracking.The 4th, because turbulent bed revivifier coke burning degree is relatively low, make the higher and catalyzer of the catalyst inventory of revivifier longly cause catalyzer hydrothermal deactivation comparatively serious in the revivifier residence time.The 5th, the steam stripping efficiency of stripping stage is lower, causes producing more can stripping burnt.The 6th, catalytic gasoline cannot carry out independent upgrading, and quality is lower.

For many years, both at home and abroad a large amount of research work has been done overcoming aspect the existing shortcoming of above-mentioned conventional catalytic cracking unit by research institution.

The principal character of the disclosed a kind of catalytic cracking technology of Chinese patent CN1710029 is: adopt Double-lifted pipe catalytic cracking device, catalytic gasoline is carried out independent upgrading and utilizes the technical superiority of Double-lifted pipe catalytic cracking device, by part or all of remaining activity higher (be equivalent to regenerator activity 90%), temperature lower (500 ℃ of left and right) and the steam stripped lighter hydrocarbons riser tube reclaimable catalyst of process return to the catalyst mix device that heavy oil riser tube bottom arranges, together with after mixing with regenerated catalyst from revivifier, enter heavy oil riser tube and heavy oil contact reacts in catalyst mix device.Due to catalytic gasoline is carried out to independent upgrading, gasoline property is improved greatly; Heat exchange action due to two strands of catalyzer in mixing tank makes the temperature of mixed catalyst lower simultaneously, has realized finish " low temperature contact, high agent-oil ratio " operation, thereby effectively reduces dry gas, the coke yield of device, has improved total liquid yield.But this technology exists, following some is not enough: the first, and the catalytic cracking unit of riser tubes more than adopting the measure of lighter hydrocarbons riser tube reclaimable catalyst and regenerated catalyst hybrid cooling to cause the advantage of this Techniques For Reducing riser tube finish Contact Temperature and rising agent oil ratio only can be embodied in to there are two; The second, the catalyst cracker adopting due to this technology is traditional lifting tubular reactor, still shows because the reaction times is long and causes product distribution relative poor with catalyzer back-mixing; The 3rd, because adopting traditional turbulent bed revivifier to exist, this technology burns inefficient deficiency; The 4th, owing to adopting conventional stripping mode, the raising of catalyst recirculation amount has a negative impact to Srteam Stripping effect.

The principal character of the disclosed a kind of molecular sieve catalyst highly efficient regeneration catalytic cracking process technology of Chinese patent CN1210762 is: it is separated with flue gas that reclaimable catalyst enters external cyclone water-separator group after the regeneration of one-level riser regenerator, then half regenerated catalyst enters two-stage hoisting pipe revivifier through dipleg and proceeds regeneration, regenerated catalyst enters external warmer heat-obtaining through two-stage hoisting pipe revivifier external cyclone water-separator group dipleg, and last regenerated catalyst enters riser reactor through external warmer bottom inclined tube.This technology time of burning was controlled in 10 seconds, and coke burning degree (the burning carbon amount of unit catalyst inventory in the unit time) is 10 times of left and right of prior art.And can effectively reduce finish Contact Temperature, rising agent oil ratio.But there is following some deficiency in this technology: the first, and because adopting traditional lifting tubular reactor cannot realize the raw material short reaction time and overcoming catalyzer back-mixing.The second, technological process and complicated operation, be difficult to carry out in engineering.The 3rd, adopt single reactor and cannot realize the independent upgrading to catalytic gasoline.

The principal character of the disclosed a kind of catalytic cracking riser revivifier technology of Chinese patent CN2169473 is: in riser regenerator, be provided with multistage air inlet and carry out reclaimable catalyst regeneration.This technique the coke burning regeneration process of reclaimable catalyst, avoided riser tube ingress to introduce and cause the too low nonflammable phenomenon of coke that occurs of catalyst temperature due to a large amount of freezing airs simultaneously, it is simple in structure, easy to operate.But the technical measures that not yet relate to reactive moieties.

US Patent No. 5,462, the principal character of 652 disclosed a kind of catalytic cracking process technology is: the first, by the method for mixing with reclaimable catalyst, reduce the temperature of regenerated catalyst, reacting-settler dilute phase section arranges catalyst mix tank, from the regenerated catalyst of revivifier with through steam stripped reclaimable catalyst therein mixed heat transfer enter reacting-settler under backward, second, adopt the finish way of contact different from traditional riser reactor, catalyzer and raw material react and the stripping of reclaimable catalyst all carries out in reacting-settler, catalyzer is flowed downward under action of gravity by the mixed catalyst chamber central opening that is located at reacting-settler top, the raw material injection direction of nozzle and the catalyzer direction angle in 90 ° that flows, stock oil carries catalyzer along continuous straight runs high-speed motion and reacts after contacting with catalyzer, reactant flow enters the plug-in cyclonic separator of reacting-settler and carries out the separated of reaction oil gas and catalyzer afterwards.Due to above feature, this technology has realized finish " low temperature contact, high agent-oil ratio " operation, has shortened the reaction times to a certain extent simultaneously, has overcome the back-mixing of catalyzer, product is distributed and improve.But also there is following some deficiency in this technology: the first, and owing to adopting conventional turbulent bed revivifier, it is lower that it burns efficiency.The second, reclaimable catalyst participates in reaction, has reduced the average activity of mixed catalyst, also certainly will bring disadvantageous effect to product distribution and product property.The 3rd, technological process and operation are comparatively complicated.The 4th, adopt single reactor and cannot realize the independent upgrading to gasoline.

US Patent No. 4, 514, the principal character of 285 disclosed a kind of catalytic cracking process technology is: first, adopt finish contact and the separate mode different from traditional riser reactor, regenerated catalyst enters tubular reactor downwards from the settling vessel outlet at bottom of regenerating, under the effect of gravity, along downer reactor, flow downward, along downer reactor, axially in different level heights, be provided with some layers of raw material nozzles, the raw material injection direction of nozzle is tilted to down, different raw materials enters downer reactor according to the never level nozzle of different reaction needed and contacts mixing with regenerated catalyst and react along downer reactor is descending, reactant flow enters reacting-settler from downer reactor outlet at bottom, most of catalyzer continues descending until enter close phase section under the effect of gravity, reaction oil gas has significantly reduced mobile linear speed due to the rapid expansion of actual internal area, is carrying a small amount of catalyzer secretly and is entering cyclonic separator and carry out further separation, the second, the temperature of the method raising stripping stage of regenerated catalyst is introduced in employing, at two different stripping stages of reacting-settler bottom set temperature, the 3rd, adopt riser regenerator, reclaimable catalyst enters reclaimable catalyst transfer lime under two sections of strippings are backward, and under the conveying effect of main air, enters riser regenerator and carry out coke burning regeneration, catalyzer after regeneration enters regeneration settling vessel downwards and carries out initial gross separation through being located at the inertial separator outlet at riser regenerator top together with flue gas, and its separation principle is identical with the sepn process of reaction oil gas and reclaimable catalyst.Due to above feature, this technology has shortened the reaction times to a certain extent, and can realize the flexible control to the reaction times, has overcome the back-mixing of catalyzer simultaneously, has improved steam stripping efficiency, product is distributed and improve, and has improved in addition regeneration efficiency.But still there is following some deficiency in this technology: the first, and regenerated catalyst temperature cannot be controlled flexibly, cannot realize " low temperature contact, high agent-oil ratio " operation, and then product distribution and product property are brought to disadvantageous effect.The second, the inertial separator finish separation that downer reactor end adopts is not thorough, and the part oil gas reaction times is longer.The 3rd, adopt single reactor and cannot realize the independent upgrading to gasoline.

According to above-mentioned analysis, can find out, adopt an effective measure and reduce and control regenerated catalyst temperature, under the prerequisite that keeps catalyst activity, suitably improve catalytic cracking reaction agent-oil ratio, shorten and the flexible control reaction times, overcome the back-mixing of catalyst in reactor, improve steam stripping efficiency and regeneration efficiency, catalytic gasoline is carried out to independent upgrading, to improving product distribution and product property, reduction plant energy consumption and the catalyst inventory of catalytic cracking reaction, slow down catalyst aging process, dwindle reactor size and then reduce facility investment and there is important effect.

Summary of the invention

Technical problem to be solved by this invention is: provide a kind of and can overcome the existing regenerated catalyst of existing conventional catalytic cracking process and stock oil Contact Temperature is higher, agent-oil ratio is lower, the reaction times is long, catalyst in reactor back-mixing is serious, steam stripping efficiency and regeneration efficiency is lower, catalytic gasoline cannot carry out the complex art difficulties such as independent upgrading catalyst cracking method.

A kind of catalyst cracking method provided by the invention, is characterized in that there is the following step:

1) heavy oil feedstock 43 contacts and reacts with the regenerated catalyst from catalyst mix tank 8 in heavy oil downer reactor 26, heavy oil reactant flow enters settling vessel 25 and carries out gas solid separation, isolated heavy oil reaction oil gas enters heavy oil reaction oil gas separation column, and heavy oil reclaimable catalyst enters step 3);

2) light hydrocarbon feedstocks 44 contacts and reacts with the regenerated catalyst from catalyst mix tank 8 in lighter hydrocarbons downer reactor 13, lighter hydrocarbons reactant flow enters settling vessel 25 and carries out gas solid separation, isolated lighter hydrocarbons reaction oil gas enters lighter hydrocarbons reaction oil gas separation column, and lighter hydrocarbons reclaimable catalyst enters step 3);

3) after heavy oil reclaimable catalyst and the mixing of lighter hydrocarbons reclaimable catalyst, enter stripping stage 23 and carry out stripping, through steam stripped mixing reclaimable catalyst, carry out coke burning regeneration successively through riser regenerator 2 and turbulent bed revivifier 1, the regenerated catalyst of process two-stage regeneration enters catalyst mix tank 8.

The described regenerated catalyst through two-stage regeneration, a part enters catalyst mix tank 8 after external warmer 32 is cooling, another part enters catalyst mix tank 8 through catalyst mix tank high temperature catalyst transfer lime 5, two strands of regenerated catalysts mixed heat transfer under the disturbance of air 40 that enters catalyst mix tank 8 through air-distributor 6b, the air 40 of discharging from catalyst mix tank 8 tops carries a small amount of regenerated catalyst and from bottom, enter turbulent bed revivifier 1 together with another strand of air 40.

The described regenerated catalyst through two-stage regeneration enters catalyst mix tank 8 by turbulent bed revivifier 1 through catalyst mix tank high temperature catalyst transfer lime 5.

The described regenerated catalyst from catalyst mix tank 8 enters heavy oil downer reactor 26 through heavy oil reactor catalyst transfer lime 29 downwards, by catalyst distribution plate 11a, undertaken continuing a descending segment distance after rectification and contact mixing with heavy oil feedstock 43 again, reactant flow is descending and react along heavy oil downer reactor 26.

The described regenerated catalyst from catalyst mix tank 8 enters lighter hydrocarbons downer reactor 13 through lighter hydrocarbons reactor catalyst transfer lime 9 downwards, by catalyst distribution plate 11b, undertaken continuing a descending segment distance after rectification and contact mixing with light hydrocarbon feedstocks 44 again, reactant flow is descending and react along lighter hydrocarbons downer reactor 13.

Described heavy oil feedstock 43 enters heavy oil downer reactor 26 and contacts with the regenerated catalyst from catalyst mix tank 8 through being tilted to the heavy oil feedstock nozzle 27 of lower setting.

Described light hydrocarbon feedstocks 44 enters lighter hydrocarbons downer reactor 13 and contacts with the regenerated catalyst from catalyst mix tank 8 through being tilted to the light hydrocarbon feedstocks nozzle 12 of lower setting.

Described heavy oil feedstock 43 comprises 1～5 kind.

Described light hydrocarbon feedstocks 44 comprises 1～5 kind.

Described heavy oil feedstock 43, different types ofly can, according to reaction needed, enter heavy oil downer reactor 26 from being arranged on the heavy oil feedstock nozzle 27 of heavy oil downer reactor 26 axial different heights.

Described light hydrocarbon feedstocks 44, different types ofly can, according to reaction needed, enter lighter hydrocarbons downer reactor 13 from being arranged on the light hydrocarbon feedstocks nozzle 12 of lighter hydrocarbons downer reactor 13 axial different heights.

Described heavy oil reactant flow directly enters from heavy oil downer reactor 26 the thick cyclonic separator 22 of heavy oil reactor that is positioned at settling vessel 25 and carries out gas solid separation, and isolated gaseous stream enters heavy oil reactor primary cyclone 21 through connecting tube and carries out further gas solid separation.

Described lighter hydrocarbons reactant flow directly enters from lighter hydrocarbons downer reactor 13 the thick cyclonic separator 17 of lighter hydrocarbons reactor that is positioned at settling vessel 25 and carries out gas solid separation, and isolated gaseous stream enters lighter hydrocarbons reactor primary cyclone 18 through connecting tube and carries out further gas solid separation.

Described heavy oil reclaimable catalyst and lighter hydrocarbons reclaimable catalyst enter stripping stage 23 through each cyclone dip-leg respectively to be mixed, and prior to stripping stage 23 tops, at lower temperature, with water vapor 45, carry out stripping, after enter after mix with the regenerated catalyst that enters stripping stage 23 bottoms through stripping stage regenerated catalyst 4 from turbulent bed revivifier 1 stripping stage 23 bottoms with water vapor 45, further carry out stripping at higher temperature.

Described enters stripping stage 23 through being located at the pre-stripping of pre-stripper of the thick cyclonic separator of heavy oil reactor 22 belows by dipleg by the isolated heavy oil reclaimable catalyst of the thick cyclonic separator 22 of heavy oil reactor, by the isolated lighter hydrocarbons reclaimable catalyst of the thick cyclonic separator 17 of lighter hydrocarbons reactor, through being located at the pre-stripping of pre-stripper of the thick cyclonic separator of lighter hydrocarbons reactor 17 belows, by dipleg, enter stripping stage 23, by heavy oil reactor primary cyclone 21 isolated reclaimable catalysts with by lighter hydrocarbons reactor primary cyclone 18 isolated reclaimable catalysts, through dipleg, enter stripping stage 23 respectively, above-mentioned several strands of reclaimable catalysts mix at stripping stage 23, then prior to stripping stage 23 tops, at lower temperature, with water vapor 45, carry out stripping, at higher temperature, with water vapor 45, further carry out stripping entering after mix with the regenerated catalyst that enters stripping stage 23 bottoms through stripping stage regenerated catalyst 4 from turbulent bed revivifier 1 stripping stage 23 bottoms.

The stripping logistics that described mixing reclaimable catalyst produces in by stripping process is divided into two portions, a part enters heavy oil reactor primary cyclone 21 and carries out gas solid separation, and another part enters lighter hydrocarbons reactor primary cyclone 18 and carries out gas solid separation.

The described stripping logistics being produced in pre-stripping process by the isolated heavy oil reclaimable catalyst of the thick cyclonic separator 22 of heavy oil reactor mixes with the isolated gaseous stream of the thick cyclonic separator 22 of heavy oil reactor and by connecting tube, enters heavy oil reactor primary cyclone 21 and carry out further gas solid separation, and the stripping logistics being produced in stripping process in advance by the isolated lighter hydrocarbons reclaimable catalyst of the thick cyclonic separator 17 of lighter hydrocarbons reactor mixes with the isolated gaseous stream of the thick cyclonic separator 17 of lighter hydrocarbons reactor and by connecting tube, enters lighter hydrocarbons reactor primary cyclone 18 and carry out further gas solid separation.

Described heavy oil reaction oil gas and the hydro carbons oil gas that gone out by stripping of a part enter heavy oil reaction oil gas separation column as the charging 42 of heavy oil reaction oil gas separation column through heavy oil reaction collection chamber 20 and heavy oil reaction oil gas pipeline and carry out fractionation.

The hydro carbons oil gas that described lighter hydrocarbons reaction oil gas and another part are gone out by stripping enters lighter hydrocarbons reaction oil gas separation column as the charging 41 of lighter hydrocarbons reaction oil gas separation column through lighter hydrocarbons reactions collection chamber 19 and lighter hydrocarbons reaction oil gas pipeline and carries out fractionation.

The steam stripped mixing reclaimable catalyst of described process enters riser regenerator 2 through reclaimable catalyst transfer lime 15 downwards, up and carry out coke burning regeneration along riser regenerator 2.

Described riser regenerator 2 is burnt required air 40 and is entered along separate routes from 2～6 layer of air entrances 3 that are arranged on the air-distributor 6c of its bottom and be arranged on the wall of its axial different heights, wherein, accounting for the air 40 that enters riser regenerator air total amount 20%～50% enters from air-distributor 6c, remaining air 40 enters from 2～6 layer of air entrances 3, and the air input of each layer of air entrance 3 can flexible allocation.

Described riser regenerator 2 burning-offs more than 30% are deposited on the coke mixing on reclaimable catalyst.

Half regenerated catalyst that described riser regenerator (2) generates enters inertial separator 38 downwards through riser regenerator 2 outlets and carries out gas solid separation together with regenerated flue gas, and isolated half regenerated catalyst enters the further coke burning regeneration of air 40 contact that the close phase Duan Yujing air-distributor of turbulent bed revivifier 1 6a enters turbulent bed revivifier 1 downwards.

The regenerated flue gas of described riser regenerator 2 and the regenerated flue gas of turbulent bed revivifier 1 and a small amount of granules of catalyst of carrying secretly thereof carry out gas solid separation through revivifier primary cyclone 35 and revivifier secondary cyclone 36 successively, isolated granules of catalyst returns to the close phase section of turbulent bed revivifier 1 through the dipleg of each cyclonic separator of revivifier, and isolated mixed flue gas 39 enters smoke energy recovering system through flue gas collection chamber 37 and flue gas pipeline.

From turbulent bed revivifier 1, enter external warmer 32, catalyst mix tank 8 and stripping stage 23, the flow that enters catalyst mix tank 8 and enter the regenerated catalyst of heavy oil downer reactor 26 and lighter hydrocarbons downer reactor 13 from catalyst mix tank 8 from external warmer 32, the flow that enters the reclaimable catalyst of riser regenerator 2 from stripping stage 23 all can pass through Flux Valve Control.

The operational condition of described heavy oil downer reactor 26 is, 460～580 ℃ of temperature of reaction, reaction times 0.2～2.0s, agent-oil ratio 5～40, reaction absolute pressure 0.15～0.40Mpa, catalyst activity 58～75.

The operational condition of described lighter hydrocarbons downer reactor (13) is, 450～600 ℃ of temperature of reaction, reaction times 0.2～2.5s, agent-oil ratio 3～35, reaction absolute pressure 0.15～0.40Mpa, catalyst activity 58～75.

The operational condition of described settling vessel 25 is, 450～590 ℃ of dilute phase temperature; Top absolute pressure 0.20～0.50Mpa.

The operational condition of described riser regenerator 2 is, 500～600 ℃ of temperature ins, and 560～720 ℃ of temperature outs, average gas linear speed 3.0～10.0m/s, coke burning degree 300～1200kg/th, burns time 5～40s.

The operational condition of described turbulent bed revivifier 1 is, 580～740 ℃ of regeneration temperatures, and coke burning degree 0～120kg/th, burns time 1.0～4.0min, top absolute pressure 0.10～0.40Mpa.

Compare with existing conventional catalytic cracking technology, the present invention has following beneficial effect:

1. owing to adopting shorter downer reactor of finish contact reacts time, can effectively reduce secondary reaction, control depth of conversion, and overcome the disadvantageous effect that catalyzer back-mixing comes cracking reaction zone, significantly reduce reacted gas and coke yield, significantly improve the cetane value of yield of light oil and catalytic diesel oil; Meanwhile, multiple feed mode makes the control of reaction conditions more flexible.

2. due to the method that adopts riser regenerator to combine with turbulent bed revivifier and use, both can improve coke burning degree and burn efficiency, can guarantee regeneration effect again, thereby having shortened the residence time of catalyzer in revivifier, having slowed down the hydrothermal deactivation of catalyzer; Meanwhile, the mode of multiple spot air intake makes the temperature at each position of riser regenerator be easy to control, and operates more steady.

3. owing to adopting the method for the cooling regenerated catalyst of external warmer, can effectively control regenerated catalyst temperature, realizing regenerated catalyst operates with " low temperature contacts; high agent-oil ratio " of raw material, and then inhibition heat cracking reaction, promote catalytic cracking reaction, reduce dry gas and coke yield, reduce plant energy consumption simultaneously.

4. owing to adopting two sections of steam stripped methods, give full play to physics stripping and chemical steam stripped dual function, can significantly improve Srteam Stripping effect, overcome the catalyst recirculation amount disadvantageous effect that operation brings to stripping greatly, thereby reduce can stripping burntly, further improve yield of light oil.

5. owing to adopting double-reactor and two fractionating column system, can under suitable condition, carry out independent upgrading to catalytic gasoline or other lighter hydrocarbons, thereby guarantee to produce high-quality gasoline.

Below in conjunction with accompanying drawing, embodiment and embodiment, the present invention is further detailed explanation.But do not limit the scope of protection of present invention.

Accompanying drawing and accompanying drawing explanation

Fig. 1 is the schematic diagram of realizing the device reaction-regeneration system of catalyst cracking method of the present invention.

Wherein:

1. turbulent bed revivifier, 2. riser regenerator, 3a, 3b, 3c. gas inlet, 4. stripping stage regenerated catalyst, 5. catalyst transport, 6a, 6b, 6c. air-distributor, 7. catalyst mix tank high temperature catalyst flow control valve, 8. catalyst mix tank, 9. lighter hydrocarbons reactor regenerated catalyst, 10. lighter hydrocarbons reactor regenerated catalyst flow control valve, 11a, 11b. catalyst distribution plate, 12a, 12b, 12c. light hydrocarbon feedstocks nozzle, 13. reactors, 14. stripping stage regenerated catalyst flow control valves, 15. reclaimable catalyst transfer limes, 16. reclaimable catalyst flow control valves, the thick cyclonic separator of 17. lighter hydrocarbons reactor, 18. lighter hydrocarbons reactor primary cyclones, 19. lighter hydrocarbons reaction collection chambers, 20. heavy oil reaction collection chambers, 21. heavy oil reactor primary cyclones, the thick cyclonic separator of 22. heavy oil reactor, 23. stripping stages, 24a, 24b. steam distributor, 25. settling vessels, 26. reactors, 27a, 27b, 27c. heavy oil feedstock nozzle, 28. heavy oil reactor regenerated catalyst flow control valves, 29. heavy oil reactor regenerated catalyst, 30. external warmer catalyst outlet flow control valves, 31. external warmer catalyst outlet pipes, 32. external warmers, 33. external warmer catalyst inlet pipes, 34. external warmer catalyst inlet flow control valves, 35a, 35b. revivifier primary cyclone, 36a, 36b. revivifier secondary cyclone, 37. flue gas collection chambers, 38. inertial separators, 39. mixed flue gas, 40. air, 41. lighter hydrocarbons reaction oil gas separation column chargings, 42. heavy oil reaction oil gas separation column chargings, 43. heavy oil feedstocks, 44. light hydrocarbon feedstocks, 45. water vapors.

Embodiment

As shown in Figure 1, the device of realizing catalyst cracking method of the present invention is mainly comprised of heavy oil downer reactor 26, lighter hydrocarbons downer reactor 13, settling vessel 25, riser regenerator 2, turbulent bed revivifier 1, catalyst mix tank 8 and external warmer 32, turbulent bed revivifier 1 is positioned at settling vessel 25 tops, and both adopt coaxial-type to arrange; The close phase section of turbulent bed revivifier 1 is connected with external warmer 32 tops, catalyst mix tank 8 tops and the close phase pars infrasegmentalis of settling vessel 25 by external warmer catalyst inlet pipe 33, catalyst mix tank high temperature catalyst transfer lime 5 and stripping stage regenerated catalyst 4 respectively, and external warmer 32 bottoms are connected with catalyst mix tank 8 tops by external warmer catalyst outlet pipe 31; Catalyst mix tank 8 bottoms are connected with heavy oil downer reactor 26 tops and lighter hydrocarbons downer reactor 13 tops by heavy oil reactor regenerated catalyst 29 and lighter hydrocarbons reactor regenerated catalyst 9 respectively; Heavy oil downer reactor 26 bottoms and lighter hydrocarbons downer reactor 13 bottoms enter respectively settling vessel 25 dilute phase sections; The close phase section of settling vessel 25 is stripping stage 23, and stripping stage 23 bottoms are connected with riser regenerator 2 bottoms by reclaimable catalyst transfer lime 15; Riser regenerator 2 tops are connected with turbulent bed revivifier 1 top by inertial separator 38.

External warmer catalyst inlet pipe 33, catalyst mix tank high temperature catalyst transfer lime 5 and stripping stage regenerated catalyst 4 entrances all adopt and flood head piece form and setting and flood stream bucket, external warmer catalyst inlet pipe 33, catalyst mix tank high temperature catalyst transfer lime 5, stripping stage regenerated catalyst 4, external warmer catalyst outlet pipe 31, heavy oil reactor regenerated catalyst 29, on lighter hydrocarbons reactor regenerated catalyst 9 and reclaimable catalyst transfer lime 15, be respectively equipped with external warmer catalyst inlet flow control valve 34, catalyst mix tank high temperature catalyst flow control valve 7, stripping stage regenerated catalyst flow control valve 14, external warmer catalyst outlet flow control valve 30, heavy oil reactor regenerated catalyst flow control valve 28, lighter hydrocarbons reactor regenerated catalyst flow control valve 10 and reclaimable catalyst flow control valve 16, seven described variable valve are fluidized solids flow control valve, guiding valve particularly, 31 outlets of external warmer catalyst outlet pipe are positioned at the axial centre region on catalyst mix tank 8 tops, and the outlet of stripping stage regenerated catalyst 4 is positioned at the axial centre region of stripping stage 23 bottoms.

Catalyst mix tank 8 is a cylinder shape cylindrical shell; Cylindrical shell two ends are provided with disk bottom, the top of cylindrical shell is provided with two catalyst inlets, the bottom of cylindrical shell is provided with two catalyst outlets, catalyst mix tank 8 bottoms are provided with air-distributor 6b, top is provided with venting port, and this venting port is connected with the gas inlet pipeline of turbulent bed regenerator bottoms by air line.

Heavy oil downer reactor 26 is identical with lighter hydrocarbons downer reactor 13 structures, by finish mixing tube and reactant flow delivery line, is composed in series, two finish mixing tubes vertically arrange, and its top entrance is connected with the outlet at bottom of lighter hydrocarbons reactor regenerated catalyst 9 with heavy oil reactor regenerated catalyst 29 respectively, its top is equipped with dome head, and bottom is equipped with conical head, the entrance below of two finish mixing tubes is respectively equipped with catalyst distribution plate 11a and catalyst distribution plate 11b, and on the wall of its axial different heights, be respectively equipped with three layers of heavy oil feedstock nozzle 27a, 27b, 27c and three layers of light hydrocarbon feedstocks nozzle 12a, 12b, 12c, every layer of heavy oil feedstock nozzle 27a wherein, 27b, 27c and light hydrocarbon feedstocks nozzle 12a, 12b, 12c comprises respectively again six the heavy oil feedstock nozzle 27 and the light hydrocarbon feedstocks nozzles 12 that become matrix distribution, with the heavy oil feedstock nozzle of layer and light hydrocarbon feedstocks nozzle arrangements consistent size and two one group, take respectively two finish mixing tube central shafts is symmetrical arranged as symmetry axis, heavy oil feedstock nozzle 27a, 27b, 27c and light hydrocarbon feedstocks nozzle 12a, 12b, the raw material injection direction of 12c is tilted to down and points to respectively two finish mixing tube central shafts, each layer of heavy oil feedstock nozzle 27a, 27b, 27c and light hydrocarbon feedstocks nozzle 12a, 12b, 12c can adopt identical or different angle of inclination as required, two reactant flow delivery lines are composed in series by inclined tube section and horizontal section, the entrance of two reactant flow delivery line inclined tube sections is connected with two finish mixing tube outlet at bottoms respectively, two reactant flow delivery line horizontal sections enter settling vessel 25 dilute phase sections through wall, and its outlet is connected with thick cyclonic separator 17 entrances of lighter hydrocarbons reactor with thick cyclonic separator 22 entrances of heavy oil reactor respectively.

In settling vessel 25, except the thick cyclonic separator 22 of heavy oil reactor and the thick cyclonic separator 17 of lighter hydrocarbons reactor, be also provided with a heavy oil reactor primary cyclone 21 and a lighter hydrocarbons reactor primary cyclone 18; Thick cyclonic separator 22 outlet conduits of heavy oil reactor and heavy oil reactor primary cyclone 21 inlet ducts socket-connect, be that thick cyclonic separator 22 outlet conduits of heavy oil reactor are outer little through proportion oil reactor primary cyclone 21 inlet duct internal diameters, and insert wherein, simultaneously to assist inner member to fix and centering, pipeline annular space is connected with settling vessel 25 dilute phase sections as the entrance of stripping logistics, and 21 outlets of heavy oil reactor primary cyclone are connected with heavy oil reaction collection chamber 20 by closed conduct; Thick cyclonic separator 17 outlet conduits of lighter hydrocarbons reactor and lighter hydrocarbons reactor primary cyclone 18 inlet ducts socket-connect, be that thick cyclonic separator 17 outlet conduits of lighter hydrocarbons reactor are outer through less than lighter hydrocarbons reactor primary cyclone 18 inlet duct internal diameters, and insert wherein, simultaneously to assist inner member to fix and centering, pipeline annular space is connected with settling vessel 25 dilute phase sections with the entrance as stripping logistics, and 18 outlets of lighter hydrocarbons reactor primary cyclone are connected with lighter hydrocarbons reaction collection chamber 19 by closed conduct; Heavy oil reaction collection chamber 20 and lighter hydrocarbons reaction collection chamber 19 are all positioned at settling vessel 25 tops, be separate two independently spaces, by heavy oil reaction oil gas pipeline and lighter hydrocarbons reaction oil gas pipeline, be connected with heavy oil reaction oil gas separation column and lighter hydrocarbons reaction oil gas separation column respectively.

In stripping stage 23, be provided with two steam distributor 24a, 24b, wherein steam distributor 24a is arranged on stripping stage regenerated catalyst 4 outlet at bottom tops, and steam distributor 24b is arranged on stripping stage 23 bottoms.

Riser regenerator 2 is composed in series with horizontal section by vertical section; Vertically section bottom inlet is connected with reclaimable catalyst transfer lime 15 outlet at bottoms; Vertically section top is provided with air cushion elbow, and bottom is provided with dome head; Vertically section bottom is provided with air-distributor 6c, and on the wall of its axial different heights, is provided with three layer of air entrance 3a, 3b, 3c, wherein every layer of gas inlet 3 that includes the identical and horizontal tangential air intake of four equally distributed scantlings of the structure; Horizontal section outlet is connected with inertial separator 38 entrances, and horizontal section exit end is also provided with air cushion elbow.

Inertial separator 38 is a pipe, vertically arranges, and its outlet is positioned at turbulent bed revivifier 1 dilute phase section top.

The close phase section of turbulent bed revivifier 1 bottom is provided with air-distributor 6a; Its dilute phase section top is provided with two groups of revivifier two stage cyclone separators, wherein, revivifier primary cyclone 35a, 35b entrance are connected with the dilute phase section of turbulent bed revivifier 1, revivifier primary cyclone 35a, 35b outlet is connected by closed conduct with revivifier secondary cyclone 36a, 36b entrance, and revivifier secondary cyclone 36a, 36b outlet is connected with the flue gas collection chamber 37 that is positioned at turbulent bed revivifier 1 top by closed conduct; Flue gas collection chamber 37 is connected with smoke energy recovering system by flue gas pipeline.

Each equipment body is metal material above, is generally carbon steel or stainless steel, wherein, external warmer catalyst inlet pipe 33, catalyst mix tank high temperature catalyst transfer lime 5, stripping stage regenerated catalyst 4, external warmer catalyst outlet pipe 31, heavy oil reactor regenerated catalyst 29, lighter hydrocarbons reactor regenerated catalyst 9, reclaimable catalyst transfer lime 15, heavy oil downer reactor 26, lighter hydrocarbons downer reactor 13, settling vessel 25, riser regenerator 2, turbulent bed revivifier 1, catalyst mix tank 8, external warmer 32, the thick cyclonic separator 22 of heavy oil reactor, the thick cyclonic separator 17 of lighter hydrocarbons reactor, heavy oil reactor primary cyclone 21, lighter hydrocarbons reactor primary cyclone 18, revivifier primary cyclone 35a, 35b, revivifier secondary cyclone 36a, 36b inside is equipped with liner insulating and wearing-resistant lining, the model of lining and thickness are determined according to the service temperature at each position and catalyst stream moving-wire speed and chips washing system.

The total length of heavy oil downer reactor 26 is generally 8～15m, wherein, the length of finish mixing tube is generally 6～10m, the length of reactant flow delivery line inclined tube section is generally 1.5～3.2m, the length of reactant flow delivery line horizontal section is generally 0.5～1.8m, finish mixing tube internal diameter is not more than the logical internal diameter of reactant flow delivery line, and both internal diameters are generally 400～2500mm.

The total length of lighter hydrocarbons downer reactor 13 is generally 8～15m, wherein, the length of finish mixing tube is generally 6～10m, the length of reactant flow delivery line inclined tube section is generally 1.5～3.2m, the length of reactant flow delivery line horizontal section is generally 0.5～1.8m, finish mixing tube internal diameter is not more than the logical internal diameter of reactant flow delivery line, and both internal diameters are generally 300～1800mm.

The concrete length of heavy oil downer reactor 26 and lighter hydrocarbons downer reactor 13 each several parts can adopt the design and calculation method of conventional riser fluid catalytic cracking riser reactor to be determined according to the concrete structure size of the pressure equilibrium parameter request of the design linear speed of the design reaction times of each reactor, reactor each several part and whole catalytic cracking unit and settling vessel; The concrete internal diameter of heavy oil downer reactor 26 and lighter hydrocarbons downer reactor 13 each several parts can adopt the design and calculation method of conventional riser fluid catalytic cracking riser reactor to be determined according to the parameter requests such as design linear speed of the designing treatment amount of each reactor and reactor each several part; The inclined tube section of two reactant flow delivery lines and the angle of horizontal plane are generally 45 °～70 °, and being beneficial to descending reactant flow derives from finish mixing tube bottom.

Catalyst distribution plate 11a, 11b belong to existing conventional equipment, and its concrete structure and size can adopt the design and calculation method of existing catalyst distribution plate to be determined according to the operational condition of device.

Heavy oil feedstock nozzle 27a, 27b, 27c and light hydrocarbon feedstocks nozzle 12a, the raw material injection direction of 12b, 12c and the angle of horizontal plane are generally 45 °～80 °, are beneficial to the mixing of finish and the fluidisation of catalyzer; It specifically arranges height and carries out calculative determination according to each burst of needed reaction times of charging and the design linear speed of downer reactor each several part and the parameters such as length of reactant flow delivery line.

Heavy oil feedstock nozzle 27a, 27b, 27c and light hydrocarbon feedstocks nozzle 12a, 12b, 12c belong to existing conventional equipment, meet the general feature of conventional catalytically cracked material nozzle; Its concrete structure size can be according to the designing treatment amount of reactor, and the operational conditions such as atomizing steam amount adopt the design and calculation method of conventional catalytically cracked material nozzle to be determined, its concrete material can be determined according to feedstock property and operational condition.

The internal diameter of external warmer catalyst inlet pipe 33 is generally 200～1000mm, the internal diameter of catalyst mix tank high temperature catalyst transfer lime 5 is generally 400～2000mm, the internal diameter of stripping stage regenerated catalyst 4 is generally 300～1800mm, the internal diameter of external warmer catalyst outlet pipe 31 is generally 200～1000mm, the internal diameter of heavy oil reactor regenerated catalyst 29 is generally 300～1800mm, the internal diameter of lighter hydrocarbons reactor regenerated catalyst 9 is generally 200～1500mm, and the internal diameter of reclaimable catalyst transfer lime 15 is generally 500～3500mm; Above-mentioned several catalyst transports belong to existing conventional equipment, the general feature that meets dense-phase catalyst transport pipe, its concrete structure and size can adopt the design and calculation method of dense-phase catalyst transport pipe to be determined according to the device catalyst recirculation amount of each catalyst recirculation circuit and the space layout of device.

The riser regenerator 2 vertically length of section is generally 50～65m, and its internal diameter is generally 1200～8000mm; The length of riser regenerator 2 horizontal sections is generally 3～9m, and its internal diameter is generally 800～6000mm; Riser regenerator 2 meets the general feature of dilute catalyst phase transport pipe, can adopt the method for calculation of dilute catalyst phase transport pipe to determine the concrete structure size at its each position according to the design linear speed at the pressure equilibrium relation of device, design carbon-burning capacity and each position; Specifically arranging highly of three layer of air entrance 3a on riser regenerator 2 walls, 3b, 3c can be determined by calculating according to the air output of riser regenerator 2 bottom air spargers and each layer of air entrance and in conjunction with the coke burning degree of riser regenerator 2 each sections.

The length of inertial separator 38 is generally 4～8m, and its internal diameter is generally 600～4000mm.Its length is greater than the internal diameter of riser regenerator 2 horizontal sections, and its internal diameter is not more than the internal diameter of riser regenerator 2 horizontal sections.

The height of the cylinder shape staving of catalyst mix tank 8 is generally 2～8m, the internal diameter of cylinder shape staving is generally 1200～5000mm, and its concrete structure size can be carried out calculative determination according to the total catalyst internal circulating load of two reactors and the even parameters such as needed time of mixing of cold and hot catalyzer realization.

Settling vessel 25 belongs to existing conventional equipment, meets the conventional general feature that promotes tubular type catalytic cracking unit settling vessel, and its concrete structure size can adopt the design and calculation method of existing catalytic cracking unit settling vessel to be determined according to the operational condition of device.

Turbulent bed revivifier 1 belongs to existing conventional equipment, meet the conventional general feature that promotes tubular type catalytic cracking unit (employing) turbulent bed revivifier, its concrete structure size can adopt the design and calculation method of existing catalytic cracking unit turbulent bed revivifier to be determined according to the operational condition of device.

External warmer 32 belongs to existing conventional equipment, and its concrete structure size can adopt the design and calculation method of existing catalytic cracking unit external warmer to be determined according to the operational condition of device.

The thick cyclonic separator 22 of heavy oil reactor, the thick cyclonic separator 17 of lighter hydrocarbons reactor, heavy oil reactor primary cyclone 21, lighter hydrocarbons reactor primary cyclone 18 and revivifier primary cyclone 35a, 35b and revivifier secondary cyclone 36a, 36b belong to existing conventional equipment, and its concrete structure size can adopt the design and calculation method of existing cyclonic separator to be determined according to the operational condition of device.

Steam distributor 24a, 24b and air-distributor 6a, 6b, 6c can adopt the form of distribution pipe or grid distributor, also all belong to existing conventional equipment, its concrete structure size can adopt the design and calculation method of existing steam distributor and air-distributor to be determined according to the operational condition of device.

The stream bucket that floods that heavy oil reactor regenerated catalyst 29, lighter hydrocarbons reactor regenerated catalyst 9, stripping stage regenerated catalyst 4 ingress arrange belongs to existing conventional equipment, and its concrete structure size can adopt the existing design and calculation method that floods stream bucket to be determined according to the operational condition of device.

The catalyst cracking method of the present invention that adopts Fig. 1 shown device to carry out is as follows: a part of regenerated catalyst in turbulent bed revivifier 1 enters regenerated catalyst that catalyst mix tank 8 is not cooled with another part from turbulent bed revivifier 1 after external warmer 32 is cooling to be mixed and carries out heat exchange; Mixed regeneration catalyzer is divided into two strands, wherein a stock-traders' know-how heavy oil reactor regenerated catalyst 29 enters heavy oil downer reactor 26 and heavy oil feedstock 43 contact reactss, and another stock-traders' know-how lighter hydrocarbons reactor regenerated catalyst 9 enters lighter hydrocarbons downer reactor 13 and light hydrocarbon feedstocks 44 contact reactss; After reaction finishes, two bursts of reactant flow enter settling vessel 25 respectively oil separately the special-purpose minute separator that revolves carry out gas solid separation; Isolated heavy oil reclaimable catalyst and lighter hydrocarbons reclaimable catalyst enter riser regenerator 2 and carry out coke burning regeneration after mixing at stripping stage 23 and carrying out two sections of strippings; Half regenerated catalyst that riser regenerator 2 generates enters the further coke burning regeneration of turbulent bed revivifier 1; Regenerated catalyst through two-stage regeneration recycles, the hydrocarbon component that heavy oil reaction oil gas and a part are gone out by stripping is as heavy oil reaction oil gas separation column charging 42, and the hydrocarbon component that lighter hydrocarbons reaction oil gas and another part are gone out by stripping is as lighter hydrocarbons reaction oil gas separation column charging 41.

In above operating process, the different regenerated catalyst of two bursts of temperature that enters catalyst mix tank 8 through external warmer catalyst outlet pipe 31 and catalyst mix tank high temperature catalyst transfer lime 5 respectively evenly mixes and carries out heat exchange under the perturbation action of air 40 that enters catalyst mix tank 8 through air-distributor 6b; The air 40 of discharging from catalyst mix tank 8 tops carries a small amount of regenerated catalyst and from bottom, enters turbulent bed revivifier 1 together with after air line converges with another strand of air 40.

In above operating process, two strands of mixed regeneration catalyzer autocatalysis agent mixing tanks 8 enter heavy oil downer reactor 26 and lighter hydrocarbons downer reactor 13 through heavy oil reactor regenerated catalyst 29 and lighter hydrocarbons reactor regenerated catalyst 9 respectively downwards; And by catalyst distribution plate 11a and catalyst distribution plate 11b, carry out rectification respectively, after rectification, continue a descending segment distance and contact mixing with heavy oil feedstock 43 with light hydrocarbon feedstocks 44 respectively again, two bursts of reactant flow are descending and react along heavy oil downer reactor 26 and lighter hydrocarbons downer reactor 13 respectively afterwards.

In above operating process, heavy oil feedstock 43 comprises 3 kinds, and light hydrocarbon feedstocks 44 also comprises 3 kinds; According to reaction needed, any one heavy oil feedstock 43 can be from being arranged on three layers of heavy oil feedstock nozzle 27a the wall of heavy oil downer reactor 26 axial different heights, any one deck in 27b, 27c enters heavy oil downer reactor 26 and contacts with regenerated catalyst, and any one light hydrocarbon feedstocks 44 can be from being arranged on three layers of light hydrocarbon feedstocks nozzle 12a the wall of lighter hydrocarbons downer reactor 13 axial different heights, any one deck in 12b, 12c enters lighter hydrocarbons downer reactor 13 and contacts with regenerated catalyst.

In above operating process, the reactant flow delivery line of heavy oil downer reactor 26 reactant flow through heavy oil downer reactor 26 bottoms directly enters the thick cyclonic separator 22 of heavy oil reactor that is positioned at settling vessel 25 and carries out gas solid separation, and isolated gaseous stream enters heavy oil reactor primary cyclone 21 through connecting tube and carries out further gas solid separation; The reactant flow delivery line of lighter hydrocarbons downer reactor 13 reactant flow through lighter hydrocarbons downer reactor 13 bottoms directly enters the thick cyclonic separator 17 of lighter hydrocarbons reactor that is positioned at settling vessel 25 and carries out gas solid separation, and isolated gaseous stream enters lighter hydrocarbons reactor primary cyclone 18 through connecting tube and carries out further gas solid separation; Stripping logistics (the hydro carbons oil gas being gone out by stripping and a small amount of catalyzer of carrying secretly thereof) is divided into two portions, a part enters heavy oil reactor primary cyclone 21 and carries out gas solid separation, and another part enters lighter hydrocarbons reactor primary cyclone 18 and carries out gas solid separation; By the isolated heavy oil reaction oil gas of heavy oil reactor primary cyclone 21 and the hydro carbons oil gas that gone out by stripping of a part, through heavy oil reaction collection chamber 20 and heavy oil reaction oil gas pipeline, enter heavy oil reaction oil gas separation column and carry out fractionation, the hydro carbons oil gas being gone out by stripping by the isolated lighter hydrocarbons reaction oil gas of lighter hydrocarbons reactor primary cyclone 18 and another part enters lighter hydrocarbons reaction oil gas separation column through lighter hydrocarbons reaction collection chamber 19 and lighter hydrocarbons reaction oil gas pipeline and carries out fractionation.

In above operating process, heavy oil reclaimable catalyst and lighter hydrocarbons reclaimable catalyst enter stripping stage 23 through each cyclone dip-leg respectively to be mixed, prior to stripping stage 23 tops lower temperature with under water vapor 45 carry out stripping, after enter after mix with one regenerated catalyst that enters stripping stage bottom through stripping stage regenerated catalyst 4 from turbulent bed revivifier 1 stripping stage 23 bottoms with water vapor 45, further carry out stripping at higher temperature.

In above operating process, through reclaimable catalyst transfer lime 15, enter riser regenerator 2 downwards through steam stripped mixing reclaimable catalyst, up and carry out coke burning regeneration along riser regenerator 2; Riser regenerator 2 is burnt required air 40 and is entered along separate routes riser regenerator 2 from the three layer of air entrance 3a, 3b, the 3c that are arranged on the air-distributor 6c of riser regenerator 2 bottoms and be arranged on the wall of the axial different heights of riser regenerator, wherein, accounting for the air 40 that enters riser regenerator air total amount 20%～50% enters from air-distributor 6c, remaining air 40 enters from three layer of air entrance 3a, 3b, 3c, and the air input of each layer of air entrance 3a, 3b, 3c can flexible allocation.

In above operating process, riser regenerator 2 burning-offs more than 50% are deposited on the coke mixing on reclaimable catalyst, and half regenerated catalyst of generation enters inertial separator 38 downwards through riser regenerator 2 top exits together with regenerated flue gas and carries out separated; Isolated half regenerated catalyst enters the close phase Duan Yucong turbulent bed of turbulent bed revivifier 1 revivifier 1 bottom downwards and through air-distributor 6a, enters the further coke burning regeneration of air 40 contact of the close phase section of turbulent bed revivifier 1, and the regenerated flue gas of the regenerated flue gas of isolated riser regenerator 2 and turbulent bed revivifier 1 and a small amount of granules of catalyst of carrying secretly thereof carry out gas solid separation through revivifier primary cyclone 35a, 35b and revivifier secondary cyclone 36a, 36b successively; Isolated granules of catalyst returns to the close phase section of turbulent bed revivifier 1 through the dipleg of revivifier primary cyclone 35a, 35b and the dipleg of revivifier secondary cyclone 36a, 36b, and isolated mixed flue gas 39 enters smoke energy recovering system through flue gas collection chamber 37 and flue gas pipeline.

In above operating process, from turbulent bed revivifier 1, enter external warmer 32, catalyst mix tank 8 and stripping stage 23, the flow that enters catalyst mix tank 8 and enter the regenerated catalyst of heavy oil downer reactor 29 and lighter hydrocarbons downer reactor 9 from catalyst mix tank 8 from external warmer 32, the flow that enters the reclaimable catalyst of riser regenerator 2 from stripping stage 23 can pass through respectively external warmer catalyst inlet flow control valve 34, catalyst mix tank high temperature catalyst flow control valve 7, stripping stage regenerated catalyst flow control valve 14, external warmer catalyst outlet flow control valve 30, heavy oil reactor regenerated catalyst flow control valve 28, lighter hydrocarbons reactor regenerated catalyst flow control valve 10 and reclaimable catalyst flow control valve 16 are controlled.

In above operating process, the operational condition of heavy oil downer reactor 26 is: temperature of reaction (reactor outlet temperature) is generally 460～580 ℃, preferably 470～560 ℃, is preferably 480～540 ℃; Reaction times is generally 0.2～2.0s, and preferably 0.5～1.7s, is preferably 0.7～1.5s; Agent-oil ratio is generally 5～40, and preferably 8～30, be preferably 10～20; Catalyst activity is generally 58～75, and preferably 62～72, be preferably 65～70.

In above operating process, the operational condition of lighter hydrocarbons downer reactor 13 is: temperature of reaction (reactor outlet temperature) is generally 450～600 ℃, preferably 480～580 ℃, is preferably 500～550 ℃; Reaction times is generally 0.2～2.5s, and preferably 0.5～2.2s, is preferably 1.0～2.0s; Agent-oil ratio is generally 3～35, and preferably 5～25, be preferably 8～12; Catalyst activity is generally 58～75, and preferably 62～72, be preferably 65～70.

In above operating process, the charging of heavy oil downer reactor 26 comprises long residuum, vacuum residuum, straight-run gas oil, wax tailings, deasphalted oil, hydrogenation tail oil, recycle stock, slurry oil, crude oil, shale oil, synthetic oil, coal tar.The charging of lighter hydrocarbons downer reactor 13 comprises catalytically cracked gasoline, light FCC gasoline, coker gasoline, pneumatic press condensed oil.Catalyzer can adopt existing various catalytic cracking catalyst (for example CC-20D), can select routinely.

In above operating process, the operational condition of settling vessel 25 is: dilute phase temperature is generally 450～590 ℃; Top absolute pressure is generally 0.20～0.50Mpa, and preferably 0.25～0.45Mpa, is preferably 0.30～0.40Mpa.

In above operating process, the operational condition of stripping stage 23 is: one section of steam stripped stripping temperature is generally 480～560 ℃, and one steam stripped stripping period is for being generally 1.0～3.0min; Two sections of steam stripped stripping temperature are generally 520～620 ℃, and two steam stripped stripping periods are generally 1.0～2.0min; Stripped vapor consumption is generally 2～5kg/t _cat.

In above operating process, the operational condition of riser regenerator 2 is: temperature in is generally 500～600 ℃, preferably 520～600 ℃, is preferably 540～600 ℃; Temperature out is generally 560～720 ℃, preferably 600～680 ℃, is preferably 630～650 ℃; Average gas linear speed is generally 3.0～10.0m/s, and preferably 4.0～9.0m/s, is preferably 5.0～8.0m/s; Coke burning degree (catalyst inventory per ton burning carbon hourly amount) is generally 300～1200kg/ (th), and the time of burning is generally 5～40s; Air capacity is determined according to amount of burnt, meets the demand of more than 30% coke on burning-off mixing reclaimable catalyst; Mix reclaimable catalyst burning-off in riser regenerator 2 revivifiers and deposit superincumbent more than 30% coke.

In above operating process, the operational condition of turbulent bed revivifier 1 is: regeneration temperature is generally 580～740 ℃, preferably 620～700 ℃, is preferably 650～670 ℃; Coke burning degree is generally 0～120kg/ (th); The time of burning is generally 1.0～4.0min; Top absolute pressure is generally 0.10～0.40Mpa, and preferably 0.15～0.35Mpa, is preferably 0.20～0.30Mpa; Air capacity is determined according to amount of burnt, meets the residual coke on burning-off half regenerated catalyst.

In above operating process, the operational condition of external warmer 32 can be adjusted flexibly according to the variation of heat-obtaining load.

In above operating process, the operational condition of catalyst mix tank 8 is: average gas linear speed is generally 0.3～1.0m/s; The mixed regeneration catalyst temperature of drawing from catalyst mix tank 8 is generally 550～700 ℃, preferably 570～680 ℃, is preferably 590～650 ℃.

Embodiment 1, comparative example

On conventional double lift pipe catalytic cracking pilot plant, test.Heavy oil riser reactor processing Daqing atmospheric residue, lighter hydrocarbons riser reactor processing heavy oil catalytic gasoline that riser reactor produces, catalyzer adopts commercially available CC-20D catalytic cracking industry equilibrium catalyst.

Heavy oil riser reactor design treatment capacity is 60kg/d, simulates full freshening operation, and heavy oil feedstock mixes by feed nozzle and enters heavy oil riser reactor with recycle stock; Lighter hydrocarbons riser reactor design treatment capacity is 24kg/d.The carbon content of regenerated catalyst is 0.03w%, and micro-activity is 62.The stripping medium of stripping stage is water vapor, and stripping temperature is 500 ℃.

Catalytically cracked material character is in Table 1, and the conventional main operational condition of Double-lifted pipe catalytic cracking device of the present embodiment and product distribute in Table 2.Conventional Double-lifted pipe catalytic cracking device liquid product main character is in Table 3.

Embodiment 2

Test being similar on the Novel fluidization catalytic cracking pilot plant of Fig. 1 shown device.This Novel fluidization catalytic cracking pilot plant, heavy oil downer reactor and lighter hydrocarbons downer reactor all can need to be changed flexibly according to technique.The Daqing atmospheric residue that the processing of heavy oil downer reactor is identical with comparative example, lighter hydrocarbons downer reactor processing heavy oil catalytic gasoline that downer reactor produces, catalyzer adopts the commercially available CC-20D catalytic cracking industry equilibrium catalyst identical with comparative example.

Heavy oil downer reactor designing treatment amount is 60kg/d, simulates full freshening operation, and heavy oil feedstock mixes by feed nozzle and enters heavy oil downer reactor with recycle stock; Lighter hydrocarbons downer reactor designing treatment amount is 30kg/d, and the carbon content of regenerated catalyst is 0.03w%, and micro-activity is 66.The stripping medium of stripping stage is water vapor, and stripping temperature is 500 ℃.

The main operational condition of the present embodiment Novel fluidization catalytic cracking unit and product distribute in Table 4.Novel fluidization catalytic cracking unit liquid product main character is in Table 5.

Embodiment 3

Press embodiment 2, the key distinction is regeneration temperature, the coke burning degree of turbulent bed revivifier and riser regenerator and burns the time and the average gas linear speed of riser regenerator, the temperature of mixed regeneration catalyzer, the agent-oil ratio of heavy oil downer reactor and lighter hydrocarbons downer reactor, and the recycle ratio of heavy oil downer reactor.The main operational condition of this enforcement Novel fluidization catalytic cracking unit and product distribute in Table 6.Novel fluidization catalytic cracking unit liquid product main character is in Table 7.

Embodiment 4

Press embodiment 2, the key distinction is regeneration temperature, the coke burning degree of turbulent bed revivifier and riser regenerator and burns the time and the average gas linear speed of riser regenerator, the temperature of mixed regeneration catalyzer, the agent-oil ratio of heavy oil downer reactor and lighter hydrocarbons downer reactor, and the recycle ratio of heavy oil downer reactor.The main operational condition of this enforcement Novel fluidization catalytic cracking unit and product distribute in Table 8.Novel fluidization catalytic cracking unit liquid product main character is in Table 9.

Embodiment 5

Press embodiment 3, the key distinction is the coke burning degree of turbulent bed revivifier and burns the time, the reaction times of heavy oil downer reactor and recycle ratio.The main operational condition of this enforcement Novel fluidization catalytic cracking unit and product distribute in Table 10.Novel fluidization catalytic cracking unit liquid product main character is in Table 11.

Embodiment 6

Press embodiment 3, the key distinction is the coke burning degree of turbulent bed revivifier and burns the time, the reaction times of heavy oil downer reactor and recycle ratio.The main operational condition of this enforcement Novel fluidization catalytic cracking unit and product distribute in Table 12.Novel fluidization catalytic cracking unit liquid product main character is in Table 13.

Embodiment 7

Press embodiment 3, the key distinction is the coke burning degree of turbulent bed revivifier and riser regenerator and burns the average gas linear speed of time and riser regenerator, the temperature of reaction of heavy oil downer reactor, agent-oil ratio and recycle ratio.The main operational condition of this enforcement Novel fluidization catalytic cracking unit and product distribute in Table 14.Novel fluidization catalytic cracking unit liquid product main character is in Table 15.

Embodiment 8

Press embodiment 3, the key distinction is the coke burning degree of turbulent bed revivifier and riser regenerator and burns the average gas linear speed of time and riser regenerator, the temperature of reaction of heavy oil downer reactor, agent-oil ratio and recycle ratio.The main operational condition of this enforcement Novel fluidization catalytic cracking unit and product distribute in Table 16.Novel fluidization catalytic cracking unit liquid product main character is in Table 17.

Table 1 catalytically cracked material character

Catalytic cracking charging charging	Daqing atmospheric residue
		Density (20 ℃), kgm -3	900.2
Carbon residue, w%	4.2
		Group composition, w%
Stable hydrocarbon	62.3
		Aromatic hydrocarbons	22.6
Colloid+bituminous matter	15.1
		Sulphur content, μ gg -1	1450
Ni，μg·g -1	4.3
		V，μg·g -1	0.2

[0121]the main operational condition of table 2 embodiment 1 and product distribute

Table 3 embodiment 1 liquid product main character

The main operational condition of table 4 embodiment 2 and product distribute

Table 5 embodiment 2 liquid product main character

The main operational condition of table 6 embodiment 3 and product distribute

Table 7 embodiment 3 liquid product main character

The main operational condition of table 8 embodiment 4 and product distribute

Table 9 embodiment 4 liquid product main character

The main operational condition of table 10 embodiment 5 and product distribute

Table 11 embodiment 5 liquid product main character

The main operational condition of table 12 embodiment 6 and product distribute

Table 13 embodiment 6 liquid product main character

The main operational condition of table 14 embodiment 7 and product distribute

Table 15 embodiment 7 liquid product main character

The main operational condition of table 16 embodiment 8 and product distribute

Table 17 embodiment 8 liquid product main character

Claims (28)

1. a catalyst cracking method, is characterized in that, has the following step:

1) heavy oil feedstock (43) contacts and reacts with the regenerated catalyst from catalyst mix tank (8) in heavy oil downer reactor (26), heavy oil reactant flow enters settling vessel (25) and carries out gas solid separation, isolated heavy oil reaction oil gas enters heavy oil reaction oil gas separation column, and heavy oil reclaimable catalyst enters step 3);

2) light hydrocarbon feedstocks (44) contacts and reacts with the regenerated catalyst from catalyst mix tank (8) in lighter hydrocarbons downer reactor (13), lighter hydrocarbons reactant flow enters settling vessel (25) and carries out gas solid separation, isolated lighter hydrocarbons reaction oil gas enters lighter hydrocarbons reaction oil gas separation column, and lighter hydrocarbons reclaimable catalyst enters step 3);

3) after heavy oil reclaimable catalyst and the mixing of lighter hydrocarbons reclaimable catalyst, enter stripping stage (23) and carry out stripping, through steam stripped mixing reclaimable catalyst, carry out coke burning regeneration successively through riser regenerator (2) and turbulent bed revivifier (1), the regenerated catalyst of process two-stage regeneration enters catalyst mix tank (8).

2. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: the described regenerated catalyst through two-stage regeneration, a part enters catalyst mix tank (8) after external warmer (32) is cooling, another part enters catalyst mix tank (8) through catalyst mix tank high temperature catalyst transfer lime (5), two strands of regenerated catalysts mixed heat transfer under the disturbance of air (40) that enters catalyst mix tank (8) through air-distributor (6b), the air (40) of discharging from catalyst mix tank (8) top carries a small amount of regenerated catalyst and from bottom, enter turbulent bed revivifier (1) together with another strand of air (40).

3. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: the described regenerated catalyst through two-stage regeneration enters catalyst mix tank (8) by turbulent bed revivifier (1) through catalyst mix tank high temperature catalyst transfer lime (5).

4. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: the described regenerated catalyst from catalyst mix tank (8) enters heavy oil downer reactor (26) through heavy oil reactor catalyst transfer lime (29) downwards, by catalyst distribution plate (11a), undertaken continuing a descending segment distance after rectification and contact mixing with heavy oil feedstock (43) again, reactant flow is descending and react along heavy oil downer reactor (26).

5. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: the described regenerated catalyst from catalyst mix tank (8) enters lighter hydrocarbons downer reactor (13) through lighter hydrocarbons reactor catalyst transfer lime (9) downwards, by catalyst distribution plate (11b), undertaken continuing a descending segment distance after rectification and contact mixing with light hydrocarbon feedstocks (44) again, reactant flow is descending and react along lighter hydrocarbons downer reactor (13).

6. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: described heavy oil feedstock (43) enters heavy oil downer reactor (26) and contacts with the regenerated catalyst from catalyst mix tank (8) through being tilted to the heavy oil feedstock nozzle (27) of lower setting.

7. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: described light hydrocarbon feedstocks (44) enters lighter hydrocarbons downer reactor (13) and contacts with the regenerated catalyst from catalyst mix tank (8) through being tilted to the light hydrocarbon feedstocks nozzle (12) of lower setting.

8. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: described heavy oil feedstock (43) comprises 1～5 kind.

9. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: described light hydrocarbon feedstocks (44) comprises 1～5 kind.

10. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: described heavy oil feedstock (43), different types of can be according to reaction needed, from be arranged on heavy oil downer reactor (26) axially the heavy oil feedstock nozzle (27) of different heights enter heavy oil downer reactor (26).

11. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: described light hydrocarbon feedstocks (44), different types of can be according to reaction needed, from be arranged on lighter hydrocarbons downer reactor (13) axially the light hydrocarbon feedstocks nozzle (12) of different heights enter lighter hydrocarbons downer reactor (13).

12. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: described heavy oil reactant flow directly enters from heavy oil downer reactor (26) the thick cyclonic separator of heavy oil reactor (22) that is positioned at settling vessel (25) and carries out gas solid separation, and isolated gaseous stream enters heavy oil reactor primary cyclone (21) through connecting tube and carries out further gas solid separation.

13. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: described lighter hydrocarbons reactant flow directly enters from lighter hydrocarbons downer reactor (13) the thick cyclonic separator of lighter hydrocarbons reactor (17) that is positioned at settling vessel (25) and carries out gas solid separation, and isolated gaseous stream enters lighter hydrocarbons reactor primary cyclone (18) through connecting tube and carries out further gas solid separation.

14. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: described heavy oil reclaimable catalyst and lighter hydrocarbons reclaimable catalyst enter stripping stage (23) through each cyclone dip-leg respectively to be mixed, and prior to stripping stage (23) top, at lower temperature, with water vapor (45), carry out stripping, after enter after mix with the regenerated catalyst that enters stripping stage (23) bottom through stripping stage regenerated catalyst (4) from turbulent bed revivifier (1) stripping stage (23) bottom with water vapor (45), further carry out stripping at higher temperature.

15. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: the stripping logistics that described mixing reclaimable catalyst produces in by stripping process is divided into two portions, a part enters heavy oil reactor primary cyclone (21) and carries out gas solid separation, and another part enters lighter hydrocarbons reactor primary cyclone (18) and carries out gas solid separation.

16. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: described heavy oil reaction oil gas and the hydro carbons oil gas that gone out by stripping of a part enter heavy oil reaction oil gas separation column as heavy oil reaction oil gas separation column charging (42) through heavy oil reaction collection chamber (20) and heavy oil reaction oil gas pipeline and carries out fractionation.

17. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: the hydro carbons oil gas that described lighter hydrocarbons reaction oil gas and another part are gone out by stripping enters lighter hydrocarbons reaction oil gas separation column as lighter hydrocarbons reaction oil gas separation column charging (41) through lighter hydrocarbons reactions collection chamber (19) and lighter hydrocarbons reaction oil gas pipeline and carries out fractionation.

18. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: the steam stripped mixing reclaimable catalyst of described process enters riser regenerator (2) through reclaimable catalyst transfer lime (15) downwards, up and carry out coke burning regeneration along riser regenerator (2).

19. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: described riser regenerator (2) is burnt required air (40) and entered from 2～6 layer of air entrances (3) shunt that are arranged on the air-distributor (6c) of its bottom and be arranged on the wall of its axial different heights, wherein, accounting for the air (40) that enters riser regenerator air total amount 20%～50% enters from air-distributor (6c), remaining air (40) enters from 2～6 layer of air entrances (3), and the air input of each layer of air entrance (3) can flexible allocation.

20. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: described riser regenerator (2) burning-off more than 30% is deposited on the coke mixing on reclaimable catalyst.

21. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: half regenerated catalyst that described riser regenerator (2) generates enters inertial separator (38) downwards through riser regenerator (2) outlet and carries out gas solid separation together with regenerated flue gas, isolated half regenerated catalyst enters the air (40) that the close phase Duan Yujing air-distributor of turbulent bed revivifier (1) (6a) enters turbulent bed revivifier (1) downwards and contacts further coke burning regeneration.

22. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: the regenerated flue gas of the regenerated flue gas of described riser regenerator (2) and turbulent bed revivifier (1) and a small amount of granules of catalyst of carrying secretly thereof carry out gas solid separation through revivifier primary cyclone (35) and revivifier secondary cyclone (36) successively, isolated granules of catalyst returns to the close phase section of turbulent bed revivifier (1) through the dipleg of each cyclonic separator of revivifier, and isolated mixed flue gas (39) enters smoke energy recovering system through flue gas collection chamber (37) and flue gas pipeline.

23. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: from turbulent bed revivifier (1), enter external warmer (32), catalyst mix tank (8) and stripping stage (23), the flow that enters catalyst mix tank (8) and enter the regenerated catalyst of heavy oil downer reactor (26) and lighter hydrocarbons downer reactor (13) from catalyst mix tank (8) from external warmer (32), the flow that enters the reclaimable catalyst of riser regenerator (2) from stripping stage (23) all can pass through Flux Valve Control.

24. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: the operational condition of described heavy oil downer reactor (26) is, 460～580 ℃ of temperature of reaction, reaction times 0.2～2.0s, agent-oil ratio 5～40, reaction absolute pressure 0.10～0.40Mpa, catalyst activity 58～75.

25. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: the operational condition of described lighter hydrocarbons downer reactor (13) is, 450～600 ℃ of temperature of reaction, reaction times 0.2～2.5s, agent-oil ratio 3～35, reaction absolute pressure 0.10～0.40Mpa, catalyst activity 58～75.

26. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: the operational condition of described settling vessel (25) is, 450～590 ℃ of dilute phase temperature; Top absolute pressure 0.20～0.50Mpa.

27. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: the operational condition of described riser regenerator (2) is, 500～600 ℃ of temperature ins, 560～720 ℃ of temperature outs, average gas linear speed 3.0～10.0m/s, coke burning degree 300～1200kg/ (th), burns time 5～40s.

28. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: the operational condition of described turbulent bed revivifier (1) is, 580～740 ℃ of regeneration temperatures, coke burning degree 0～120kg/ (th), burn time 1.0～4.0min, top absolute pressure 0.10～0.40Mpa.

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