CN103540345B - 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 absence of 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 uses is varied, but the process form of its reaction-regeneration system is basically identical, most adopt single riser reactor (or single riser tube combine with fast bed two section reactor) and turbulent bed revivifier (or turbulent bed combine with fast bed two-part revivifier).Along the up reaction of riser tube after catalyzer and stock oil contact and mixes bottom riser tube, reactant flow enters settling vessel from riser tube top exit and carries out being separated of reaction oil gas and catalyzer; Isolated reclaimable catalyst enters revivifier coke burning regeneration after stripping stage one section of conventional stripping; Regenerated catalyst returns riser tube bottom cycle and uses.In above-mentioned Conventional catalytic cracking device, there is the shortcoming of following several respects: first, regenerated catalyst temperature cannot realize flexible control, regeneration temperature catalyzer is general all higher than 650 DEG C, in riser reactor, finish Contact Temperature is higher, the degree that higher finish Contact Temperature makes heat cracking reaction carry out is higher, and the degree of catalytic cracking reaction is lower, cause dry gas and coke yield is higher, total liquid yield lower (total liquid yield refers to liquefied gas yield, gasoline yield and diesel yield sum); Due to higher regenerated catalyst temperature, limit 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 weight internal circulating load of riser reactor inner catalyst and the ratio of the weight rate of heavy oil riser reactor charging), thus the number of active center making the stock oil of unit weight touch is less, this also inhibits the carrying out of catalytic cracking reaction.Second, length due to gasoline stock determines the reaction times longer (generally at about 4s) of raw material, the longer reaction times also exacerbates the secondary reaction of crack materials resultant while 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.3rd, because catalyzer in gasoline stock to move upward the landing and back-mixing that cause coked catalyst against gravity field, on gasoline stock raw material nozzles top, the coked catalyst of landing and atomized feed and cracking resultant contact reacts again, thus be degrading product slates, reduce the product selectivity of catalyzer to crack materials.4th, because turbulent bed revivifier coke burning degree is relatively low, make the catalyst inventory of revivifier higher and catalyzer is comparatively serious in the revivifier residence time longer catalyzer hydrothermal deactivation that causes.5th, the steam stripping efficiency of stripping stage is lower, cause producing more can stripping burnt.6th, catalytic gasoline cannot carry out independent upgrading, and quality is lower.

For many years, a large amount of research work has been done overcoming in the shortcoming existing for above-mentioned Conventional catalytic cracking device by domestic and international research institution.

The principal character of a kind of catalytic cracking technology disclosed in Chinese patent CN1710029 is: adopt Double-lifted pipe catalytic cracking device, independent upgrading is carried out to catalytic gasoline and utilizes the technical superiority of Double-lifted pipe catalytic cracking device, by higher for part or all of remaining activity (being equivalent to 90% of regenerator activity), temperature lower (about 500 DEG C) and return the catalyst mix device arranged bottom heavy oil riser tube through steam stripped lighter hydrocarbons riser tube reclaimable catalyst, heavy oil riser tube and heavy oil contact reacts is entered together with after mixing with the regenerated catalyst from revivifier in catalyst mix device.Owing to carrying out independent upgrading to catalytic gasoline, gasoline property is improved greatly; Simultaneously because the heat exchange action of two strands of catalyzer in mixing tank makes the temperature of mixed catalyst lower, achieve finish " low temperature contacts, high agent-oil ratio " operation, thus effectively reduce dry gas, the coke yield of device, improve total liquid yield.But there is some deficiency following in this technology: the first, and the advantage adopting the measure of lighter hydrocarbons riser tube reclaimable catalyst and regenerated catalyst hybrid cooling to cause this technology to reduce riser tube finish Contact Temperature and rising agent oil ratio only can be embodied in the catalytic cracking unit with more than two riser tubes; The second, the catalyst cracker adopted due to this technology is traditional gasoline stock, still shows and causes product slates relative poor because the reaction times is longer with catalyzer back-mixing; 3rd, exist because this technology adopts traditional turbulent bed revivifier and burn inefficient deficiency; 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 a kind of molecular sieve catalyst highly efficient regeneration catalytic cracking process technology disclosed in Chinese patent CN1210762 is: reclaimable catalyst enters external cyclone water-separator group and is separated with flue gas after the regeneration of one-level riser regenerator, then semi regeneration catalyzer 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 inclined tube bottom external warmer enters riser reactor.This technology char length controls within 10 seconds, and the coke burning degree burning carbon amounts of unit catalyst reserve (in the unit time) is about 10 times of prior art.And can effectively reduce finish Contact Temperature, rising agent oil ratio.But there is some deficiency following in this technology: the first, cannot realize the raw material short reaction time because adopting traditional gasoline stock and overcome catalyzer back-mixing.The second, technological process and complicated operation, engineering is difficult to carry out.3rd, adopt single reactor and the independent upgrading that cannot realize catalytic gasoline.

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

US Patent No. 5,462, the principal character of a kind of catalytic cracking process technology disclosed in 652 is: the first, is reduced the temperature of regenerated catalyst by the method mixed with reclaimable catalyst, reacting-settler dilute phase section arranges catalyst mix tank, from revivifier regenerated catalyst with through steam stripped reclaimable catalyst wherein mixed heat transfer backward under enter reacting-settler, second, adopt the finish way of contact different from conventional lift pipe reactor, the reaction of catalyzer and raw material and the stripping of reclaimable catalyst all carry out in reacting-settler, catalyzer is flowed downward under gravity by the mixed catalyst room central opening being located at reacting-settler top, the raw material injection direction of nozzle and catalyzer flow direction angle in 90 °, catalyzer high-speed motion reacting in the horizontal direction is carried after stock oil and catalyst exposure, reactant flow enters the plug-in cyclonic separator of reacting-settler and carries out being separated of reaction oil gas and catalyzer afterwards.Due to above feature, this technology achieves finish " low temperature contacts, high agent-oil ratio " operation, shortens the reaction times to a certain extent simultaneously, overcomes the back-mixing of catalyzer, product slates is improved.But this technology also exists, and following some is not enough: the first, owing to adopting conventional turbulent bed revivifier, it is lower that it burns efficiency.The second, reclaimable catalyst participates in reaction, reduces the average activity of mixed catalyst, also certainly will bring disadvantageous effect to product slates and product property.3rd, technological process and operation are comparatively complicated.4th, adopt single reactor and the independent upgrading that cannot realize gasoline.

US Patent No. 4, 514, the principal character of a kind of catalytic cracking process technology disclosed in 285 is: first, the finish different with conventional lift pipe reactor is adopted to contact and separate mode, regenerated catalyst enters tubular reactor downwards from regeneration disengager outlet at bottom, flow downward along downer reactor under gravity, axially in different level heights, some layers of raw material nozzles are provided with along downer reactor, 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 to contact with regenerated catalyst and mix and react along downer reactor is descending, reactant flow enters reacting-settler from downer reactor outlet at bottom, major part catalyzer continues descending until enter close phase section under gravity, reaction oil gas then significantly reduces flowing linear speed due to the rapid expansion of actual internal area, is entrained with a small amount of catalyzer and enters cyclonic separator and be separated further, the second, adopt the method introducing regenerated catalyst to improve the temperature of stripping stage, two stripping stages that set temperature is different bottom reacting-settler, 3rd, adopt riser regenerator, reclaimable catalyst enters reclaimable catalyst transfer lime under two-stage stripping is backward, and under the conveying effect of main air, enters riser regenerator carry out coke burning regeneration, the inertial separator outlet of catalyzer after regeneration through being located at riser regenerator top together with flue gas enters regeneration disengager downwards and carries out initial gross separation, and its separation principle is identical with the sepn process of reclaimable catalyst with reaction oil gas.Due to above feature, this technology shortens the reaction times to a certain extent, and can realize, to the flexible control in reaction times, overcoming the back-mixing of catalyzer simultaneously, improve steam stripping efficiency, product slates is improved, improves regeneration efficiency in addition.But this technology still exists some deficiency following: the first, and regenerated catalyst temperature cannot control flexibly, " low temperature contacts, high agent-oil ratio " operation cannot be realized, and then disadvantageous effect is brought to product slates and product property.The second, the inertial separator finish that downer reactor end adopts is separated not thorough, and the part oil gas reaction times is longer.3rd, adopt single reactor and the independent upgrading that cannot realize gasoline.

Can find out according to above-mentioned analysis, adopt an effective measure and reduce and control regenerated catalyst temperature, suitable raising catalytic cracking reaction agent-oil ratio under the prerequisite keeping catalyst activity, shorten and control the reaction times flexibly, overcome the back-mixing of catalyst in reactor, improve steam stripping efficiency and regeneration efficiency, independent upgrading is carried out to catalytic gasoline, to the product slates and product property, reduction plant energy consumption and the catalyst inventory that improve catalytic cracking reaction, slow down catalyst aging process, reduce reactor size so that reduce facility investment 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 regenerated catalyst existing for existing Conventional catalytic cracking technique 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 with the regenerated catalyst from catalyst mix tank 8 and reacts 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 with the regenerated catalyst from catalyst mix tank 8 and reacts in lighter hydrocarbons downer reactor 13, light hydrogen cracking logistics enters settling vessel 25 and carries out gas solid separation, isolated light hydrogen cracking oil gas enters light hydrogen cracking oil gas separation column, and lighter hydrocarbons reclaimable catalyst enters step 3);

3) enter stripping stage 23 and carry out stripping after heavy oil reclaimable catalyst and the mixing of lighter hydrocarbons reclaimable catalyst, carry out coke burning regeneration through riser regenerator 2 and turbulent bed revivifier 1 successively through steam stripped mixing reclaimable catalyst, the regenerated catalyst through 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 cools, 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 entering 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 enter turbulent bed revivifier 1 from bottom 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, continue a descending segment distance after carrying out rectification by catalyst distribution plate 11a 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 light hydrogen cracking device catalyst transport 9 downwards, continue a descending segment distance after carrying out rectification by catalyst distribution plate 11b and contact mixing with light hydrocarbon feedstocks 44 again, reactant flow is descending and react along lighter hydrocarbons downer reactor 13.

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

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

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

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

Described heavy oil reactant flow directly enters the thick cyclonic separator 22 of the heavy oil reactor being positioned at settling vessel 25 from heavy oil downer reactor 26 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 light hydrogen cracking logistics directly enters the thick cyclonic separator 17 of the light hydrogen cracking device being positioned at settling vessel 25 from lighter hydrocarbons downer reactor 13 and carries out gas solid separation, and isolated gaseous stream enters light hydrogen cracking device 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 and mix, and carry out stripping with water vapor 45 at a lower temperature prior to stripping stage 23 top, after enter stripping stage 23 bottom and after the regenerated catalyst that stripping stage regenerated catalyst 4 enters stripping stage 23 bottom mixes, carry out stripping further with water vapor 45 with from turbulent bed revivifier 1 at a higher temperature.

Described enters stripping stage 23 through dipleg by the isolated heavy oil reclaimable catalyst of the thick cyclonic separator of heavy oil reactor 22 after being located at the pre-stripping of pre-stripper below the thick cyclonic separator of heavy oil reactor 22, after being located at the pre-stripping of pre-stripper below the thick cyclonic separator of light hydrogen cracking device 17, stripping stage 23 is entered through dipleg by the isolated lighter hydrocarbons reclaimable catalyst of the thick cyclonic separator of light hydrogen cracking device 17, stripping stage 23 is entered through dipleg respectively by the isolated reclaimable catalyst of heavy oil reactor primary cyclone 21 with by the isolated reclaimable catalyst of light hydrogen cracking device primary cyclone 18, above-mentioned several strands of reclaimable catalysts mix at stripping stage 23, then stripping is carried out with water vapor 45 at a lower temperature prior to stripping stage 23 top, after the regenerated catalyst that stripping stage regenerated catalyst 4 enters stripping stage 23 bottom mixes, stripping is carried out further with water vapor 45 at a higher temperature entering stripping stage 23 bottom with from turbulent bed revivifier 1.

The stripping stream 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 light hydrogen cracking device primary cyclone 18 and carries out gas solid separation.

Enter heavy oil reactor primary cyclone 21 through connecting tube after the described stripping stream produced in pre-stripping process by the isolated heavy oil reclaimable catalyst of the thick cyclonic separator of heavy oil reactor 22 mixes with the isolated gaseous stream of the thick cyclonic separator of heavy oil reactor 22 and carry out further gas solid separation, enter light hydrogen cracking device primary cyclone 18 through connecting tube after the stripping stream produced mixes with the isolated gaseous stream of the thick cyclonic separator of light hydrogen cracking device 17 carry out further gas solid separation by the isolated lighter hydrocarbons reclaimable catalyst of the thick cyclonic separator of light hydrogen cracking device 17 in pre-stripping process.

Described heavy oil reaction oil gas and a part are entered 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 by the hydro carbons oil gas that stripping goes out and carry out fractionation.

Described light hydrogen cracking oil gas and another part are entered light hydrogen cracking oil gas separation column as light hydrogen cracking oil gas separation column charging 41 through light hydrogen cracking collection chamber 19 and light hydrogen cracking gas pipeline by the hydro carbons oil gas that stripping goes out and carry out fractionation.

Described enters riser regenerator 2 through reclaimable catalyst transfer lime 15 downwards through steam stripped mixing reclaimable catalyst, 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 the air-distributor 6c be arranged on bottom it and 2 ~ 6 layer of air entrances 3 arranged the wall of axially different heights, wherein, account for the air 40 entering riser regenerator air total amount 20% ~ 50% to enter 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-off more than 30% is deposited on the coke on mixing reclaimable catalyst.

The semi regeneration catalyzer that described riser regenerator (2) generates exports through riser regenerator 2 and enters inertial separator 38 downwards and carry out gas solid separation together with regenerated flue gas, and isolated semi regeneration catalyzer enters the air 40 that turbulent bed revivifier 1 close phase Duan Yujing air-distributor 6a enters turbulent bed revivifier 1 downwards and contacts further coke burning regeneration.

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 carried secretly thereof carry out gas solid separation through revivifier primary cyclone 35 and revivifier secondary cyclone 36 successively, isolated granules of catalyst returns 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.

External warmer 32, catalyst mix tank 8 and stripping stage 23 is entered from turbulent bed revivifier 1, enter catalyst mix tank 8 from external warmer 32 and enter the flow of regenerated catalyst of heavy oil downer reactor 26 and lighter hydrocarbons downer reactor 13 from catalyst mix tank 8, the flow entering 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, temperature of reaction 460 ~ 580 DEG C, 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, temperature of reaction 450 ~ 600 DEG C, 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, dilute phase temperature 450 ~ 590 DEG C; Top absolute pressure 0.20 ~ 0.50Mpa.

The operational condition of described riser regenerator 2 is, temperature in 500 ~ 600 DEG C, temperature out 560 ~ 720 DEG C, average gas linear speed 3.0 ~ 10.0m/s, coke burning degree 300 ~ 1200kg/th, char length 5 ~ 40s.

The operational condition of described turbulent bed revivifier 1 is, regeneration temperature 580 ~ 740 DEG C, coke burning degree 0 ~ 120kg/th, char length 1.0 ~ 4.0min, top absolute pressure 0.10 ~ 0.40Mpa.

Compared with existing Conventional catalytic cracking technology, the present invention has following beneficial effect:

1. the downer reactor owing to adopting the finish contact reacts time shorter, effectively can reduce secondary reaction, control depth of conversion, and overcome the catalyzer back-mixing disadvantageous effect next to cracking reaction zone, remarkable reduction 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., owing to adopting riser regenerator to combine with turbulent bed revivifier the method used, both can improve coke burning degree and burn efficiency, can regeneration effect have been ensured again, thus the shortening residence time of catalyzer in revivifier, slow 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 external warmer cooling regenerated catalyst, effectively can control regenerated catalyst temperature, realize regenerated catalyst to operate with " low temperature contacts; high agent-oil ratio " of raw material, and then suppression heat cracking reaction, promote catalytic cracking reaction, reduce dry gas and coke yield, reduce plant energy consumption simultaneously.

4. owing to adopting the method for two-stage stripping, give full play to physics stripping and the steam stripped dual function of chemistry, significantly can improve Srteam Stripping effect, overcome catalyst recirculation amount greatly to the disadvantageous effect that stripping operation brings, thus reduce can stripping burnt, improve yield of light oil further.

5. owing to adopting double-reactor and two fractionating column system, independent upgrading can be carried out under appropriate conditions to catalytic gasoline or other lighter hydrocarbons, thus 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 the device reaction-regeneration system realizing 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. light hydrogen cracking device regenerated catalyst, 10. light hydrogen cracking device 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. light hydrogen cracking device, 18. light hydrogen cracking device primary cyclones, 19. light hydrogen cracking 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. light hydrogen cracking 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 realizing catalyst cracking method of the present invention forms primarily 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 above settling vessel 25, and both adopt coaxial-type to arrange; Turbulent bed revivifier 1 close phase section is connected with the close phase pars infrasegmentalis of settling vessel 25 with external warmer 32 top, catalyst mix tank 8 top respectively by external warmer catalyst inlet pipe 33, catalyst mix tank high temperature catalyst transfer lime 5 and stripping stage regenerated catalyst 4, is connected bottom external warmer 32 by external warmer catalyst outlet pipe 31 with catalyst mix tank 8 top; Be connected with lighter hydrocarbons downer reactor 13 top with heavy oil downer reactor 26 top with light hydrogen cracking device regenerated catalyst 9 respectively by heavy oil reactor regenerated catalyst 29 bottom catalyst mix tank 8; Settling vessel 25 dilute phase section is entered respectively bottom heavy oil downer reactor 26 He bottom lighter hydrocarbons downer reactor 13; The close phase section of settling vessel 25 is stripping stage 23, is connected bottom stripping stage 23 by reclaimable catalyst transfer lime 15 with bottom riser regenerator 2; Riser regenerator 2 top is 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 entrance all adopt to flood head piece form and arrange 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, light hydrogen cracking device regenerated catalyst 9 and reclaimable catalyst transfer lime 15 are 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, light hydrogen cracking device regenerated catalyst flow control valve 10 and reclaimable catalyst flow control valve 16, seven described variable valve are fluidized solids flow control valve, particularly guiding valve, the outlet of external warmer catalyst outlet pipe 31 is positioned at the axial centre region on catalyst mix tank 8 top, and the outlet of stripping stage regenerated catalyst 4 is positioned at the axial centre region of stripping stage 23 bottom.

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, air-distributor 6b is provided with bottom catalyst mix tank 8, top is provided with venting port, and this venting port is connected by the air inlet pipeline of air line with turbulent bed regenerator bottoms.

Heavy oil downer reactor 26 is identical with lighter hydrocarbons downer reactor 13 structure, is composed in series by finish mixing tube and reactant flow delivery line, two finish mixing tubes are vertically arranged, and its top entry is connected with the outlet at bottom of heavy oil reactor regenerated catalyst 29 with light hydrogen cracking device regenerated catalyst 9 respectively, its top is equipped with dome head, and bottom is equipped with conical head, catalyst distribution plate 11a and catalyst distribution plate 11b is respectively equipped with below the entrance of two finish mixing tubes, and the wall of axially different heights is respectively equipped with three layers of heavy oil feedstock nozzle 27a, 27b, 27c and three layer of light hydrocarbon feedstocks nozzle 12a, 12b, 12c, wherein every layer of heavy oil feedstock nozzle 27a, 27b, 27c and light hydrocarbon feedstocks nozzle 12a, 12b, 12c comprises again heavy oil feedstock nozzle 27 and the light hydrocarbon feedstocks nozzle 12 that six become matrix distribution respectively, with the heavy oil feedstock nozzle of layer and light hydrocarbon feedstocks nozzle arrangements consistent size and two one group respectively with two finish mixing tube central shafts for symmetry axis is symmetrical arranged, 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 two finish mixing tube central shafts respectively, each layer 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 section through wall, and its outlet is connected with light hydrogen cracking device thick cyclonic separator 17 entrance with heavy oil reactor thick cyclonic separator 22 entrance respectively.

In settling vessel 25, except the thick cyclonic separator of heavy oil reactor 22 and the thick cyclonic separator 17 of light hydrogen cracking device, be also provided with a heavy oil reactor primary cyclone 21 and a light hydrogen cracking device primary cyclone 18; Heavy oil reactor thick cyclonic separator 22 outlet conduit and heavy oil reactor primary cyclone 21 inlet duct socket-connect, namely heavy oil reactor thick cyclonic separator 22 outlet conduit is outer little through proportion oil reactor primary cyclone 21 inlet duct internal diameter, and insert wherein, fix and centering with auxiliary inner member simultaneously, pipeline annular space is connected with settling vessel 25 dilute phase section as the entrance of stripping stream, and heavy oil reactor primary cyclone 21 exports and reacts collection chamber 20 by closed conduct and heavy oil and be connected; Light hydrogen cracking device thick cyclonic separator 17 outlet conduit and light hydrogen cracking device primary cyclone 18 inlet duct socket-connect, namely light hydrogen cracking device thick cyclonic separator 17 outlet conduit is outer through less than light hydrogen cracking device primary cyclone 18 inlet duct internal diameter, and insert wherein, fix and centering with auxiliary inner member simultaneously, pipeline annular space is connected with settling vessel 25 dilute phase section with the entrance as stripping stream, and light hydrogen cracking device primary cyclone 18 is exported and is connected with light hydrogen cracking collection chamber 19 by closed conduct; Heavy oil reaction collection chamber 20 and light hydrogen cracking collection chamber 19 are all positioned at settling vessel 25 top, be separate two independently spaces, be connected with light hydrogen cracking oil gas separation column with heavy oil reaction oil gas separation column with light hydrogen cracking gas pipeline respectively by heavy oil reaction oil gas pipeline.

Be provided with two steam distributors 24a, 24b in stripping stage 23, wherein steam distributor 24a is arranged on above stripping stage regenerated catalyst 4 outlet at bottom, and steam distributor 24b is arranged on bottom stripping stage 23.

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

Air-distributor 6a is provided with bottom the close phase section of turbulent bed revivifier 1; Its dilute phase section top is provided with two groups of revivifier two stage cyclone separators, wherein, revivifier primary cyclone 35a, 35b entrance is 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 being 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, light hydrogen cracking device 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 light hydrogen cracking device, heavy oil reactor primary cyclone 21, light hydrogen cracking device 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 according to the service temperature at each position and catalyst stream moving-wire is fast and chips washing system is determined.

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 reactant flow delivery line and leads to internal diameter, 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 reactant flow delivery line and leads to internal diameter, 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 part can be determined according to the design and calculation method of the design linear speed of the design reaction times of each reactor, reactor each several part and the pressure equilibrium parameter request of whole catalytic cracking unit and the concrete structure size employing Conventional riser FCC riser of settling vessel; The concrete internal diameter of heavy oil downer reactor 26 and lighter hydrocarbons downer reactor 13 each several part can adopt the design and calculation method of Conventional riser FCC riser to be determined according to parameter requests such as the design linear speeds 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 be beneficial to descending reactant flow derives bottom finish mixing tube.

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.

The raw material injection direction of heavy oil feedstock nozzle 27a, 27b, 27c and light hydrocarbon feedstocks nozzle 12a, 12b, 12c and the angle of horizontal plane are generally 45 ° ~ 80 °, are beneficial to the mixing of finish and the fluidisation of catalyzer; The reaction times of its concrete rational height required for each stock charging and the parameter such as the design linear speed of downer reactor each several part and the length of reactant flow delivery line are carried out calculating and are determined.

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 catalytic cracking raw material nozzles; Its concrete structure size can 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 catalytic cracking raw material nozzles 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 light hydrogen cracking device 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, meet the general feature of 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 space layout of the catalyst recirculation amount of each catalyst recirculation circuit of device and device.

The length of the vertical section of riser regenerator 2 is generally 50 ~ 65m, and its internal diameter is generally 1200 ~ 8000mm; The length of riser regenerator 2 horizontal section 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, the method for calculation of dilute catalyst phase transport pipe can be adopted 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; The concrete rational height of three layer of air entrance 3a, 3b, 3c on riser regenerator 2 wall can according to riser regenerator 2 bottom air sparger and the air output of each layer of air entrance and the coke burning degree in conjunction with each section of riser regenerator 2 determined by calculating.

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 section, and its internal diameter is not more than the internal diameter of riser regenerator 2 horizontal section.

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 realize the parameters such as time required for Homogeneous phase mixing according to the total catalyst internal circulating load of two reactors and cold and hot catalyzer and carry out calculating and determine.

Settling vessel 25 belongs to existing conventional equipment, meets the general feature of conventional lift 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 general feature of conventional lift 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 of heavy oil reactor 22, the thick cyclonic separator of light hydrogen cracking device 17, heavy oil reactor primary cyclone 21, light hydrogen cracking device 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 of heavy oil reactor regenerated catalyst 29, light hydrogen cracking device regenerated catalyst 9, the setting of stripping stage regenerated catalyst 4 ingress belongs to existing conventional equipment, and its concrete structure size can adopt the existing design and calculation method flooding stream bucket be determined according to the operational condition of device.

The catalyst cracking method of the present invention adopting Fig. 1 shown device to carry out is as follows: a part of regenerated catalyst in turbulent bed revivifier 1 enters catalyst mix tank 8 and mixes with the regenerated catalyst that the another part from turbulent bed revivifier 1 is not cooled and carry out heat exchange after external warmer 32 cools; 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 reacts, and another stock-traders' know-how light hydrogen cracking device regenerated catalyst 9 enters lighter hydrocarbons downer reactor 13 and light hydrocarbon feedstocks 44 contact reacts; After reaction terminates, two bursts of reactant flow enter settling vessel 25 respectively the oil point separator that revolves special separately 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 carry out two-stage stripping; The semi regeneration catalyzer that riser regenerator 2 generates enters turbulent bed revivifier 1 coke burning regeneration further; 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 light hydrogen cracking oil gas and another part are gone out by stripping is as light hydrogen cracking oil gas separation column charging 41.

In above operating process, enter the different regenerated catalyst of two bursts of temperature of catalyst mix tank 8 Homogeneous phase mixing carry out heat exchange under the perturbation action of air 40 entering catalyst mix tank 8 through air-distributor 6b through external warmer catalyst outlet pipe 31 and catalyst mix tank high temperature catalyst transfer lime 5 respectively; From catalyst mix tank 8 top discharge air 40 carry a small amount of regenerated catalyst after air line converges with another strand of air 40 together with enter turbulent bed revivifier 1 from bottom.

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 light hydrogen cracking device regenerated catalyst 9 downwards respectively; And carry out rectification by catalyst distribution plate 11a and catalyst distribution plate 11b respectively, continue a descending segment distance after rectification to contact with light hydrocarbon feedstocks 44 with heavy oil feedstock 43 respectively again and mix, afterwards two bursts of reactant flow respectively along heavy oil downer reactor 26 and lighter hydrocarbons downer reactor 13 descending and react.

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 enter heavy oil downer reactor 26 and contacts with regenerated catalyst by any one deck in three layers of heavy oil feedstock nozzle 27a, 27b, 27c from the wall being arranged on the axial different heights of heavy oil downer reactor 26, and any one light hydrocarbon feedstocks 44 can enter lighter hydrocarbons downer reactor 13 and contact with regenerated catalyst by any one deck in three layers of light hydrocarbon feedstocks nozzle 12a, 12b, 12c from the wall being arranged on the axial different heights of lighter hydrocarbons downer reactor 13.

In above operating process, the reactant flow delivery line of heavy oil downer reactor 26 reactant flow bottom heavy oil downer reactor 26 directly enters the thick cyclonic separator 22 of the heavy oil reactor being 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 bottom lighter hydrocarbons downer reactor 13 directly enters the thick cyclonic separator 17 of the light hydrogen cracking device being positioned at settling vessel 25 and carries out gas solid separation, and isolated gaseous stream enters light hydrogen cracking device primary cyclone 18 through connecting tube and carries out further gas solid separation; Stripping stream (the hydro carbons oil gas gone out by stripping and a small amount of catalyzer carried 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 light hydrogen cracking device primary cyclone 18 and carries out gas solid separation; Entered heavy oil reaction oil gas separation column by the hydro carbons oil gas that stripping goes out through heavy oil reaction collection chamber 20 and heavy oil reaction oil gas pipeline by the isolated heavy oil reaction oil gas of heavy oil reactor primary cyclone 21 and a part and carry out fractionation, entered light hydrogen cracking oil gas separation column by the hydro carbons oil gas that stripping goes out through light hydrogen cracking collection chamber 19 and light hydrogen cracking gas pipeline by the isolated light hydrogen cracking oil gas of light hydrogen cracking device primary cyclone 18 and another part and carry 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 and mix, prior to stripping stage 23 top lower temperature with under water vapor 45 carry out stripping, after enter stripping stage 23 bottom and after one regenerated catalyst that stripping stage regenerated catalyst 4 enters stripping stage bottom mixes, carry out stripping further with water vapor 45 with from turbulent bed revivifier 1 at a higher temperature.

In above operating process, enter riser regenerator 2 through reclaimable catalyst transfer lime 15 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 riser regenerator 2 along separate routes from the air-distributor 6c be arranged on bottom riser regenerator 2 and three layer of air entrance 3a, 3b, the 3c be arranged on the wall of the axial different heights of riser regenerator, wherein, account for the air 40 entering riser regenerator air total amount 20% ~ 50% to enter 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-off more than 50% is deposited on the coke on mixing reclaimable catalyst, and the semi regeneration catalyzer of generation enters inertial separator 38 downwards through riser regenerator 2 top exit together with regenerated flue gas and is separated; Isolated semi regeneration catalyzer enters the air 40 entering turbulent bed revivifier 1 close phase section through air-distributor 6a bottom turbulent bed revivifier 1 close phase Duan Yucong turbulent bed revivifier 1 downwards and contacts further coke burning regeneration, and the regenerated flue gas of isolated riser regenerator 2 and the regenerated flue gas of turbulent bed revivifier 1 and a small amount of granules of catalyst carried 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 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, external warmer 32 is entered from turbulent bed revivifier 1, catalyst mix tank 8 and stripping stage 23, enter catalyst mix tank 8 from external warmer 32 and enter the flow of regenerated catalyst of heavy oil downer reactor 29 and lighter hydrocarbons downer reactor 9 from catalyst mix tank 8, the flow entering the reclaimable catalyst of riser regenerator 2 from stripping stage 23 can respectively by 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, light hydrogen cracking device regenerated catalyst flow control valve 10 and reclaimable catalyst flow control valve 16 control.

In above operating process, the operational condition of heavy oil downer reactor 26 is: temperature of reaction (reactor outlet temperature) is generally 460 ~ 580 DEG C, preferably 470 ~ 560 DEG C, is preferably 480 ~ 540 DEG C; Reaction times is generally 0.2 ~ 2.0s, 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 DEG C, preferably 480 ~ 580 DEG C, is preferably 500 ~ 550 DEG C; Reaction times is generally 0.2 ~ 2.5s, 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 (such as CC-20D), can select routinely.

In above operating process, the operational condition of settling vessel 25 is: dilute phase temperature is generally 450 ~ 590 DEG C; Top absolute pressure is generally 0.20 ~ 0.50Mpa, 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 DEG C, and one section of steam stripped stripping time is for being generally 1.0 ~ 3.0min; Two sections of steam stripped stripping temperature are generally 520 ~ 620 DEG C, and two sections of steam stripped stripping time 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 DEG C, preferably 520 ~ 600 DEG C, is preferably 540 ~ 600 DEG C; Temperature out is generally 560 ~ 720 DEG C, preferably 600 ~ 680 DEG C, is preferably 630 ~ 650 DEG C; Average gas linear speed is generally 3.0 ~ 10.0m/s, preferably 4.0 ~ 9.0m/s, is preferably 5.0 ~ 8.0m/s; Coke burning degree (catalyst inventory per ton burning carbon amounts hourly) is generally 300 ~ 1200kg/ (th), and char length is generally 5 ~ 40s; Air capacity is determined according to amount of burnt, meets the demand of the coke of on burning-off mixing reclaimable catalyst more than 30%; The coke of mixing reclaimable catalyst burning-off deposition superincumbent more than 30% in riser regenerator 2 revivifier.

In above operating process, the operational condition of turbulent bed revivifier 1 is: regeneration temperature is generally 580 ~ 740 DEG C, preferably 620 ~ 700 DEG C, is preferably 650 ~ 670 DEG C; Coke burning degree is generally 0 ~ 120kg/ (th); Char length is generally 1.0 ~ 4.0min; Top absolute pressure is generally 0.10 ~ 0.40Mpa, 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 semi regeneration catalyzer.

In above operating process, the operational condition of external warmer 32 can adjust flexibly according to the change 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 DEG C, preferably 570 ~ 680 DEG C, is preferably 590 ~ 650 DEG C.

Embodiment 1, comparative example

Conventional double lift pipe catalytic cracking pilot plant is tested.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 the operation of full freshening, enters heavy oil riser reactor after heavy oil feedstock mixes with recycle stock through feed nozzle; 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 fluid of stripping stage is water vapor, and stripping temperature is 500 DEG C.

Catalytically cracked material character is in table 1, and the conventional Double-lifted pipe catalytic cracking device prevailing operating conditions of the present embodiment and product slates are in table 2.Conventional Double-lifted pipe catalytic cracking device liquid product main character is in table 3.

Embodiment 2

The Novel fluidization catalytic cracking pilot plant being similar to Fig. 1 shown device is tested.This Novel fluidization catalytic cracking pilot plant, heavy oil downer reactor and lighter hydrocarbons downer reactor all can need to change 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 the operation of full freshening, enters heavy oil downer reactor after heavy oil feedstock mixes with recycle stock through feed nozzle; 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 fluid of stripping stage is water vapor, and stripping temperature is 500 DEG C.

The present embodiment Novel fluidization catalytic cracking unit prevailing operating conditions and product slates are in table 4.Novel fluidization catalytic cracking unit liquid product main character is in table 5.

Embodiment 3

By embodiment 2, the key distinction is the average gas linear speed of the regeneration temperature of turbulent bed revivifier and riser regenerator, coke burning degree and char length and 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.This enforcement Novel fluidization catalytic cracking unit prevailing operating conditions and product slates are in table 6.Novel fluidization catalytic cracking unit liquid product main character is in table 7.

Embodiment 4

By embodiment 2, the key distinction is the average gas linear speed of the regeneration temperature of turbulent bed revivifier and riser regenerator, coke burning degree and char length and 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.This enforcement Novel fluidization catalytic cracking unit prevailing operating conditions and product slates are in table 8.Novel fluidization catalytic cracking unit liquid product main character is in table 9.

Embodiment 5

By embodiment 3, the key distinction is coke burning degree and the char length of turbulent bed revivifier, the reaction times of heavy oil downer reactor and recycle ratio.This enforcement Novel fluidization catalytic cracking unit prevailing operating conditions and product slates are in table 10.Novel fluidization catalytic cracking unit liquid product main character is in table 11.

Embodiment 6

By embodiment 3, the key distinction is coke burning degree and the char length of turbulent bed revivifier, the reaction times of heavy oil downer reactor and recycle ratio.This enforcement Novel fluidization catalytic cracking unit prevailing operating conditions and product slates are in table 12.Novel fluidization catalytic cracking unit liquid product main character is in table 13.

Embodiment 7

By embodiment 3, the key distinction is the coke burning degree of turbulent bed revivifier and riser regenerator and the average gas linear speed of char length and riser regenerator, the temperature of reaction of heavy oil downer reactor, agent-oil ratio and recycle ratio.This enforcement Novel fluidization catalytic cracking unit prevailing operating conditions and product slates are in table 14.Novel fluidization catalytic cracking unit liquid product main character is in table 15.

Embodiment 8

By embodiment 3, the key distinction is the coke burning degree of turbulent bed revivifier and riser regenerator and the average gas linear speed of char length and riser regenerator, the temperature of reaction of heavy oil downer reactor, agent-oil ratio and recycle ratio.This enforcement Novel fluidization catalytic cracking unit prevailing operating conditions and product slates are in table 16.Novel fluidization catalytic cracking unit liquid product main character is in table 17.

Table 1 catalytically cracked material character

Catalytic cracking feeds charging	Daqing atmospheric residue
		Density (20 DEG C), 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

Table 2 embodiment 1 prevailing operating conditions and product slates

Table 3 embodiment 1 liquid product main character

Table 4 embodiment 2 prevailing operating conditions and product slates

Table 5 embodiment 2 liquid product main character

Table 6 embodiment 3 prevailing operating conditions and product slates

Table 7 embodiment 3 liquid product main character

Table 8 embodiment 4 prevailing operating conditions and product slates

Table 9 embodiment 4 liquid product main character

Table 10 embodiment 5 prevailing operating conditions and product slates

Table 11 embodiment 5 liquid product main character

Table 12 embodiment 6 prevailing operating conditions and product slates

Table 13 embodiment 6 liquid product main character

Table 14 embodiment 7 prevailing operating conditions and product slates

Table 15 embodiment 7 liquid product main character

Table 16 embodiment 8 prevailing operating conditions and product slates

Table 17 embodiment 8 liquid product main character

Claims (27)

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

1) heavy oil feedstock (43) contacts with the regenerated catalyst from catalyst mix tank (8) and reacts 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 with the regenerated catalyst from catalyst mix tank (8) and reacts in lighter hydrocarbons downer reactor (13), light hydrogen cracking logistics enters settling vessel (25) and carries out gas solid separation, isolated light hydrogen cracking oil gas enters light hydrogen cracking oil gas separation column, and lighter hydrocarbons reclaimable catalyst enters step 3);

3) enter stripping stage (23) and carry out stripping after heavy oil reclaimable catalyst and the mixing of lighter hydrocarbons reclaimable catalyst, coke burning regeneration is carried out through riser regenerator (2) and turbulent bed revivifier (1) successively through steam stripped mixing reclaimable catalyst, a regenerated catalyst part through two-stage regeneration enters catalyst mix tank (8) after external warmer (32) 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) entering 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 enter turbulent bed revivifier (1) from bottom together with another strand of air (40).

2. according to a kind of catalyst cracking method according to 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).

3. according to a kind of catalyst cracking method according to 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, continue a descending segment distance after carrying out rectification by catalyst distribution plate (11a) to contact with heavy oil feedstock (43) and mix, reactant flow is descending and react along heavy oil downer reactor (26).

4. according to a kind of catalyst cracking method according to claim 1, it is characterized in that: the described regenerated catalyst from catalyst mix tank (8) enters lighter hydrocarbons downer reactor (13) through light hydrogen cracking device catalyst transport (9) downwards, continue a descending segment distance after carrying out rectification by catalyst distribution plate (11b) to contact with light hydrocarbon feedstocks (44) and mix, reactant flow is descending and react along lighter hydrocarbons downer reactor (13).

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

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

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

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

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

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

11. according to a kind of catalyst cracking method according to 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) being 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.

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

13. according to a kind of catalyst cracking method according to 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 and mix, and use water vapor (45) to carry out stripping at a lower temperature prior to stripping stage (23) top, after enter stripping stage (23) bottom and after the regenerated catalyst that stripping stage regenerated catalyst (4) enters stripping stage (23) bottom mixes, use water vapor (45) to carry out stripping further with from turbulent bed revivifier (1) at a higher temperature.

14. according to a kind of catalyst cracking method according to claim 1, it is characterized in that: the stripping stream 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 light hydrogen cracking device primary cyclone (18) and carries out gas solid separation.

15., according to a kind of catalyst cracking method according to claim 1, is characterized in that: described heavy oil reaction oil gas and a part are entered 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 by the hydro carbons oil gas that stripping goes out and carry out fractionation.

16., according to a kind of catalyst cracking method according to claim 1, is characterized in that: described light hydrogen cracking oil gas and another part are entered light hydrogen cracking oil gas separation column as light hydrogen cracking oil gas separation column charging (41) through light hydrogen cracking collection chamber (19) and light hydrogen cracking gas pipeline by the hydro carbons oil gas that stripping goes out and carry out fractionation.

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

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

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

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

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

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

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

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

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

26. according to a kind of catalyst cracking method according to claim 1, it is characterized in that: the operational condition of described riser regenerator (2) is, temperature in 500 ~ 600 DEG C, temperature out 560 ~ 720 DEG C, average gas linear speed 3.0 ~ 10.0m/s, coke burning degree 300 ~ 1200kg/ (th), char length 5 ~ 40s.

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