CN104342197A - Double lift pipe catalytic cracking method and device - Google Patents

Double lift pipe catalytic cracking method and device Download PDF

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Publication number
CN104342197A
CN104342197A CN201310346814.6A CN201310346814A CN104342197A CN 104342197 A CN104342197 A CN 104342197A CN 201310346814 A CN201310346814 A CN 201310346814A CN 104342197 A CN104342197 A CN 104342197A
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China
Prior art keywords
heavy oil
turbulent bed
lighter hydrocarbons
riser tube
catalyst
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CN201310346814.6A
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CN104342197B (en
Inventor
陈曼桥
武立宪
王文柯
樊麦跃
张亚西
汤海涛
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Sinopec Engineering Group Co Ltd
Sinopec Luoyang Guangzhou Engineering Co Ltd
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Sinopec Luoyang Petrochemical Engineering Corp
Sinopec Engineering Group Co Ltd
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process

Abstract

The invention provides a double lift pipe catalytic cracking method and device. The method comprises the following steps: respectively carrying out heavy oil catalytic cracking and light hydrocarbon catalytic modification by adopting two lift pipes, wherein the contact time of an oil agent for heavy oil catalytic cracking is 0.2-1.5s; performing gas-solid separation to two reactant flows respectively through special cyclone separators; fractioning two flows of reactive oil-gas respectively through special fractioning towers; stripping to-be-regenerated catalysts generated in the two lift pipes, then entering a first turbulent bed generator and a second turbulent bed generator for performing reverse smoke flow for burning more than 90% of generated coke, leading semi-regenerated catalysts to enter the second turbulent bed generator so as to contact with reverse main air flow for burning the remaining generated coke and performing heat-exchange and cooling, and leading the cooled regenerated catalysts to return the two lift pipes for recycling, wherein main air is directly delivered to the second turbulent bed generator during the regeneration process. The invention further discloses a double lift pipe catalytic cracking device for realizing the method.

Description

A kind of double lift pipe catalytic cracking method and device thereof
Technical field
The present invention relates to a kind of double lift pipe catalytic cracking method and the device thereof of petroleum chemical industry.
Background technology
At present, the shortcoming of following several respects of Conventional catalytic cracking device ubiquity that petroleum chemical industry uses: first, limit by regeneration kinetics, regeneration temperature is higher, causes the regenerated catalyst temperature higher (generally at about 700 DEG C) participating in reaction; Limit by device thermal equilibrium, make the agent-oil ratio of heavy oil riser tube relatively little, general total agent-oil ratio is 5 ~ 8 (total agent-oil ratio of riser tube is the weight internal circulating load of riser tube inner catalyst and the ratio of the weight rate summation of each stock charging of riser tube), thus the number of active center making the heavy oil feed of unit weight touch is less, this inhibits catalytic cracking reaction to a great extent.Meanwhile, in riser tube, the Contact Temperature of finish is higher, facilitates heat cracking reaction to a certain extent.Second, the time of finish contact is longer (generally at about 4s, s is second), this also exacerbates the secondary reaction of cracking resultant while improving feedstock conversion, make reacted gas (comprising dry gas and liquefied gas) higher with the productive rate of coke, the yield of vapour, diesel oil distillate is lower; Also make the inferior quality of catalytic diesel oil, be not suitable as vehicle fuel blending component.3rd, 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.
A kind of catalyst cracking method and device disclosed in Chinese patent CN100338185C, its technical characteristics is: adopt Double-lifted pipe catalytic cracking device, utilize the technical superiority of Double-lifted pipe catalytic cracking device, by higher for part or all of remaining activity (being about equivalent to 90% of regenerated catalyst activity), temperature lower (about 500 DEG C) and send into the catalyst mix device bottom heavy oil riser tube through steam stripped lighter hydrocarbons riser tube reclaimable catalyst, heavy oil riser tube is entered together with after mixing with the regenerated catalyst from revivifier in catalyst mix device, contact with heavy oil feed.Due to the heat exchange action of two strands of catalyzer in mixing tank, make the temperature of mixed catalyst lower, achieve heavy oil riser tube " contact of finish low temperature, high agent-oil ratio " operation, reduce dry gas, coke yield to a certain extent, improve total liquid yield.This technology also exists some deficiency following: the first, and lighter hydrocarbons reclaimable catalyst mixes with regenerated catalyst, reduces the activity of the catalyzer participating in reaction in heavy oil riser tube to a certain extent, brings disadvantageous effect to product slates and product property.The second, what this technology adopted is traditional riser catalytic cracking reactor, and nozzle setting position is lower, and in fact the finish of heavy oil riser tube can only control to be 2 ~ 4s duration of contact, and the reaction times being shorter than 2s is difficult to realize.Because finish is longer for duration of contact, cause the product slates of heavy oil riser tube relative with the character of catalytic diesel oil poor.
A kind of apparatus and method reducing temperature of catalytic cracking regenerated catalyst disclosed in Chinese patent CN101575534B, its technical characteristics is: arrange a regenerated catalyst water cooler in the below of revivifier, regenerated catalyst in revivifier enters wherein through regenerated catalyst, passes into cooling main air mixed heat transfer in regenerated catalyst water cooler with by cooling main air distributor.Cooled regenerated catalyst enters riser tube, with stock oil feed contacts.Upwards entered in revivifier through the annular space between sleeve pipe and regenerated catalyst by the cooling main air heated, contact with reclaimable catalyst and carry out coke burning regeneration.Due to above feature, this technology achieves heavy oil riser tube " contact of finish low temperature, high agent-oil ratio " operation, reduces dry gas, coke yield to a certain extent, improves total liquid yield.The weak point that this technology exists is: the first, and the barrel diameter of regenerated catalyst water cooler is less, therefore just needs the cooling main air amount to being passed into by cooling main air distributor to limit.Otherwise cooled regenerated catalyst is carried secretly by the cooling main air heated, upwards flowed in revivifier through the annular space between sleeve pipe and regenerated catalyst in a large amount of regenerated catalyst water cooler, form catalyzer internal recycle, affect device normal running.Because cooling main air amount is restricted, the cooling performance to high-temperature regenerated catalyst thus can be affected.The second, employing be traditional riser catalytic cracking reactor, heavy oil riser tube is difficult to realize shorter finish duration of contact, and reasous and results of wrong subjects is similar to the explanation of CN100338185C.3rd, revivifier, sleeve pipe and regenerated catalyst water cooler are arranged in series up and down, make the total height of device higher.
US Patent No. 6,059, disclosed in 958, a kind of principal character of Catalytic Cracking Technique of Heavy Oil is: will partly or entirely deliver to bottom heavy oil riser tube through the cooled regenerated catalyst of external warmer, mix with the high-temperature regenerated catalyst from revivifier, mixed regeneration catalyzer contacts with heavy oil feed in heavy oil riser tube.Due to above feature, this technology achieves heavy oil riser tube " contact of finish low temperature, high agent-oil ratio " operation.The weak point existed is: first, adopt through the cooled regenerated catalyst of external warmer and the measure from the high-temperature regenerated catalyst hybrid cooling of revivifier, the advantage causing this technology to reduce finish Contact Temperature and rising agent oil ratio only can be embodied in the catalytic cracking unit with superfluous heat.The second, employing be traditional riser catalytic cracking reactor, heavy oil riser tube is difficult to realize shorter finish duration of contact, and reasous and results of wrong subjects is similar to the explanation of CN100338185C.3rd, adopt single heavy oil riser reactor, the independent upgrading to gasoline cannot be realized.
Summary of the invention
The object of this invention is to provide a kind of double lift pipe catalytic cracking method and device thereof, with the measure scope of application solving the reduction regenerated catalyst temperature existing for existing catalytic cracking process narrower (being only applicable to have the catalytic cracking unit of superfluous heat), regulate underaction (adopting main air cooling regenerated catalyst because cooling main air amount is restricted, cooling performance to be affected), enter the catalyst activity lower (impact by lighter hydrocarbons reclaimable catalyst is mixed into) that heavy oil riser tube participates in reaction, heavy oil riser tube is difficult to realize the problems such as shorter finish duration of contact.
For solving the problem, the technical solution used in the present invention is: a kind of double lift pipe catalytic cracking method, heavy oil feed mixes with catalyst exposure and carries out catalytic cracking reaction in heavy oil riser tube, lighter hydrocarbons charging mixes with catalyst exposure and carries out catalytic reforming reaction in lighter hydrocarbons riser tube, heavy oil reactant flow and light hydrogen cracking logistics enter cyclonic separator special separately from heavy oil leg outlet and lighter hydrocarbons leg outlet through closed conduct respectively and carry out gas solid separation, isolated heavy oil reaction oil gas and light hydrogen cracking oil gas enter separation column special separately respectively and carry out fractionation, heavy oil reclaimable catalyst and lighter hydrocarbons reclaimable catalyst carry out turbulent bed regeneration after stripping, regenerated catalyst returns heavy oil riser tube respectively and lighter hydrocarbons riser tube recycles, it is characterized in that: finish duration of contact of heavy oil feed is 0.2 ~ 1.5s, the first turbulent bed revivifier is entered through steam stripped heavy oil reclaimable catalyst and lighter hydrocarbons reclaimable catalyst, with the second turbulent bed regenerator flue gas counter current contact and the generation coke of burning-off more than 90%, semi regeneration catalyzer enters the second turbulent bed revivifier downwards, with the remaining generation coke of main air counter current contact burning-off and heat exchange cool, only directly main air is carried to the second turbulent bed revivifier in regenerative process.
For realizing the Double-lifted pipe catalytic cracking device of aforesaid method, mainly comprise heavy oil riser tube, lighter hydrocarbons riser tube, settling vessel, revivifier, the outlet of heavy oil riser tube is connected with cyclone inlet special separately respectively by closed conduct with the outlet of lighter hydrocarbons riser tube, cyclonic separator is connected by the close phase section of dipleg and settling vessel, the close phase section of settling vessel is stripping stage, it is characterized in that: heavy oil riser tube conversion zone length is 10 ~ 20m, revivifier comprises the first turbulent bed revivifier and the second turbulent bed revivifier, first turbulent bed revivifier is positioned at above the second turbulent bed revivifier, both are coaxial is arranged, separated by flue gas distributor, second turbulent bed revivifier is a cylinder shape cylindrical shell, first turbulent bed revivifier close phase section is identical with the second turbulent bed revivifier internal diameter, be connected with the first turbulent bed revivifier close phase section top by reclaimable catalyst transfer lime bottom stripping stage, be connected with the second turbulent bed revivifier by semi regeneration catalyst transport bottom the close phase section of first turbulent bed revivifier, second turbulent bed regenerator bottoms is connected with bottom heavy oil riser tube with bottom lighter hydrocarbons riser tube with lighter hydrocarbons regenerated catalyst respectively by heavy oil regenerated catalyst.
Described heavy oil riser tube can arrange 2 ~ 5 layers of heavy oil feed nozzle along its axially spaced-apart, and lighter hydrocarbons riser tube can arrange 2 ~ 5 layers of lighter hydrocarbons feed nozzle along its axially spaced-apart.
The single settling vessel Double-lifted pipe catalytic cracking device of one of the present invention, described settling vessel is public settling vessel, coaxial setting is regenerated with the first turbulent bed revivifier and the second turbulent bed, public settling vessel dilute phase section is positioned at above the first turbulent bed revivifier, the close phase section of public settling vessel is mixing reclaimable catalyst stripping stage, mixing reclaimable catalyst stripping stage is positioned at the first turbulent bed revivifier dilute phase section, heavy oil riser tube and lighter hydrocarbons riser tube are composed in series by vertical section and horizontal section all from bottom to top, heavy oil riser tube horizontal section and lighter hydrocarbons riser tube horizontal section are each passed through wall and enter public settling vessel dilute phase section top, reclaimable catalyst transfer lime is mixing regeneration standpipe, semi regeneration catalyst transport is semi-regeneration stand pipe, heavy oil regenerated catalyst is attached most importance to oil regeneration inclined tube, lighter hydrocarbons regenerated catalyst is lighter hydrocarbons regenerator sloped tube.
The two settling vessel Double-lifted pipe catalytic cracking device of one of the present invention, described settling vessel comprises heavy oil reacting-settler and light hydrogen cracking settling vessel, heavy oil reacting-settler regenerates coaxial setting with the first turbulent bed revivifier and the second turbulent bed, its dilute phase section is positioned at above the first turbulent bed revivifier, light hydrogen cracking settling vessel and the first turbulent bed revivifier and the second turbulent bed revivifier height are set up in parallel, the close phase section of heavy oil reacting-settler is heavy oil reclaimable catalyst stripping stage, the close phase section of light hydrogen cracking settling vessel is lighter hydrocarbons reclaimable catalyst stripping stage, heavy oil reclaimable catalyst stripping stage is positioned at the first turbulent bed revivifier dilute phase section, heavy oil riser tube is composed in series by vertical section and horizontal section from bottom to top, heavy oil riser tube horizontal section enters heavy oil reacting-settler dilute phase section top through wall, lighter hydrocarbons riser tube only has vertical section, coaxially arrange with light hydrogen cracking settling vessel, and enter light hydrogen cracking settling vessel dilute phase section top through lighter hydrocarbons reclaimable catalyst stripping stage, reclaimable catalyst transfer lime comprise be communicated with bottom heavy oil reclaimable catalyst stripping stage with the heavy oil regeneration standpipe on the first turbulent bed revivifier close phase section top and the lighter hydrocarbons inclined tube to be generated that is communicated with the first turbulent bed revivifier close phase section top bottom lighter hydrocarbons reclaimable catalyst stripping stage, semi regeneration catalyst transport is semi-regeneration stand pipe, heavy oil regenerated catalyst is attached most importance to oil regeneration inclined tube, lighter hydrocarbons regenerated catalyst is lighter hydrocarbons regenerator sloped tube.
The two settling vessel Double-lifted pipe catalytic cracking device of another kind of the present invention, described settling vessel comprises heavy oil reacting-settler and light hydrogen cracking settling vessel, heavy oil reacting-settler and light hydrogen cracking settling vessel are all set up in parallel with the first turbulent bed revivifier and the second turbulent bed revivifier height, the close phase section of heavy oil reacting-settler is heavy oil reclaimable catalyst stripping stage, the close phase section of light hydrogen cracking settling vessel is lighter hydrocarbons reclaimable catalyst stripping stage, heavy oil riser tube and lighter hydrocarbons riser tube all only have vertical section, coaxially arrange with heavy oil reacting-settler and light hydrogen cracking settling vessel respectively, and be each passed through heavy oil reclaimable catalyst stripping stage and lighter hydrocarbons reclaimable catalyst stripping stage enters heavy oil reacting-settler dilute phase section top and light hydrogen cracking settling vessel dilute phase section top, reclaimable catalyst transfer lime comprise be communicated with bottom heavy oil reclaimable catalyst stripping stage with the heavy oil inclined tube to be generated on the first turbulent bed revivifier close phase section top and the lighter hydrocarbons inclined tube to be generated that is communicated with the first turbulent bed revivifier close phase section top bottom lighter hydrocarbons reclaimable catalyst stripping stage, semi regeneration catalyst transport is semi-regeneration stand pipe, heavy oil regenerated catalyst is attached most importance to oil regeneration inclined tube, lighter hydrocarbons regenerated catalyst is lighter hydrocarbons regenerator sloped tube.
Compared with existing catalytic cracking technology, adopt the present invention, there is following beneficial effect:
(1) single device air feed is adopted (only directly to carry main air to the second turbulent bed revivifier, directly do not carry main air to the first turbulent bed revivifier), flue gas series winding (the second turbulent bed regenerator flue gas enters the first turbulent bed revivifier) be deposited on the two-stage regeneration mode of the generation coke of on reclaimable catalyst more than 90% at the first turbulent bed revivifier burning-off, second turbulent bed revivifier is remaining coke on burning-off semi regeneration catalyzer not only, and becomes a regenerated catalyst water cooler cooled high-temperature regenerated catalyst with main air.Because whole or most main airs all enters the second turbulent bed revivifier, so the intensification heat that can make full use of main air takes cooling down high-temperature regenerated catalyst.Therefore the present invention can realize on the Double-lifted pipe catalytic cracking device of any heavy oil feed of processing maintenance first turbulent bed revivifier burn temperature substantially constant, namely regeneration efficiency is not produced to the temperature effectively reducing regenerated catalyst under the prerequisite of considerable influence, thus realize under the prerequisite keeping the catalyst activity participating in heavy oil feed catalytic cracking reaction, carry out heavy oil riser tube " contact of finish low temperature, high agent-oil ratio " operation, and then suppress heat cracking reaction, promotion catalytic cracking reaction, the dry gas of reduction heavy oil riser tube and the productive rate of coke.Also can realize, under maintenance participates in the prerequisite of the catalyst activity of lighter hydrocarbons charging catalytic reforming reaction, carrying out lighter hydrocarbons riser tube " contact of finish low temperature " operation simultaneously, and then suppress heat cracking reaction, the dry gas of reduction lighter hydrocarbons riser tube and the productive rate of coke.
(2) the cooling degree (i.e. the heat of regenerated catalyst and main air) of regenerated catalyst carries out flexible by control second turbulent bed revivifier height of dense phase (namely changing the heat-exchange time of regenerated catalyst and main air), thus makes the control of the reaction conditions to catalytic cracking and catalytic reforming more flexible.
(3) the first turbulent bed revivifier of the present invention, the second turbulent bed revivifier adopt be close to up and down, the set-up mode of stacked series winding, make the total height of device lower, thus plant investment and energy consumption lower.
(4) the heavy oil riser reactor owing to adopting conversion zone length shorter, can realize shorter heavy oil finish duration of contact, thus the character of heavy oil fluid catalytic cracking product slates and catalytic diesel oil is significantly improved.
The present invention can be used for heavy oil fluid catalytic cracking and lighter hydrocarbons catalytic reforming.
Below in conjunction with accompanying drawing, embodiment and embodiment, the present invention is further detailed explanation.Accompanying drawing, embodiment and embodiment do not limit the scope of protection of present invention.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of a kind of single settling vessel Double-lifted pipe catalytic cracking device of the present invention.
Fig. 2 is the schematic diagram of a kind of pair of settling vessel Double-lifted pipe catalytic cracking device of the present invention.
Fig. 3 is the schematic diagram of the two settling vessel Double-lifted pipe catalytic cracking device of another kind of the present invention.
In Fig. 1, Fig. 2 and Fig. 3, same reference numerals represents identical technical characteristic.Reference numeral represents:
1. public settling vessel, 2. heavy oil reacting-settler, 3. light hydrogen cracking settling vessel, 4. the first turbulent bed revivifier, 5. the second turbulent bed revivifier, 6. external warmer, 7. heavy oil riser tube, 8. lighter hydrocarbons riser tube, 9. mix reclaimable catalyst stripping stage, 10. heavy oil reclaimable catalyst stripping stage, 11. lighter hydrocarbons reclaimable catalyst stripping stages, 12a, 12b, 12c. heavy oil feed nozzle, 13a, 13b, 13c. lighter hydrocarbons feed nozzle, 14. heavy oil react thick cyclonic separator, the thick cyclonic separator of 15. light hydrogen cracking, 16. heavy oil reaction primary cyclones, 17. light hydrogen cracking primary cyclones, 18. heavy oil reaction collection chambers, 19. light hydrogen cracking collection chambers, 20. revivifier primary cyclones, 21. revivifier secondary cyclones, 22. flue gas collection chambers, 23a, 23b, 23c, 23d, 23e. steam distribution pipe, 24. flue gas distributors, 25. distributor pipe of cardinal wind, 26a, 26b. pre-lift medium spray head, 27. old catalyst distrbutors, 28. semi regeneration catalyst dispensers, 29. mixing regeneration standpipes, 30. heavy oil regeneration standpipes, 31. heavy oil inclined tube to be generated, 32. lighter hydrocarbons inclined tube to be generated, 33. semi-regeneration stand pipe, 34. heavy oil regenerator sloped tubes, 35. lighter hydrocarbons regenerator sloped tubes, 36. external warmer catalyst inlet pipes, 37. low temperature catalyst circulation tubes, 38. low temperature catalyst transfer limes, 39. heavy oil guiding valve to be generated, 40. lighter hydrocarbons guiding valve to be generated, 41. semi regeneration plug valves, 42. heavy oil regeneration guiding valves, 43. lighter hydrocarbons regeneration guiding valves, 44. external warmer entrance guiding valves, 45. low temperature catalyst circulation guiding valves, 46. low temperature catalyst conveying guiding valves, 47a, 47b, 47c. heavy oil feed, 48a, 48b, the charging of 48c. lighter hydrocarbons, 49. enter the main air of the second turbulent bed revivifier 5 from distributor pipe of cardinal wind 25, 50. water vapors, 51. pre-lift media, 52. heavy oil reaction oil gas separation column chargings, 53. light hydrogen cracking oil gas separation column chargings, 54. first turbulent bed regenerator flue gas, 55a. heavy oil reacts the outlet conduit of thick cyclonic separator 14 and heavy oil reacts the annular space formed between the inlet duct of primary cyclone 16, the annular space formed between the outlet conduit of the thick cyclonic separator 15 of 55b. light hydrogen cracking and the inlet duct of light hydrogen cracking primary cyclone 17, the annular space formed between 55c. semi-regeneration stand pipe 33 and outer tube.
Embodiment
As shown in Figure 1, the single settling vessel Double-lifted pipe catalytic cracking device of one of the present invention, mainly comprises heavy oil riser tube 7, lighter hydrocarbons riser tube 8, public settling vessel 1, first turbulent bed revivifier 4, second turbulent bed revivifier 5.Public settling vessel 1 dilute phase section is positioned at above the first turbulent bed revivifier 4, and the first turbulent bed revivifier 4 is positioned at above the second turbulent bed revivifier 5, and three devices are coaxially arranged.The close phase section of public settling vessel 1 is mixing reclaimable catalyst stripping stage 9, mixing reclaimable catalyst stripping stage 9 is positioned at the first turbulent bed revivifier 4 dilute phase section, is connected bottom mixed catalyst stripping stage 9 by mixing regeneration standpipe 29 with the first turbulent bed revivifier 4 close phase section top.Be connected with the second turbulent bed revivifier 5 by semi-regeneration stand pipe 33 bottom the close phase section of first turbulent bed revivifier 4.Be connected with bottom heavy oil riser tube 7 with bottom lighter hydrocarbons riser tube 8 with lighter hydrocarbons regenerator sloped tube 35 respectively by heavy oil regenerator sloped tube 34 bottom second turbulent bed revivifier 5.Heavy oil riser tube 7 outlet and lighter hydrocarbons riser tube 8 export and are all positioned at public settling vessel 1 dilute phase section top.
First turbulent bed revivifier 4 is provided with external warmer 6, and external warmer 6 is upper intake lower outlet type.The close phase pars infrasegmentalis of first turbulent bed revivifier 4 is connected with external warmer 6 entrance by external warmer catalyst inlet pipe 36, and external warmer 6 exports and is connected respectively by bottom low temperature catalyst circulation tube 37 and low temperature catalyst transfer lime 38 and the first turbulent bed revivifier 4 close phase section top and heavy oil riser tube 7.
Heavy oil riser tube 7 is identical with lighter hydrocarbons riser tube 8 structure, is composed in series all from bottom to top by vertical section and horizontal section.Heavy oil riser tube 7 is section and lighter hydrocarbons riser tube 8 vertically section vertically, and its top is equipped with air cushion elbow, and bottom is equipped with end socket, and bottom is respectively equipped with steam distribution pipe 23d, 23e, bottom wall is respectively equipped with pre-lift medium spray head 26a, 26b.Heavy oil riser tube 7 is section and lighter hydrocarbons riser tube 8 vertically section vertically, is axially interval with two-layer heavy oil feed nozzle 12a, 12b and two-layer lighter hydrocarbons feed nozzle 13a, 13b respectively along it; Heavy oil riser tube 7 horizontal section and lighter hydrocarbons riser tube 8 horizontal section are respectively equipped with one deck heavy oil feed nozzle 12c and one deck lighter hydrocarbons feed nozzle 13c.Heavy oil riser tube 7 horizontal section and lighter hydrocarbons riser tube 8 horizontal section are each passed through wall and enter public settling vessel 1 dilute phase section top.Usually, heavy oil riser tube 7 can arrange 2 ~ 5 layers of heavy oil feed nozzle along its axially spaced-apart, and lighter hydrocarbons riser tube 8 can arrange 2 ~ 5 layers of lighter hydrocarbons feed nozzle along its axially spaced-apart.
Public settling vessel 1 dilute phase section top, is provided with 1 heavy oil and reacts thick cyclonic separator 14 and 1 thick cyclonic separator 15 of light hydrogen cracking, is also provided with 1 heavy oil reaction primary cyclone 16 and 1 light hydrogen cracking primary cyclone 17.Heavy oil riser tube 7 exports and lighter hydrocarbons riser tube 8 exports and reacts thick cyclonic separator 14 entrance respectively by closed conduct and heavy oil and be connected with light hydrogen cracking thick cyclonic separator 15 entrance.It is less than heavy oil reaction primary cyclone 16 inlet duct internal diameter that heavy oil reacts thick cyclonic separator 14 outlet conduit external diameter, and insert wherein, fix and centering with auxiliary inner member, the passage that the annular space 55a formed between two pipelines enters heavy oil reaction primary cyclone 16 as stripping stream is connected with public settling vessel 1 dilute phase section top simultaneously.Heavy oil is reacted bottom thick cyclonic separator 14 and is connected with mixing reclaimable catalyst stripping stage 9 by dipleg with bottom heavy oil reaction primary cyclone 16.Heavy oil reaction primary cyclone 16 exports and reacts collection chamber 18 by closed conduct and heavy oil and be connected.Light hydrogen cracking thick cyclonic separator 15 outlet conduit external diameter is less than light hydrogen cracking primary cyclone 17 inlet duct internal diameter, and insert wherein, fix and centering with auxiliary inner member, the annular space 55b formed between two pipelines enters light hydrogen cracking primary cyclone 17 passage as stripping stream is connected with public settling vessel 1 dilute phase section top simultaneously.Be connected with mixing reclaimable catalyst stripping stage 9 respectively by dipleg bottom the thick cyclonic separator 15 of light hydrogen cracking with bottom light hydrogen cracking primary cyclone 17.Light hydrogen cracking primary cyclone 17 is exported and is connected with light hydrogen cracking collection chamber 19 by closed conduct.Heavy oil reaction collection chamber 18 and light hydrogen cracking collection chamber 19 are all positioned at public settling vessel 1 top, are connected with light hydrogen cracking gas pipeline respectively by heavy oil reaction oil gas pipeline with heavy oil reaction oil gas separation column with light hydrogen cracking oil gas separation column.Be provided with steam distribution pipe 23a bottom mixing reclaimable catalyst stripping stage 9, mixing regeneration standpipe 29 outlet at bottom is positioned at the first turbulent bed revivifier 4 close phase section top, and is connected with old catalyst distrbutor 27.Usually, public settling vessel 1 dilute phase section top can arrange 1 heavy oil and react thick cyclonic separator 14 and 1 thick cyclonic separator 15 of light hydrogen cracking, can also arrange 1 ~ 4 heavy oil reaction primary cyclone 16 and 1 ~ 4 light hydrogen cracking primary cyclone 17 simultaneously.
Separated by flue gas distributor 24 between first turbulent bed revivifier 4 and the second turbulent bed revivifier 5.First turbulent bed revivifier 4 dilute phase section top is provided with two revivifier primary cyclones 20 and two revivifier secondary cyclones 21.Wherein, revivifier primary cyclone 20 entrance is connected with the first turbulent bed revivifier 4 dilute phase section, revivifier primary cyclone 20 outlet is connected by closed conduct with revivifier secondary cyclone 21 entrance, revivifier secondary cyclone 21 is exported and is connected with flue gas collection chamber 22 entrance being positioned at the first turbulent bed revivifier 4 top by closed conduct, and flue gas collection chamber 22 is exported and is connected with smoke energy recovering system by flue gas pipeline.Usually, the first turbulent bed revivifier 4 dilute phase section top can arrange 1 ~ 6 revivifier primary cyclone 20 and 1 ~ 6 revivifier secondary cyclone 21.
Second turbulent bed revivifier 5 is a cylinder shape cylindrical shell, and be provided with distributor pipe of cardinal wind 25 bottom it, bottom is provided with end socket.Second turbulent bed revivifier 5 internal diameter is identical with the first turbulent bed revivifier 4 close phase section internal diameter.The outlet of semi-regeneration stand pipe 33 is positioned at bottom the second turbulent bed revivifier 5, and by one with its coaxial outer tube arranged be arranged in the middle part of the second turbulent bed revivifier 5 or the semi regeneration catalyst dispenser 28 of bottom is connected, form annular space 55c between semi-regeneration stand pipe 22 and described outer tube.
Semi-regeneration stand pipe 33, heavy oil regenerator sloped tube 34, lighter hydrocarbons regenerator sloped tube 35 and external warmer catalyst inlet pipe 36 entrance all adopt to flood head piece form and arrange and flood stream bucket.Heavy oil regenerator sloped tube 34, lighter hydrocarbons regenerator sloped tube 35, external warmer catalyst inlet pipe 36, low temperature catalyst circulation tube 37 and low temperature catalyst transfer lime 38 are respectively equipped with heavy oil regeneration guiding valve 42, lighter hydrocarbons regeneration guiding valve 43, external warmer entrance guiding valve 44, low temperature catalyst circulation guiding valve 45, low temperature catalyst conveying guiding valve 46.Semi-regeneration stand pipe 33 outlet at bottom is provided with semi regeneration plug valve 41.For avoiding catalyzer to walk short circuit, the distance between external warmer catalyst inlet pipe 36 entrance and low temperature catalyst circulation tube 37 export is not less than 3 meters.
The two settling vessel Double-lifted pipe catalytic cracking device of one of the present invention shown in Fig. 2, with the main difference part of a kind of single settling vessel Double-lifted pipe catalytic cracking device of the present invention shown in Fig. 1 be, in this device, set up special heavy oil reacting-settler 2 and light hydrogen cracking settling vessel 3 respectively.Heavy oil reacting-settler 2 dilute phase section is positioned at above the first turbulent bed revivifier 4, heavy oil reacting-settler 2 and the first turbulent bed revivifier 4 and the second turbulent bed revivifier 5 are coaxially arranged, and light hydrogen cracking settling vessel 3 and the first turbulent bed revivifier 4 and the second turbulent bed revivifier 5 height are set up in parallel.The close phase section of heavy oil reacting-settler 2 is heavy oil reclaimable catalyst stripping stage 10, and heavy oil reclaimable catalyst stripping stage 10 is positioned at the first turbulent bed revivifier 4 dilute phase section; The close phase section of light hydrogen cracking settling vessel 3 is lighter hydrocarbons reclaimable catalyst stripping stage 11.Heavy oil riser tube 7 horizontal section enters heavy oil reacting-settler 2 dilute phase section top through wall.Lighter hydrocarbons riser tube 8 only has vertical section, coaxially arranges with light hydrogen cracking settling vessel 3, and enters light hydrogen cracking settling vessel 3 dilute phase section top through lighter hydrocarbons reclaimable catalyst stripping stage 11; Three layers of lighter hydrocarbons feed nozzle 13a, 13b, 13c is all arranged in the vertical section of lighter hydrocarbons riser tube 8.Heavy oil reaction collection chamber 18 and light hydrogen cracking collection chamber 19 lay respectively at the top of heavy oil reacting-settler 2 and light hydrogen cracking settling vessel 3.Be provided with 1 heavy oil in heavy oil reacting-settler 2 and react thick cyclonic separator 14 and 1 heavy oil reaction primary cyclone 16, in light hydrogen cracking settling vessel 3, be provided with 1 thick cyclonic separator 15 of light hydrogen cracking and 1 light hydrogen cracking primary cyclone 17.Be provided with steam distribution pipe 23b bottom heavy oil reclaimable catalyst stripping stage 10, and be connected with the first turbulent bed revivifier 4 close phase section top with old catalyst distrbutor 27 by heavy oil regeneration standpipe 30; Be provided with steam distribution pipe 23c bottom lighter hydrocarbons reclaimable catalyst stripping stage 11, and be connected with the first turbulent bed revivifier 4 close phase section top with old catalyst distrbutor 27 by lighter hydrocarbons inclined tube to be generated 32.Lighter hydrocarbons inclined tube to be generated 32 is provided with lighter hydrocarbons guiding valve 40 to be generated.Usually, heavy oil reacting-settler 2 dilute phase section top can arrange 1 heavy oil and react thick cyclonic separator 14 and 1 ~ 4 heavy oil reaction primary cyclone 16, and light hydrogen cracking settling vessel 3 dilute phase section top can arrange 1 thick cyclonic separator 15 of light hydrogen cracking and 1 ~ 4 light hydrogen cracking primary cyclone 17.
The two settling vessel Double-lifted pipe catalytic cracking device of another kind of the present invention shown in Fig. 3, with the main difference part of a kind of pair of settling vessel Double-lifted pipe catalytic cracking device of the present invention shown in Fig. 2 be, in this device, heavy oil reacting-settler 2 and the first turbulent bed revivifier 4 and the second turbulent bed revivifier 5 height are set up in parallel.Heavy oil riser tube 7 only has vertical section, coaxially arranges with heavy oil reacting-settler 2, and enters heavy oil reacting-settler 2 dilute phase section top through heavy oil reclaimable catalyst stripping stage 10; Three layers of heavy oil feed nozzle 12a, 12b, 12c is all arranged in the vertical section of heavy oil riser tube 7.Heavy oil reclaimable catalyst stripping stage 10 is connected with the first turbulent bed revivifier 4 close phase section top with old catalyst distrbutor 27 by heavy oil inclined tube to be generated 31.Heavy oil inclined tube to be generated 31 is provided with heavy oil guiding valve 39 to be generated.
In the present invention, each equipment body is metal material (being generally carbon steel or stainless steel).Wherein, mixing regeneration standpipe 29, heavy oil regeneration standpipe 30, heavy oil inclined tube 31 to be generated, lighter hydrocarbons inclined tube 32 to be generated, semi-regeneration stand pipe 33, heavy oil regenerator sloped tube 34, lighter hydrocarbons regenerator sloped tube 35, external warmer catalyst inlet pipe 36, low temperature catalyst circulation tube 37, low temperature catalyst transfer lime 38, heavy oil riser tube 7, lighter hydrocarbons riser tube 8, public settling vessel 1, heavy oil reacting-settler 2, light hydrogen cracking settling vessel 3, first turbulent bed revivifier 4, second turbulent bed revivifier 5, external warmer 6, heavy oil reacts thick cyclonic separator 14, the thick cyclonic separator 15 of light hydrogen cracking, heavy oil reaction primary cyclone 16, light hydrogen cracking primary cyclone 17, revivifier primary cyclone 20, insulating and wearing-resistant lining is lined with in revivifier secondary cyclone 21 inside is equal.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 internal diameter of equipment of the present invention or pipeline, for the equipment or the pipeline that are provided with insulating and wearing-resistant lining, all refers to the internal diameter of corresponding insulating and wearing-resistant lining.
In the present invention, heavy oil riser tube 7 total length is generally 40 ~ 60m, and wherein, conversion zone length is generally 10 ~ 20m, and pre lift zone length is generally 20 ~ 50m, and conversion zone internal diameter is generally 400 ~ 2500mm, and pre lift zone internal diameter is generally 200 ~ 1300mm.For the heavy oil riser tube 7 be composed in series by vertical section and horizontal section shown in Fig. 1 and Fig. 2, vertical segment length is generally 30 ~ 55m, and the length of horizontal section is generally 5 ~ 10m.For the heavy oil riser tube 7 only comprising vertical section shown in Fig. 3, vertical segment length is generally 40 ~ 60m.
In the present invention, lighter hydrocarbons riser tube 8 total length is generally 40 ~ 60m, and wherein, conversion zone length is generally 10 ~ 30m, and pre lift zone length is generally 10 ~ 50m, and conversion zone internal diameter is generally 300 ~ 2000mm, and pre lift zone internal diameter is generally 150 ~ 1000mm.For the lighter hydrocarbons riser tube 8 be composed in series by vertical section and horizontal section shown in Fig. 1, vertical segment length is generally 30 ~ 55m, and the length of horizontal section is generally 5 ~ 10m.For the lighter hydrocarbons riser tube 8 only comprising vertical section shown in Fig. 2 and Fig. 3, vertical segment length is generally 40 ~ 60m.
In the present invention, heavy oil riser tube 7 and lighter hydrocarbons riser tube 8 meet the general feature of the riser tube that Conventional riser catalytic cracking unit adopts.The concrete length of its each several part can respectively according to the design finish duration of contact of two riser tubes, the design linear speed of each several part, the parameters such as the scantlings of the structure of each settling vessel and each revivifier and the pressure equilibrium of whole catalytic cracking unit, adopt the design and calculation method of Conventional riser catalytic cracking unit riser tube to be determined.The concrete internal diameter of two riser tube each several parts can, respectively according to parameters such as the design linear speeds of the designing treatment amount of each riser tube, water vapor and pre-lift medium consumption and two riser tube each several parts, adopt the design and calculation method of Conventional riser catalytic cracking unit riser tube to be determined.
In the present invention, heavy oil feed nozzle and lighter hydrocarbons feed nozzle belong to existing conventional equipment, meet the general feature of Conventional catalytic cracking feed nozzle.Its concrete structure size and space layout can adopt the design and calculation method of Conventional catalytic cracking feed nozzle to be determined according to the scantlings of the structure of two riser tubes, the operational condition such as designing treatment amount and atomizing steam amount respectively.The concrete setting position of each layer heavy oil feed nozzle and lighter hydrocarbons feed nozzle the parameter such as design linear speed of finish duration of contact respectively required for each stock heavy oil feed and lighter hydrocarbons charging and each riser tube conversion zone can carry out calculating and determines.The concrete material of heavy oil feed nozzle and lighter hydrocarbons feed nozzle can be determined according to the character of each stock heavy oil feed and lighter hydrocarbons charging and operational condition respectively.
In the present invention, mixing regeneration standpipe 29 internal diameter is generally 350 ~ 2200mm, heavy oil regeneration standpipe 30 internal diameter is generally 300 ~ 1800mm, heavy oil inclined tube 31 to be generated internal diameter is generally 300 ~ 1800mm, lighter hydrocarbons inclined tube 32 to be generated internal diameter is generally 200 ~ 1200mm, semi-regeneration stand pipe 33 internal diameter is generally 350 ~ 2200mm, heavy oil regenerator sloped tube 34 internal diameter is generally 300 ~ 1800mm, lighter hydrocarbons regenerator sloped tube 35 internal diameter is generally 200 ~ 1200mm, external warmer catalyst inlet pipe 36 internal diameter is generally 150 ~ 900mm, low temperature catalyst circulation tube 37 internal diameter is generally 150 ~ 900mm, low temperature catalyst transfer lime 38 internal diameter is generally 150 ~ 900mm.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.
In the present invention, the first turbulent bed revivifier 4 close phase section internal diameter n is generally 2400 ~ 16000mm, and its dilute phase section internal diameter w is generally 3000 ~ 20000mm, and the second turbulent bed revivifier 5 internal diameter is generally 2400 ~ 16000mm.First turbulent bed revivifier 4 and the second turbulent bed revivifier 5 meet the general feature of the turbulent bed revivifier that Conventional riser catalytic cracking unit adopts.Can according to the design linear speed at the design carbon-burning capacity of the first turbulent bed revivifier 4 and coke burning degree, the first each position of turbulent bed revivifier 4, and the Parameter Conditions such as the scantlings of the structure of revivifier primary cyclone 20 and revivifier secondary cyclone 21 and mounting means, adopt the design and calculation method of existing catalytic cracking unit turbulent bed revivifier to determine the concrete structure size at the first each position of turbulent bed revivifier 4.The internal diameter of the second turbulent bed revivifier 5 is identical with the internal diameter n of the first turbulent bed revivifier 4 close phase section.Can according to the temperature range of the first turbulent bed revivifier 4 and the second turbulent bed revivifier 5, the concentration limit of the second turbulent bed regenerator flue gas entrained catalyst particles, the design linear speed of the second turbulent bed revivifier 5 and internal diameter, and the Parameter Conditions such as the scantlings of the structure of distributor pipe of cardinal wind 25 and supporting structure, the total height of the second turbulent bed revivifier 5 is determined in conjunction with gas-solid direct heat transfer rule and transport disengaging height method of calculation.
In the present invention, public settling vessel 1, heavy oil reacting-settler 2 and light hydrogen cracking settling vessel 3 belong to existing conventional equipment, meet the general feature of conventional lift tubular type catalytic cracking unit settling vessel.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.
In the present invention, external warmer 6 belongs to existing conventional equipment.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.
In the present invention, heavy oil reacts thick cyclonic separator 14, the thick cyclonic separator of light hydrogen cracking 15, heavy oil reaction primary cyclone 16, light hydrogen cracking primary cyclone 17 and revivifier primary cyclone 20 and revivifier secondary cyclone 21 and belongs to existing conventional equipment.Its concrete structure size and space layout can adopt the design and calculation method of existing cyclonic separator to be determined according to the operational condition of device.
In the present invention, steam distribution pipe 23a, 23b, 23c, 23d, 23e and distributor pipe of cardinal wind 25 can adopt dendriform distribution pipe or annular spread pipe, all belong to existing conventional equipment.Its concrete structure size and space layout can adopt the design and calculation method of existing steam distribution pipe and distributor pipe of cardinal wind to be determined according to the operational condition of device.
In the present invention, pre-lift medium spray head 26a, 26b belong to existing conventional equipment.The design and calculation method that its concrete structure size, setting position and space layout can adopt pre existing to promote medium spray head according to the operational condition of device is determined.
In the present invention, flue gas distributor 24 can adopt dish, plate shaped or arch grid distributor, all belongs to existing conventional equipment.Its concrete structure size and space layout can adopt the design and calculation method of existing main air distributing plate to be determined according to the operational condition of device.
In the present invention, what semi-regeneration stand pipe 33, heavy oil regenerator sloped tube 34, lighter hydrocarbons regenerator sloped tube 35 and external warmer catalyst inlet pipe 36 ingress were arranged flood stream bucket all belongs to existing conventional equipment.Its concrete structure size can adopt the existing design and calculation method flooding stream bucket to be determined according to the operational condition of device.
In the present invention, old catalyst distrbutor 27 and semi regeneration catalyst dispenser 28 all belong to existing conventional equipment.Its concrete structure size and space layout can adopt the design and calculation method of existing catalyst dispenser to be determined according to the operational condition of device.
The Double-lifted pipe catalytic cracking device shown in Fig. 1 is adopted to carry out the method for double lift pipe catalytic cracking of the present invention as follows: three kinds of heavy oil feed 47a, 47b, 47c mix with catalyst exposure and carry out the catalytic cracking reaction that finish is 0.2 ~ 1.5 second duration of contact in heavy oil riser tube 7, and lighter hydrocarbons charging 48a, 48b, 48c contact with regenerated catalyst and mix and carry out catalytic reforming reaction in lighter hydrocarbons riser tube 8.Heavy oil reactant flow and light hydrogen cracking logistics enter public settling vessel 1 respectively and carry out gas solid separation, isolated heavy oil reaction oil gas and light hydrogen cracking oil gas enter heavy oil reaction oil gas separation column respectively and light hydrogen cracking oil gas separation column carries out fractionation, and isolated heavy oil reclaimable catalyst and lighter hydrocarbons reclaimable catalyst enter mixing reclaimable catalyst stripping stage 9 and carry out stripping.The generation coke of the first turbulent bed revivifier 4 and the second turbulent bed regenerator flue gas counter current contact burning-off more than 90% is entered through steam stripped mixing reclaimable catalyst (comprising heavy oil reclaimable catalyst and lighter hydrocarbons reclaimable catalyst).Semi regeneration catalyzer enters the second turbulent bed revivifier 5, with the remaining generation coke of main air 49 counter current contact burning-off and heat exchange cool, regenerated catalyst returns heavy oil riser tube 7 respectively and lighter hydrocarbons riser tube 8 recycles.
In above operating process, heavy oil riser tube 7 processes three kinds of heavy oil feed 47a, 47b, 47c simultaneously, and lighter hydrocarbons riser tube 8 processes three kinds of lighter hydrocarbons chargings 48a, 48b, 48c simultaneously.According to reaction needed, three kinds of heavy oil feed 47a, 47b, 47c enter heavy oil riser tube 7, three kinds of lighter hydrocarbons chargings 48a, 48b, 48c from three layers of heavy oil feed nozzle 12a, 12b, 12c respectively and enter lighter hydrocarbons riser tube 8 from three layers of lighter hydrocarbons feed nozzle 13a, 13b, 13c respectively.
In above operating process, the regenerated catalyst in the second turbulent bed revivifier 5 is divided into two portions.Wherein a part enters bottom heavy oil riser tube 7 through heavy oil regenerator sloped tube 34 downwards bottom the second turbulent bed revivifier 5, first undertaken loosening and fluidisation by the water vapor 50 passed into through steam distribution pipe 23d, then contact with heavy oil feed 47a, 47b, 47c after promoting a up segment distance by the pre-lift medium 51 passed into through pre-lift medium spray head 26a.Another part regenerated catalyst enters bottom lighter hydrocarbons riser tube 8 through lighter hydrocarbons regenerator sloped tube 35 downwards bottom the second turbulent bed revivifier 5, first undertaken loosening and fluidisation by the water vapor 50 passed into through steam distribution pipe 23e, then contact with lighter hydrocarbons charging 48a, 48b, 48c after promoting a up segment distance by the pre-lift medium 51 passed into through pre-lift medium spray head 26b.
In above operating process, heavy oil reactant flow enters through closed conduct the heavy oil being positioned at public settling vessel 1 from heavy oil riser tube 7 horizontal section and reacts thick cyclonic separator 14 and carry out gas solid separation, and isolated gaseous stream enters heavy oil reaction primary cyclone 16 and carries out further gas solid separation; Light hydrogen cracking logistics enters the thick cyclonic separator 15 of the light hydrogen cracking being positioned at public settling vessel 1 from lighter hydrocarbons riser tube 8 horizontal section through closed conduct and carries out gas solid separation, and isolated gaseous stream enters light hydrogen cracking primary cyclone 17 and carries out further gas solid separation.The stripping stream (the hydro carbons oil gas gone out by stripping and a small amount of catalyzer carried secretly thereof) produced in stripping process is divided into two portions, a part enters heavy oil reaction primary cyclone 16 through annular space 55a and carries out gas solid separation, and another part enters light hydrogen cracking primary cyclone 17 through annular space 55b and carries out gas solid separation.Heavy oil reacts thick cyclonic separator 14 isolated heavy oil reclaimable catalyst, the isolated lighter hydrocarbons reclaimable catalyst of the thick cyclonic separator of light hydrogen cracking 15 and heavy oil reaction primary cyclone 16 and light hydrogen cracking primary cyclone 17 isolated mixing reclaimable catalyst enters mixing reclaimable catalyst stripping stage through each cyclone dip-leg, carries out stripping by the water vapor 50 passed into through steam distribution pipe 23a.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 52 through heavy oil reaction collection chamber 18 and heavy oil reaction oil gas pipeline by the hydro carbons oil gas that stripping goes out and carry out fractionation, and 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 53 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.
In above operating process, enter the first turbulent bed revivifier 4 close phase section top through mixing regeneration standpipe 29 and old catalyst distrbutor 27 downwards through steam stripped mixing reclaimable catalyst, contact with the second turbulent bed regenerator flue gas entering the first turbulent bed revivifier 4 from flue gas distributor 24.First turbulent bed regenerator flue gas 54 and a small amount of granules of catalyst carried secretly thereof carry out gas solid separation through revivifier primary cyclone 20 and revivifier secondary cyclone 21 successively, isolated granules of catalyst returns the close phase section of the first turbulent bed revivifier 4 through the dipleg of each cyclonic separator of revivifier, and isolated first turbulent bed regenerator flue gas 54 enters smoke energy recovering system through flue gas collection chamber 22 and flue gas pipeline.
In above operating process, semi regeneration catalyzer downwards through semi-regeneration stand pipe 33, upwards enter the second turbulent bed revivifier 5 through annular space 55c and semi regeneration catalyst dispenser 28 again, contacts with the main air 49 entering the second turbulent bed revivifier 5 from distributor pipe of cardinal wind 25 bottom the close phase section of the first turbulent bed revivifier 4.
In above operating process, the heat balance of full device carries out auxiliary adjustment by external warmer 6, namely as required a part of semi regeneration catalyzer is introduced heat collector 6 from the close phase pars infrasegmentalis of the first turbulent bed revivifier 4 through external warmer catalyst inlet pipe 36 and cools.Can all return to the first turbulent bed revivifier 4 close phase section top through low temperature catalyst circulation tube 37 through external warmer 6 cooled low temperature semi regeneration catalyzer, or all enter bottom heavy oil riser tube 7 through low temperature catalyst transfer lime 38.This cooled low temperature semi regeneration catalyzer or be divided into two portions, a part returns to the first turbulent bed revivifier 4 close phase section top through low temperature catalyst circulation tube 37, and another part enters bottom heavy oil riser tube 7 through low temperature catalyst transfer lime 38.The operational condition of external warmer 6, can adjust flexibly according to the change of heat-obtaining load.
Partly or entirely will return to the first turbulent bed revivifier 5 close phase section top through external warmer 6 cooled low temperature semi regeneration catalyzer through low temperature catalyst circulation tube 37, need pass into a small amount of for carrying the main air of catalyzer in low temperature catalyst circulation tube 37, this strand of main air will enter the close phase section of the first turbulent bed revivifier 4 and participate in burning.Do not belong to above-mentioned situation, main air all enters the second turbulent bed revivifier 5, first turbulent bed revivifier 4 from distributor pipe of cardinal wind 25 and burns using the second turbulent bed regenerator flue gas completely.Main air amount is determined according to amount of burnt, meets the demand all generating coke with holomorphosis mode burning-off.
The catalyzer participating in reaction of the present invention, refer to the regenerated catalyst entered bottom heavy oil riser tube 7 and bottom lighter hydrocarbons riser tube 8, or the mixed catalyst that the regenerated catalyst entered bottom heavy oil riser tube 7 and cooled low temperature semi regeneration catalyzer form.After the generation coke of reclaimable catalyst (comprising heavy oil reclaimable catalyst and lighter hydrocarbons reclaimable catalyst) burning-off more than 90% in the first turbulent bed revivifier 5, the activity of the semi regeneration catalyzer of generation is equivalent to more than 95% of regenerated catalyst activity.
In above operating process, the flow entering the regenerated catalyst of heavy oil riser tube 7 and lighter hydrocarbons riser tube 8 from the second turbulent bed revivifier 5 is regulated by heavy oil regeneration guiding valve 42 and lighter hydrocarbons regeneration guiding valve 43 respectively, the second turbulent bed revivifier 5 and external warmer 6 is entered from the first turbulent bed revivifier 4, the first turbulent bed revivifier 4 is returned from external warmer 6, the flow of the semi regeneration catalyzer of heavy oil riser tube 7 is entered respectively by semi regeneration plug valve 41 from external warmer 6, external warmer entrance guiding valve 44, low temperature catalyst circulation guiding valve 45, low temperature catalyst conveying guiding valve 46 regulates.
The method adopting Double-lifted pipe catalytic cracking device shown in Fig. 2 to carry out double lift pipe catalytic cracking of the present invention is with the main difference part adopting Fig. 1 shown device to carry out double lift pipe catalytic cracking method: lighter hydrocarbons charging carries out catalytic reforming reaction in the lighter hydrocarbons riser tube 8 only having vertical section.Heavy oil reactant flow carries out gas solid separation in heavy oil reacting-settler 2, and light hydrogen cracking logistics carries out gas solid separation in light hydrogen cracking settling vessel 3.Heavy oil reclaimable catalyst carries out stripping at heavy oil reclaimable catalyst stripping stage 10, and lighter hydrocarbons reclaimable catalyst carries out stripping at lighter hydrocarbons reclaimable catalyst stripping stage 11.The stripping stream that heavy oil reclaimable catalyst produces in stripping process enters heavy oil reaction primary cyclone 16 through annular space 55a and carries out gas solid separation, and the stripping stream that lighter hydrocarbons reclaimable catalyst produces in stripping process enters light hydrogen cracking primary cyclone 17 through annular space 55b and carries out gas solid separation.The first turbulent bed revivifier 4 close phase section top is entered through heavy oil regeneration standpipe 30 and old catalyst distrbutor 27 downwards through steam stripped heavy oil reclaimable catalyst; Enter the first turbulent bed revivifier 4 close phase section top through lighter hydrocarbons inclined tube to be generated 32 and old catalyst distrbutor 27 downwards through steam stripped lighter hydrocarbons reclaimable catalyst, the flow of this strand of catalyzer is regulated by lighter hydrocarbons guiding valve 40 to be generated.
The method adopting Double-lifted pipe catalytic cracking device shown in Fig. 3 to carry out double lift pipe catalytic cracking of the present invention is with the main difference part adopting Fig. 2 shown device to carry out double lift pipe catalytic cracking method: heavy oil feed carries out catalytic cracking reaction in the heavy oil riser tube 7 only having vertical section.Enter the first turbulent bed revivifier 4 close phase section top through heavy oil inclined tube to be generated 31 and old catalyst distrbutor 27 downwards through steam stripped heavy oil reclaimable catalyst, the flow of this strand of catalyzer is regulated by heavy oil guiding valve 39 to be generated.
In the present invention, heavy oil riser tube 7 can process 1 ~ 5 kind of heavy oil feed simultaneously.Heavy oil feed 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.Different types of heavy oil feed, according to reaction needed, enters heavy oil riser tube 7 from each layer heavy oil feed nozzle being axially disposed within different positions along heavy oil riser tube 7, reacts with catalyst exposure.Lighter hydrocarbons riser tube 8 can process 1 ~ 5 kind of lighter hydrocarbons charging simultaneously.Lighter hydrocarbons charging comprises catalytically cracked gasoline, light FCC gasoline, coker gasoline, straight-run spirit, pneumatic press condensed oil.Different types of lighter hydrocarbons charging, according to reaction needed, enters lighter hydrocarbons riser tube 8 from each layer lighter hydrocarbons feed nozzle being axially disposed within different positions along lighter hydrocarbons riser tube 8, reacts with catalyst exposure.The catalyzer that the present invention is used can be existing various catalytic cracking catalyst (such as CC-20D).
In the present invention, pre-lift medium 51 is steam or dry gas, can select on demand.
In the present invention, the prevailing operating conditions of heavy oil riser tube 7 is: temperature of reaction (heavy oil riser tube 7 temperature out) is generally 460 ~ 560 DEG C, preferably 470 ~ 550 DEG C, is preferably 480 ~ 540 DEG C; Finish is generally 0.2 ~ 1.5s duration of contact, preferably 0.4 ~ 1.2s, is preferably 0.5 ~ 1.0s; Total agent-oil ratio is generally 5 ~ 20, and preferably 6 ~ 15, be preferably 7 ~ 12; The average linear speed of oil gas is generally 8.0 ~ 15.0m/s; The catalyst activity participating in reaction is generally 58 ~ 75, and preferably 62 ~ 72, be preferably 65 ~ 70.
In the present invention, the prevailing operating conditions of lighter hydrocarbons riser tube 8 is: temperature of reaction (lighter hydrocarbons riser tube 8 temperature out) is generally 450 ~ 600 DEG C, preferably 480 ~ 580 DEG C, is preferably 500 ~ 550 DEG C; Finish is generally 0.2 ~ 2.5s duration of contact, preferably 0.5 ~ 2.0s, is preferably 0.8 ~ 1.5s; Total agent-oil ratio is generally 4 ~ 20, and preferably 6 ~ 15, be preferably 7 ~ 12; The average linear speed of oil gas is generally 8.0 ~ 15.0m/s; The catalyst activity participating in reaction is generally 58 ~ 75, and preferably 62 ~ 72, be preferably 65 ~ 70.
In the present invention, the prevailing operating conditions of public settling vessel 1 is: dilute phase temperature is generally 470 ~ 560 DEG C, and top absolute pressure is generally 0.20 ~ 0.38MPa.
In the present invention, the prevailing operating conditions of heavy oil reacting-settler 2 is: dilute phase temperature is generally 470 ~ 550 DEG C, and top absolute pressure is generally 0.20 ~ 0.38MPa.
In the present invention, the prevailing operating conditions of light hydrogen cracking settling vessel 3 is: dilute phase temperature is generally 440 ~ 590 DEG C, and top absolute pressure is generally 0.20 ~ 0.38MPa.
In the present invention, the prevailing operating conditions of mixing reclaimable catalyst stripping stage 9 is: stripping temperature is generally 480 ~ 570 DEG C, and stripping time is for being generally 1.0 ~ 3.0min, and stripped vapor consumption is generally 2 ~ 5kg/t cat(kg water steam/ton catalyzer).
In the present invention, the prevailing operating conditions of heavy oil reclaimable catalyst stripping stage 10 is: stripping temperature is generally 480 ~ 560 DEG C, and stripping time is for being generally 1.0 ~ 3.0min, and stripped vapor consumption is generally 2 ~ 5kg/t cat.
In the present invention, the prevailing operating conditions of lighter hydrocarbons reclaimable catalyst stripping stage 11 is: stripping temperature is generally 450 ~ 600 DEG C, and stripping time is for being generally 1.0 ~ 3.0min, and stripped vapor consumption is generally 2 ~ 5kg/t cat.
In the present invention, the prevailing operating conditions of the first turbulent bed revivifier 4 is: dense phase temperature is generally 630 ~ 730 DEG C, dense phase gases linear speed is generally 0.7 ~ 1.0m/s, height of dense phase is generally 8 ~ 15m, and (for the device adopting plate shaped flue gas distributor, the first turbulent bed revivifier 4 height of dense phase refers to the distance of the first turbulent bed revivifier 4 level of dense bed and flue gas distributor 24, for the device adopting dish or arch flue gas distributor, first turbulent bed revivifier 4 height of dense phase refers to the distance of the first turbulent bed revivifier 4 level of dense bed and flue gas distributor 24 curved surface lower end), dilute phase linear gas velocity is generally 0.4 ~ 0.6m/s, dilute phase settling height is generally 7 ~ 10m (the first turbulent bed revivifier 4 dilute phase settling height refers to the distance of revivifier primary cyclone 20 entrance and the first turbulent bed revivifier 4 level of dense bed), coke burning degree is generally 70 ~ 180kg/ (th), char length is generally 5.0 ~ 10.0min, top absolute pressure is generally 0.22 ~ 0.40MPa.
In the present invention, the prevailing operating conditions of the second turbulent bed revivifier 5 is: dense phase temperature is generally 600 ~ 700 DEG C, dense phase gases linear speed is generally 0.7 ~ 1.0m/s, height of dense phase is generally 3 ~ 5m (the second turbulent bed revivifier 5 height of dense phase refers to the distance of the second turbulent bed revivifier 5 level of dense bed and distributor pipe of cardinal wind 25 lower surface), dilute phase linear gas velocity is generally 0.7 ~ 1.0m/s, dilute phase height is generally 5 ~ 8m (for the device adopting plate shaped flue gas distributor, second turbulent bed revivifier 5 dilute phase height refers to the distance of the second turbulent bed revivifier 5 level of dense bed and flue gas distributor 24, for the device adopting dish or arch flue gas distributor, second turbulent bed revivifier 5 dilute phase height refers to the distance of the second turbulent bed revivifier 5 level of dense bed and flue gas distributor 24 curved surface lower end), coke burning degree is generally 40 ~ 100kg/ (th), and char length is generally 1.0 ~ 3.0min.
The percentage ratio that the present invention mentions, except represent regenerated catalyst activity and represent except percent by volume with v%, be weight percentage.
Comparative example and embodiment
Comparative example
Single settling vessel double lift pipe catalytic cracking pilot plant of routine is tested.This pilot plant arranges a turbulent bed revivifier, does not arrange external warmer.The designing treatment amount of heavy oil riser tube is 60kg/d (kg/day), and the designing treatment amount of lighter hydrocarbons riser tube is 24kg/d.Heavy oil riser tube and lighter hydrocarbons riser tube arrange one deck heavy oil feed nozzle and one deck lighter hydrocarbons feed nozzle respectively.
In comparative example, the heavy oil feedstock of heavy oil riser tube processing is Daqing atmospheric residue, and the light hydrocarbon feedstocks of lighter hydrocarbons riser tube processing is attached most importance to the catalytic gasoline that oil riser produces, and catalyzer adopts commercially available CC-20D catalytic cracking industry equilibrium catalyst.In comparative example, described charging refers to Daqing atmospheric residue and recycle stock, for lighter hydrocarbons riser tube, refers to the catalytic gasoline that heavy oil riser tube produces for heavy oil riser tube.Heavy oil riser tube simulates the operation of full freshening, enters heavy oil riser tube after heavy oil feedstock mixes with recycle stock through same layer heavy oil feed nozzle; The single-pass operation of lighter hydrocarbons riser tube.The carbon content of regenerated catalyst is 0.03%, and micro-activity is 62.The stripping fluid of mixing reclaimable catalyst stripping stage is water vapor, and stripping temperature is 500 DEG C.
Heavy oil feedstock character is in table 1, and the prevailing operating conditions of comparative example and product slates are in table 2, and liquid product main character is in table 3.
Embodiment
Embodiment 1 ~ 5 is tested being similar on the single settling vessel double lift pipe catalytic cracking pilot plant shown in Fig. 1 of the present invention.With Fig. 1 shown device unlike, in this pilot plant, heavy oil riser tube arranges two-layer heavy oil feed nozzle, and lighter hydrocarbons riser tube arranges two-layer lighter hydrocarbons feed nozzle; External warmer is not set, does not have external warmer catalyst inlet pipe, external warmer entrance guiding valve, low temperature catalyst circulation tube, low temperature catalyst circulation guiding valve, low temperature catalyst transfer lime, low temperature catalyst to carry guiding valve.The designing treatment amount of heavy oil riser tube is 60kg/d, and the designing treatment amount of lighter hydrocarbons riser tube is 30kg/d.The internal diameter of heavy oil riser tube conversion zone and lighter hydrocarbons riser tube conversion zone can need to change according to technique.
In embodiment 1 ~ 5, the heavy oil feedstock of heavy oil riser tube processing is the Daqing atmospheric residue identical with comparative example, the light hydrocarbon feedstocks of lighter hydrocarbons riser tube processing is attached most importance to the catalytic gasoline that oil riser produces, and catalyzer adopts the industrial equilibrium catalyst of the commercially available CC-20D catalytic cracking identical with comparative example.In embodiment, described charging refers to Daqing atmospheric residue and recycle stock, for lighter hydrocarbons riser tube, refers to the catalytic gasoline that heavy oil riser tube produces for heavy oil riser tube, and described raw material refers to Daqing atmospheric residue, for lighter hydrocarbons riser tube, refers to the catalytic gasoline that heavy oil riser tube produces for heavy oil riser tube.Heavy oil riser tube simulates the operation of full freshening, and heavy oil feedstock and recycle stock are each respectively enters heavy oil riser tube from one deck heavy oil feed nozzle; The single-pass operation of lighter hydrocarbons riser tube, light hydrocarbon feedstocks enters lighter hydrocarbons riser tube from one deck lighter hydrocarbons feed nozzle.The carbon content of regenerated catalyst is 0.03%, and micro-activity is 62.The stripping fluid of mixing reclaimable catalyst stripping stage is water vapor, and stripping temperature is 500 DEG C.
The prevailing operating conditions of embodiment 1 and product slates are in table 4, and liquid product main character is in table 5.The prevailing operating conditions of embodiment 2 and product slates are in table 6, and liquid product main character is in table 7.The prevailing operating conditions of embodiment 3 and product slates are in table 8, and liquid product main character is in table 9.The prevailing operating conditions of embodiment 4 and product slates are in table 10, and liquid product main character is in table 11.The prevailing operating conditions of embodiment 5 and product slates are in table 12, and liquid product main character is in table 13.
Table 1 heavy oil feedstock character (comparative example, embodiment 1 ~ 5)
Heavy oil feedstock Daqing atmospheric residue
Density (20 DEG C), kgm -3 900.2
Carbon residue, % 4.2
Group composition, %
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
The prevailing operating conditions of table 2 comparative example and product slates
The liquid product main character of table 3 comparative example
The prevailing operating conditions of table 4 embodiment 1 and product slates
The liquid product main character of table 5 embodiment 1
The prevailing operating conditions of table 6 embodiment 2 and product slates
The liquid product main character of table 7 embodiment 2
The prevailing operating conditions of table 8 embodiment 3 and product slates
The liquid product main character of table 9 embodiment 3
The prevailing operating conditions of table 10 embodiment 4 and product slates
The liquid product main character of table 11 embodiment 4
The prevailing operating conditions of table 12 embodiment 5 and product slates
The liquid product main character of table 13 embodiment 5

Claims (11)

1. a double lift pipe catalytic cracking method, heavy oil feed mixes with catalyst exposure and carries out catalytic cracking reaction in heavy oil riser tube, lighter hydrocarbons charging mixes with catalyst exposure and carries out catalytic reforming reaction in lighter hydrocarbons riser tube, heavy oil reactant flow and light hydrogen cracking logistics enter cyclonic separator special separately from heavy oil leg outlet and lighter hydrocarbons leg outlet through closed conduct respectively and carry out gas solid separation, isolated heavy oil reaction oil gas and light hydrogen cracking oil gas enter separation column special separately respectively and carry out fractionation, heavy oil reclaimable catalyst and lighter hydrocarbons reclaimable catalyst carry out turbulent bed regeneration after stripping, regenerated catalyst returns heavy oil riser tube respectively and lighter hydrocarbons riser tube recycles, it is characterized in that: finish duration of contact of heavy oil feed is 0.2 ~ 1.5s, the first turbulent bed revivifier is entered through steam stripped heavy oil reclaimable catalyst and lighter hydrocarbons reclaimable catalyst, with the second turbulent bed regenerator flue gas counter current contact and the generation coke of burning-off more than 90%, semi regeneration catalyzer enters the second turbulent bed revivifier downwards, with the remaining generation coke of main air counter current contact burning-off and heat exchange cool, only directly main air is carried to the second turbulent bed revivifier in regenerative process.
2. according to double lift pipe catalytic cracking method according to claim 1, it is characterized in that: described heavy oil riser tube processes 1 ~ 5 kind of heavy oil feed simultaneously, lighter hydrocarbons riser tube processes 1 ~ 5 kind of lighter hydrocarbons charging simultaneously.
3. according to double lift pipe catalytic cracking method according to claim 1, it is characterized in that: a part of semi regeneration catalyzer is introduced external warmer from the close phase pars infrasegmentalis of the first turbulent bed revivifier and cools, cooled semi regeneration catalyzer all returns to the first turbulent bed revivifier close phase section top or all enters bottom heavy oil riser tube, or be divided into two portions, a part returns to the first turbulent bed revivifier close phase section top, and another part enters bottom heavy oil riser tube.
4. according to double lift pipe catalytic cracking method according to claim 1, it is characterized in that: the operational condition of described heavy oil riser tube is, temperature of reaction is 460 ~ 560 DEG C, total agent-oil ratio is 5 ~ 20, the average linear speed of oil gas is 8.0 ~ 15.0m/s, the catalyst activity participating in reaction is 58 ~ 75, the operational condition of lighter hydrocarbons riser tube is, temperature of reaction is 450 ~ 600 DEG C, finish duration of contact is 0.2 ~ 2.5s, total agent-oil ratio is 4 ~ 20, the average linear speed of oil gas is 8.0 ~ 15.0m/s, the catalyst activity participating in reaction is 58 ~ 75, the operational condition of the first turbulent bed revivifier is, dense phase temperature is 630 ~ 730 DEG C, dense phase gases linear speed is 0.7 ~ 1.0m/s, height of dense phase is 8 ~ 15m, dilute phase linear gas velocity is 0.4 ~ 0.6m/s, dilute phase settling height is 7 ~ 10m, coke burning degree is 70 ~ 180kg/ (th), char length is 5.0 ~ 10.0min, top absolute pressure 0.22 ~ 0.40MPa, the operational condition of the second turbulent bed revivifier is, dense phase temperature is 600 ~ 700 DEG C, dense phase gases linear speed is 0.7 ~ 1.0m/s, height of dense phase is 3 ~ 5m, dilute phase linear gas velocity is 0.7 ~ 1.0m/s, dilute phase height is 5 ~ 8m, coke burning degree is 40 ~ 100kg/ (th), char length is 1.0 ~ 3.0min.
5. one kind for realizing the Double-lifted pipe catalytic cracking device of method described in claim 1, mainly comprise heavy oil riser tube, lighter hydrocarbons riser tube, settling vessel, revivifier, the outlet of heavy oil riser tube is connected with cyclone inlet special separately respectively by closed conduct with the outlet of lighter hydrocarbons riser tube, cyclonic separator is connected by the close phase section of dipleg and settling vessel, the close phase section of settling vessel is stripping stage, it is characterized in that: heavy oil riser tube conversion zone length is 10 ~ 20m, revivifier comprises the first turbulent bed revivifier and the second turbulent bed revivifier, first turbulent bed revivifier is positioned at above the second turbulent bed revivifier, both are coaxial is arranged, separated by flue gas distributor, second turbulent bed revivifier is a cylinder shape cylindrical shell, first turbulent bed revivifier close phase section is identical with the second turbulent bed revivifier internal diameter, be connected with the first turbulent bed revivifier close phase section top by reclaimable catalyst transfer lime bottom stripping stage, be connected with the second turbulent bed revivifier by semi regeneration catalyst transport bottom the close phase section of first turbulent bed revivifier, second turbulent bed regenerator bottoms is connected with bottom heavy oil riser tube with bottom lighter hydrocarbons riser tube with lighter hydrocarbons regenerated catalyst respectively by heavy oil regenerated catalyst.
6. according to Double-lifted pipe catalytic cracking device according to claim 5, it is characterized in that: described heavy oil riser tube is provided with 2 ~ 5 layers of heavy oil feed nozzle along its axially spaced-apart, lighter hydrocarbons riser tube is provided with 2 ~ 5 layers of lighter hydrocarbons feed nozzle along its axially spaced-apart.
7. according to Double-lifted pipe catalytic cracking device according to claim 5, it is characterized in that: described settling vessel is public settling vessel, coaxial setting is regenerated with the first turbulent bed revivifier and the second turbulent bed, public settling vessel dilute phase section is positioned at above the first turbulent bed revivifier, the close phase section of public settling vessel is mixing reclaimable catalyst stripping stage, mixing reclaimable catalyst stripping stage is positioned at the first turbulent bed revivifier dilute phase section, heavy oil riser tube and lighter hydrocarbons riser tube are composed in series by vertical section and horizontal section all from bottom to top, heavy oil riser tube horizontal section and lighter hydrocarbons riser tube horizontal section are each passed through wall and enter public settling vessel dilute phase section top, reclaimable catalyst transfer lime is mixing regeneration standpipe, semi regeneration catalyst transport is semi-regeneration stand pipe, heavy oil regenerated catalyst is attached most importance to oil regeneration inclined tube, lighter hydrocarbons regenerated catalyst is lighter hydrocarbons regenerator sloped tube.
8. according to Double-lifted pipe catalytic cracking device according to claim 5, it is characterized in that: described settling vessel comprises heavy oil reacting-settler and light hydrogen cracking settling vessel, heavy oil reacting-settler regenerates coaxial setting with the first turbulent bed revivifier and the second turbulent bed, its dilute phase section is positioned at above the first turbulent bed revivifier, light hydrogen cracking settling vessel and the first turbulent bed revivifier and the second turbulent bed revivifier height are set up in parallel, the close phase section of heavy oil reacting-settler is heavy oil reclaimable catalyst stripping stage, the close phase section of light hydrogen cracking settling vessel is lighter hydrocarbons reclaimable catalyst stripping stage, heavy oil reclaimable catalyst stripping stage is positioned at the first turbulent bed revivifier dilute phase section, heavy oil riser tube is composed in series by vertical section and horizontal section from bottom to top, heavy oil riser tube horizontal section enters heavy oil reacting-settler dilute phase section top through wall, lighter hydrocarbons riser tube only has vertical section, coaxially arrange with light hydrogen cracking settling vessel, and enter light hydrogen cracking settling vessel dilute phase section top through lighter hydrocarbons reclaimable catalyst stripping stage, reclaimable catalyst transfer lime comprise be communicated with bottom heavy oil reclaimable catalyst stripping stage with the heavy oil regeneration standpipe on the first turbulent bed revivifier close phase section top and the lighter hydrocarbons inclined tube to be generated that is communicated with the first turbulent bed revivifier close phase section top bottom lighter hydrocarbons reclaimable catalyst stripping stage, semi regeneration catalyst transport is semi-regeneration stand pipe, heavy oil regenerated catalyst is attached most importance to oil regeneration inclined tube, lighter hydrocarbons regenerated catalyst is lighter hydrocarbons regenerator sloped tube.
9. according to Double-lifted pipe catalytic cracking device according to claim 5, it is characterized in that: described settling vessel comprises heavy oil reacting-settler and light hydrogen cracking settling vessel, heavy oil reacting-settler and light hydrogen cracking settling vessel are all set up in parallel with the first turbulent bed revivifier and the second turbulent bed revivifier height, the close phase section of heavy oil reacting-settler is heavy oil reclaimable catalyst stripping stage, the close phase section of light hydrogen cracking settling vessel is lighter hydrocarbons reclaimable catalyst stripping stage, heavy oil riser tube and lighter hydrocarbons riser tube all only have vertical section, coaxially arrange with heavy oil reacting-settler and light hydrogen cracking settling vessel respectively, and be each passed through heavy oil reclaimable catalyst stripping stage and lighter hydrocarbons reclaimable catalyst stripping stage enters heavy oil reacting-settler dilute phase section top and light hydrogen cracking settling vessel dilute phase section top, reclaimable catalyst transfer lime comprise be communicated with bottom heavy oil reclaimable catalyst stripping stage with the heavy oil inclined tube to be generated on the first turbulent bed revivifier close phase section top and the lighter hydrocarbons inclined tube to be generated that is communicated with the first turbulent bed revivifier close phase section top bottom lighter hydrocarbons reclaimable catalyst stripping stage, semi regeneration catalyst transport is semi-regeneration stand pipe, heavy oil regenerated catalyst is attached most importance to oil regeneration inclined tube, lighter hydrocarbons regenerated catalyst is lighter hydrocarbons regenerator sloped tube.
10. according to Double-lifted pipe catalytic cracking device according to claim 5, it is characterized in that: the first described turbulent bed revivifier is provided with external warmer, the close phase pars infrasegmentalis of first turbulent bed revivifier is connected with external warmer entrance by external warmer catalyst inlet pipe, and external warmer outlet is connected respectively by bottom low temperature catalyst circulation tube and low temperature catalyst transfer lime and the first turbulent bed revivifier close phase section top and heavy oil riser tube.
11. according to Double-lifted pipe catalytic cracking device according to claim 5, it is characterized in that: described heavy oil riser tube total length is 40 ~ 60m, wherein, pre lift zone length is 20 ~ 50m, conversion zone internal diameter is 400 ~ 2500mm, pre lift zone internal diameter is 200 ~ 1300mm, and lighter hydrocarbons riser tube total length is 40 ~ 60m, wherein, conversion zone length is 10 ~ 30m, pre lift zone length is 10 ~ 50m, and conversion zone internal diameter is 300 ~ 2000mm, and pre lift zone internal diameter is 150 ~ 1000mm.First turbulent bed revivifier close phase section internal diameter n is 2400 ~ 16000mm, and its dilute phase section internal diameter w is 3000 ~ 20000mm, and the second turbulent bed revivifier internal diameter is 2400 ~ 16000mm.
CN201310346814.6A 2013-08-03 2013-08-03 A kind of double lift pipe catalytic cracking method and device thereof Active CN104342197B (en)

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CN111944558A (en) * 2020-08-23 2020-11-17 浙江工业大学 Reaction regeneration circulating device system in catalytic cracking
CN114854441A (en) * 2022-04-14 2022-08-05 陕煤集团榆林化学有限责任公司 Pulverized coal conveying system using carbon dioxide as conveying gas

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CN102925210A (en) * 2011-08-12 2013-02-13 中国石油天然气股份有限公司 Catalytic cracking method having low oiling agent contact temperature difference, and device thereof
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