CN104342197B - A kind of double lift pipe catalytic cracking method and device thereof - Google Patents

A kind of double lift pipe catalytic cracking method and device thereof Download PDF

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Publication number
CN104342197B
CN104342197B CN201310346814.6A CN201310346814A CN104342197B CN 104342197 B CN104342197 B CN 104342197B CN 201310346814 A CN201310346814 A CN 201310346814A CN 104342197 B CN104342197 B CN 104342197B
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heavy oil
turbulent bed
bed regenerator
riser
lighter hydrocarbons
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CN104342197A (en
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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

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The invention discloses a kind of double lift pipe catalytic cracking method of petroleum chemical industry and device thereof. Method includes: adopt two risers to carry out RFCC and lighter hydrocarbons catalytic reforming respectively; Oil preparation time of contact of RFCC is 0.2��1.5s; Two bursts of reaction logistics are carried out gas solid separation by each special cyclone separator; Two strands of reaction oil gas are carried out fractional distillation by each special fractionating column; The reclaimable catalyst of two riser generations enters the first turbulent bed regenerator and the generation coke of the second turbulent bed regenerator flue gas counter current contacting burning-off more than 90% after stripping, semi regeneration catalyst enters the second turbulent bed regenerator and the remaining generation coke of main air counter current contacting burning-off heat exchange cooling, regeneration catalyzing agent after cooling returns two risers and recycles, and only directly carries main air to the second turbulent bed regenerator in regenerative process. The invention discloses the Double-lifted pipe catalytic cracking device for realizing said 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 of petroleum chemical industry and device thereof.
Background technology
At present, the shortcoming of Conventional catalytic cracking following several respects of device ubiquity that petroleum chemical industry uses: first, being limited by regeneration kinetics, regeneration temperature is higher, causes the regenerated catalyst temperature higher (being typically in about 700 DEG C) participating in reaction; Limited by device thermal balance, the oil ratio making heavy oil riser is relatively small, general total oil ratio is 5��8 (the weight circulating load that total oil ratio is riser inner catalyst of riser and the ratios of the weight flow summation of each stock charging of riser), so that the number of active center that the heavy oil feed of Unit Weight touches is less, this inhibits catalytic cracking reaction to a great extent. Meanwhile, in riser, the Contact Temperature of oil preparation is higher, has promoted heat cracking reaction to a certain extent. Second, the time of oil preparation contact longer (is typically in about 4s, s is the second), this also exacerbates the secondary response of cracking product while improving feedstock conversion, the productivity making cracked gas (including dry gas and liquefied gas) and coke is higher, vapour, diesel oil distillate yield relatively low; Also make the inferior quality of catalytic diesel oil, be not suitable as vehicle fuel blending component. 3rd, catalytic gasoline cannot be carried out independent upgrading, and quality is relatively low. For many years, substantial amounts of research work has done in overcoming the shortcoming existing for above-mentioned Conventional catalytic cracking device in domestic and international research institution.
The disclosed a kind of catalyst cracking method of Chinese patent CN100338185C and device, it is mainly technically characterized ny: adopt Double-lifted pipe catalytic cracking device, utilize the technical advantage of Double-lifted pipe catalytic cracking device, by higher for part or all of residual activity (being approximately equivalent to the 90% of regeneration catalyzing agent activity), temperature relatively low (about 500 DEG C) and the catalyst mix device bottom steam stripped lighter hydrocarbons riser reclaimable catalyst feeding heavy oil riser, heavy oil riser is entered together with after mixing from the regeneration catalyzing agent of regenerator in catalyst mix device, contact with heavy oil feed.Due to the heat exchange action of two strands of catalyst in blender, the temperature making mixed catalyst is relatively low, it is achieved that heavy oil riser " contact of oil preparation low temperature, high agent-oil ratio " operation, reduces dry gas, coke yield to a certain extent, improves total liquid yield. This technology also exists some deficiency following: first, and lighter hydrocarbons reclaimable catalyst mixes with regeneration catalyzing agent, reduces the activity of the catalyst participating in reaction in heavy oil riser to a certain extent, product slates and product property are brought adverse effect. Second, what this technology adopted is traditional riser catalytic cracking reactor, and it is relatively low that nozzle arranges position, and the oil preparation of heavy oil riser actually only can be controlled to 2��4s time of contact, and the response time being shorter than 2s is difficulty with. Owing to oil preparation is longer for time of contact, cause that the character of the product slates of heavy oil riser and catalytic diesel oil is relatively poor.
A kind of apparatus and method reducing temperature of catalytic cracking regenerated catalyst disclosed in Chinese patent CN101575534B, it is mainly technically characterized ny: be arranged below a regeneration catalyzing agent cooler at regenerator, regeneration catalyzing agent in regenerator enters wherein through regenerated catalyst, passes into the cooling main air mixed heat transfer in regeneration catalyzing agent cooler with by cooling main air distributor. Regeneration catalyzing agent after cooling enters riser, with raw oil feed contacts. Heated cooling main air annular space between sleeve pipe and regenerated catalyst is upwardly in regenerator, contacts with reclaimable catalyst and carries out coke burning regeneration. Due to features above, this technology achieves heavy oil riser " contact of oil preparation 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: first, and the barrel diameter of regeneration catalyzing agent cooler is less, and the cooling main air amount to being passed into by cooling main air distributor that is therefore accomplished by limits. Otherwise, heated cooling main air is carried secretly by the regeneration catalyzing agent after cooling in a large amount of regeneration catalyzing agent coolers, annular space between sleeve pipe and regenerated catalyst flows upwardly in regenerator, forms catalyst internal recycle, affects device normal operating. Owing to cooling main air amount is restricted, thus the cooling effect to high-temperature regenerated catalyst can be affected. Second, employing is traditional riser catalytic cracking reactor, and it is similar to the explanation of CN100338185C that heavy oil riser is difficulty with shorter oil preparation time of contact, reason and consequence. 3rd, regenerator, sleeve pipe and regeneration catalyzing agent cooler are arranged in series up and down, and the total height making device is higher.
US Patent No. 6,059, partly or entirely regeneration catalyzing agent after external warmer cools down is delivered to bottom heavy oil riser by being mainly characterized by comprising: of a kind of Catalytic Cracking Technique of Heavy Oil disclosed in 958, mixing with the high-temperature regenerated catalyst from regenerator, mixed regeneration catalyst contacts with heavy oil feed in heavy oil riser. Due to features above, this technology achieves heavy oil riser " contact of oil preparation low temperature, high agent-oil ratio " operation. The weak point existed is: first, adopt the measure of the regeneration catalyzing agent after external warmer cools down and the high-temperature regenerated catalyst hybrid cooling from regenerator, cause that this technology reduces oil preparation Contact Temperature and is only capable of being embodied in the catalytic cracking unit with superfluous heat with the advantage improving oil ratio.Second, employing is traditional riser catalytic cracking reactor, and it is similar to the explanation of CN100338185C that heavy oil riser is difficulty with shorter oil preparation time of contact, reason and consequence. 3rd, adopt single heavy oil riser reactor, it is impossible to realize the independent upgrading to gasoline.
Summary of the invention
It is an object of the invention to provide a kind of double lift pipe catalytic cracking method and device thereof, the measure scope of application to solve the reduction regenerated catalyst temperature existing for existing catalytic cracking process is narrower (being only applicable to the catalytic cracking unit with superfluous heat), regulate underaction (adopting main air cooling regeneration catalyzing agent to make cooling effect be affected because cooling main air amount is restricted), enter heavy oil riser and participate in the catalyst activity relatively low (by the impact that lighter hydrocarbons reclaimable catalyst is mixed into) of reaction, heavy oil riser is difficult to the problems such as shorter oil preparation time of contact.
For solving the problems referred to above, the technical solution used in the present invention is: a kind of double lift pipe catalytic cracking method, heavy oil feed contacts mixing in heavy oil riser and carries out catalytic cracking reaction with catalyst, lighter hydrocarbons charging contacts mixing in lighter hydrocarbons riser and carries out catalytic reforming reaction with catalyst, heavy oil reaction logistics and light hydrogen cracking logistics enter each special cyclone separator 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 respectively enter each special fractionating column and carry out fractional distillation, heavy oil reclaimable catalyst and lighter hydrocarbons reclaimable catalyst carry out turbulent bed regeneration after stripping, regeneration catalyzing agent returns heavy oil riser respectively and lighter hydrocarbons riser recycles, it is characterized in that: oil preparation time of contact of heavy oil feed is 0.2��1.5s, the first turbulent bed regenerator is entered through steam stripped heavy oil reclaimable catalyst and lighter hydrocarbons reclaimable catalyst, generation coke with the second turbulent bed regenerator flue gas counter current contacting burning-off more than 90%, semi regeneration catalyst is downwardly into the second turbulent bed regenerator, cool down with the remaining generation coke of main air counter current contacting burning-off heat exchange, regenerative process only directly carries main air to the second turbulent bed regenerator.
For realizing the Double-lifted pipe catalytic cracking device of said method, mainly include heavy oil riser, lighter hydrocarbons riser, settler, regenerator, the outlet of heavy oil riser is connected with each special cyclone inlet respectively through closed conduct with the outlet of lighter hydrocarbons riser, cyclone separator is connected by the close phase section of dipleg and settler, the close phase section of settler is stripping section, it is characterized in that: heavy oil riser conversion zone length is 10��20m, regenerator includes the first turbulent bed regenerator and the second turbulent bed regenerator, first turbulent bed regenerator is positioned at above the second turbulent bed regenerator, both are coaxially disposed, separated by flue gas distributor, second turbulent bed regenerator is a column type cylinder, first turbulent bed regenerator close phase section is identical with the second turbulent bed regenerator internal diameter, it is connected with the first turbulent bed regenerator close phase section top by reclaimable catalyst conveying pipe bottom stripping section, it is connected by semi regeneration catalyst transport and the second turbulent bed regenerator bottom the first close phase section of turbulent bed regenerator, second turbulent bed regenerator bottoms is connected with bottom heavy oil riser and bottom lighter hydrocarbons riser with lighter hydrocarbons regenerated catalyst respectively through heavy oil regenerated catalyst.
Described heavy oil riser can arrange 2��5 layers of heavy oil feed nozzle along its axially spaced-apart, and lighter hydrocarbons riser can arrange 2��5 layers of lighter hydrocarbons feed nozzle along its axially spaced-apart.
A kind of single settler Double-lifted pipe catalytic cracking device of the present invention, described settler is public settler, regenerate with the first turbulent bed regenerator and the second turbulent bed and be coaxially disposed, public settler dilute phase section is positioned at above the first turbulent bed regenerator, the close phase section of public settler is mixing reclaimable catalyst stripping section, mixing reclaimable catalyst stripping section is positioned at the first turbulent bed regenerator dilute phase section, heavy oil riser and lighter hydrocarbons riser are composed in series by vertical section and horizontal segment all from bottom to top, heavy oil riser horizontal segment and lighter hydrocarbons riser horizontal segment are each passed through wall and enter public settler dilute phase section top, reclaimable catalyst conveying pipe 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.
A kind of double, two settler Double-lifted pipe catalytic cracking devices of the present invention, described settler includes heavy oil reacting-settler and light hydrogen cracking settler, heavy oil reacting-settler and the first turbulent bed regenerator and the regeneration of the second turbulent bed are coaxially disposed, its dilute phase section is positioned at above the first turbulent bed regenerator, light hydrogen cracking settler and the first turbulent bed regenerator and the second turbulent bed regenerator height are set up in parallel, the close phase section of heavy oil reacting-settler is heavy oil reclaimable catalyst stripping section, the close phase section of light hydrogen cracking settler is lighter hydrocarbons reclaimable catalyst stripping sections, heavy oil reclaimable catalyst stripping section is positioned at the first turbulent bed regenerator dilute phase section, heavy oil riser is composed in series by vertical section and horizontal segment from bottom to top, heavy oil riser horizontal segment enters heavy oil reacting-settler dilute phase section top through wall, lighter hydrocarbons riser only has vertical section, it is coaxially disposed with light hydrogen cracking settler, and enter light hydrogen cracking settler dilute phase section top through lighter hydrocarbons reclaimable catalyst stripping section, reclaimable catalyst conveying pipe include bottom connection heavy oil reclaimable catalyst stripping section with the heavy oil regeneration standpipe on the first turbulent bed regenerator close phase section top and connect bottom lighter hydrocarbons reclaimable catalyst stripping section the lighter hydrocarbons inclined tube to be generated with the first turbulent bed regenerator close phase section top, 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.
Another kind of double, two settler Double-lifted pipe catalytic cracking devices of the present invention, described settler includes heavy oil reacting-settler and light hydrogen cracking settler, heavy oil reacting-settler and light hydrogen cracking settler are all set up in parallel with the first turbulent bed regenerator and the second turbulent bed regenerator height, the close phase section of heavy oil reacting-settler is heavy oil reclaimable catalyst stripping section, the close phase section of light hydrogen cracking settler is lighter hydrocarbons reclaimable catalyst stripping sections, heavy oil riser and lighter hydrocarbons riser all only have vertical section, it is coaxially disposed with heavy oil reacting-settler and light hydrogen cracking settler respectively, and it is each passed through heavy oil reclaimable catalyst stripping section and lighter hydrocarbons reclaimable catalyst stripping section enters heavy oil reacting-settler dilute phase section top and light hydrogen cracking settler dilute phase section top, reclaimable catalyst conveying pipe include bottom connection heavy oil reclaimable catalyst stripping section with the heavy oil inclined tube to be generated on the first turbulent bed regenerator close phase section top and connect bottom lighter hydrocarbons reclaimable catalyst stripping section the lighter hydrocarbons inclined tube to be generated with the first turbulent bed regenerator close phase section top, 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 regenerator, directly do not carry main air to the first turbulent bed regenerator), flue gas series winding (the second turbulent bed regenerator flue gas enters the first turbulent bed regenerator) and the first turbulent bed regenerator burning-off be deposited on reclaimable catalyst more than 90% generate coke two-stage regeneration mode, second turbulent bed regenerator is applied not only to remaining coke on burning-off semi regeneration catalyst, and becomes regeneration catalyzing agent cooler high-temperature regenerated catalyst cooled down with main air.Owing to whole or most main airs has been enter into the second turbulent bed regenerator, it is possible to the intensification heat making full use of main air carrys out cooling down high-temperature regeneration catalyzing agent. Therefore the present invention can realize burning the temperature that temperature is basically unchanged, effectively reduces regeneration catalyzing agent under the premise that namely regeneration efficiency do not produced considerable influence maintaining the first turbulent bed regenerator on the Double-lifted pipe catalytic cracking device processing any heavy oil feed, thus realizing under keeping the premise participating in the catalyst activity of heavy oil feed catalytic cracking reaction, carry out heavy oil riser " contact of oil preparation low temperature, high agent-oil ratio " operation, and then suppress heat cracking reaction, promote catalytic cracking reaction, reduce the dry gas of heavy oil riser and the productivity of coke. It also is able to realize under keeping the premise participating in the catalyst activity of lighter hydrocarbons charging catalytic reforming reaction simultaneously, carries out lighter hydrocarbons riser " contact of oil preparation low temperature " operation, and then suppress heat cracking reaction, reduce the dry gas of lighter hydrocarbons riser and the productivity of coke.
(2) the cooling degree (i.e. the heat exchange amount of regeneration catalyzing agent and main air) of regeneration catalyzing agent carries out flexible by controlling the second turbulent bed regenerator height of dense phase (namely changing the heat-exchange time of regeneration catalyzing agent and main air), so that the control of catalytic cracking and the reaction condition of catalytic reforming is more flexible.
(3) set-up mode of the first turbulent bed regenerator of the present invention, the second employing of turbulent bed regenerator next-door neighbour, stacked series winding up and down, the total height making device is relatively low, thus plant investment and energy consumption are relatively low.
(4) owing to adopting the shorter heavy oil riser reactor of conversion zone length, it is possible to achieve shorter heavy oil oil preparation time of contact, so that the character of RFCC product slates and catalytic diesel oil significantly improves.
The present invention can be used for RFCC and lighter hydrocarbons catalytic reforming.
Below in conjunction with accompanying drawing, detailed description of the invention and embodiment, the present invention is further detailed explanation. Accompanying drawing, detailed description of the invention and embodiment are not limiting as the scope of protection of present invention.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of a kind of single settler Double-lifted pipe catalytic cracking device of the present invention.
Fig. 2 is the schematic diagram of a kind of pair of settler Double-lifted pipe catalytic cracking device of the present invention.
Fig. 3 is the schematic diagram of another kind of double; two settler Double-lifted pipe catalytic cracking devices of the present invention.
In Fig. 1, Fig. 2 and Fig. 3, same reference numerals represents identical technical characteristic. Accompanying drawing labelling represents:
1. public settler, 2. heavy oil reacting-settler, 3. light hydrogen cracking settler, 4. the first turbulent bed regenerator, 5. the second turbulent bed regenerator, 6. external warmer, 7. heavy oil riser, 8. lighter hydrocarbons riser, 9. mixing reclaimable catalyst stripping section, 10. heavy oil reclaimable catalyst stripping section, 11. lighter hydrocarbons reclaimable catalyst stripping section, 12a, 12b, 12c. heavy oil feed nozzle, 13a, 13b, 13c. lighter hydrocarbons feed nozzle, 14. heavy oil reacts thick cyclone separator, 15. the thick cyclone separator of light hydrogen cracking, 16. heavy oil reaction primary cyclone, 17. light hydrogen cracking primary cyclone, 18. heavy oil reaction collection chamber, 19. light hydrogen cracking collection chamber, 20. regenerator primary cyclone, 21. regenerator secondary cyclone, 22. flue gas collection chamber, 23a, 23b, 23c, 23d, 23e. distribution of steam pipe, 24. flue gas distributor, 25. distributor pipe of cardinal wind, 26a, 26b. pre-lift medium spray head, 27. old catalyst distrbutor, 28. semi regeneration catalyst dispenser, 29. mixing regeneration standpipe, 30. heavy oil regeneration standpipe, 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 tube, 35. lighter hydrocarbons regenerator sloped tube, 36. external warmer catalyst inlet pipe, 37. low temperature catalyst circulation pipe, 38. low temperature catalyst conveying pipe, 39. heavy oil guiding valve to be generated, 40. lighter hydrocarbons guiding valve to be generated, 41. semi regeneration plug valve, 42. heavy oil regeneration guiding valve, 43. lighter hydrocarbons regeneration guiding valve, 44. external warmer entrance guiding valve, 45. low temperature catalyst circulation guiding valve, 46. low temperature catalyst conveying guiding valve, 47a, 47b, 47c. heavy oil feed, 48a, 48b, 48c. lighter hydrocarbons charging, 49. enter the main air of the second turbulent bed regenerator 5 from distributor pipe of cardinal wind 25, 50. water vapour, 51. pre-lift medium, 52. heavy oil reaction oil gas fractionating column charging, 53. light hydrogen cracking oil gas fractionating column charging, 54. the first turbulent bed regenerator flue gas, 55a. the outlet conduit that heavy oil reacts thick cyclone separator 14 reacts the annular space formed between the inlet duct of primary cyclone 16 with heavy oil, 55b. the annular space formed between outlet conduit and the inlet duct of light hydrogen cracking primary cyclone 17 of the thick cyclone separator 15 of light hydrogen cracking, 55c. the annular space formed between semi-regeneration stand pipe 33 and trocar sheath.
Detailed description of the invention
As it is shown in figure 1, a kind of single settler Double-lifted pipe catalytic cracking device of the present invention, mainly include heavy oil riser 7, lighter hydrocarbons riser 8, public settler the 1, first turbulent bed regenerator the 4, second turbulent bed regenerator 5. Public settler 1 dilute phase section is positioned at above the first turbulent bed regenerator 4, and the first turbulent bed regenerator 4 is positioned at above the second turbulent bed regenerator 5, and three devices are coaxially disposed. The close phase section of public settler 1 is mixing reclaimable catalyst stripping section 9, mixing reclaimable catalyst stripping section 9 is positioned at the first turbulent bed regenerator 4 dilute phase section, is connected with the first turbulent bed regenerator 4 close phase section top by mixing regeneration standpipe 29 bottom mixed catalyst stripping section 9. It is connected with the second turbulent bed regenerator 5 by semi-regeneration stand pipe 33 bottom the first close phase section of turbulent bed regenerator 4. It is connected with bottom heavy oil riser 7 and bottom lighter hydrocarbons riser 8 with lighter hydrocarbons regenerator sloped tube 35 respectively through heavy oil regenerator sloped tube 34 bottom second turbulent bed regenerator 5. Heavy oil riser 7 outlet and lighter hydrocarbons riser 8 outlet are respectively positioned on public settler 1 dilute phase section top.
First turbulent bed regenerator 4 is provided with external warmer 6, and external warmer 6 is upper intake lower outlet type. The first close phase pars infrasegmentalis of turbulent bed regenerator 4 is connected with external warmer 6 entrance by external warmer catalyst inlet pipe 36, and external warmer 6 exports carries pipe 38 to be connected with bottom the first turbulent bed regenerator 4 close phase section top and heavy oil riser 7 respectively through low temperature catalyst circulation pipe 37 with low temperature catalyst.
Heavy oil riser 7 is identical with lighter hydrocarbons riser 8 structure, is composed in series by vertical section and horizontal segment all from bottom to top. The vertical section of heavy oil riser 7 and the vertical section of lighter hydrocarbons riser 8, its top is equipped with air cushion elbow, and bottom is equipped with end socket, and bottom is respectively equipped with distribution of steam pipe 23d, 23e, and bottom wall is respectively equipped with pre-lift medium spray head 26a, 26b. The vertical section of heavy oil riser 7 and the vertical section of lighter hydrocarbons riser 8, be axially respectively separated along it and be provided with two-layer heavy oil feed nozzle 12a, 12b and two-layer lighter hydrocarbons feed nozzle 13a, 13b; Heavy oil riser 7 horizontal segment and lighter hydrocarbons riser 8 horizontal segment are respectively equipped with one layer of heavy oil feed nozzle 12c and one layer of lighter hydrocarbons feed nozzle 13c. Heavy oil riser 7 horizontal segment and lighter hydrocarbons riser 8 horizontal segment are each passed through wall and enter public settler 1 dilute phase section top. Generally, heavy oil riser 7 can arrange 2��5 layers of heavy oil feed nozzle along its axially spaced-apart, and lighter hydrocarbons riser 8 can arrange 2��5 layers of lighter hydrocarbons feed nozzle along its axially spaced-apart.
Public settler 1 dilute phase section top, is provided with 1 heavy oil and reacts thick cyclone separator 14 and 1 thick cyclone separator 15 of light hydrogen cracking, is additionally provided with 1 heavy oil reaction primary cyclone 16 and 1 light hydrogen cracking primary cyclone 17. Heavy oil riser 7 outlet exports with lighter hydrocarbons riser 8 reacts thick cyclone separator 14 entrance respectively through closed conduct with heavy oil and light hydrogen cracking thick cyclone separator 15 entrance is connected. It is less than heavy oil reaction primary cyclone 16 inlet duct internal diameter that heavy oil reacts thick cyclone separator 14 outlet conduit external diameter, and be inserted, simultaneously to assist inner member to fix and centering, 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 settler 1 dilute phase section top. Heavy oil is reacted to react with heavy oil bottom primary cyclone 16 bottom thick cyclone separator 14 and is connected with mixing reclaimable catalyst stripping section 9 by dipleg.Heavy oil reaction primary cyclone 16 exports and reacts collection chamber 18 by closed conduct with heavy oil and be connected. Light hydrogen cracking thick cyclone separator 15 outlet conduit external diameter is less than light hydrogen cracking primary cyclone 17 inlet duct internal diameter, and be inserted, simultaneously to assist inner member to fix and centering, the passage that the annular space 55b formed between two pipelines enters light hydrogen cracking primary cyclone 17 as stripping stream is connected with public settler 1 dilute phase section top. It is connected with mixing reclaimable catalyst stripping section 9 respectively through dipleg with bottom light hydrogen cracking primary cyclone 17 bottom the thick cyclone separator 15 of light hydrogen cracking. 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 respectively positioned on public settler 1 top, are connected with heavy oil reaction oil gas fractionating column and light hydrogen cracking oil gas fractionating column with light hydrogen cracking oil-gas pipeline respectively through heavy oil reaction oil gas pipeline. Being provided with distribution of steam pipe 23a bottom mixing reclaimable catalyst stripping section 9, mixing regeneration standpipe 29 outlet at bottom is positioned at the first turbulent bed regenerator 4 close phase section top, and is connected with old catalyst distrbutor 27. Generally, public settler 1 dilute phase section top can arrange 1 heavy oil and react thick cyclone separator 14 and 1 thick cyclone 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 regenerator 4 and the second turbulent bed regenerator 5. First turbulent bed regenerator 4 dilute phase section top is provided with two regenerator primary cyclones 20 and two regenerator secondary cyclones 21. Wherein, regenerator primary cyclone 20 entrance and the first turbulent bed regenerator 4 dilute phase section are connected, regenerator primary cyclone 20 outlet is connected by closed conduct with regenerator secondary cyclone 21 entrance, regenerator secondary cyclone 21 is exported and is connected with flue gas collection chamber 22 entrance being positioned at the first turbulent bed regenerator 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. Generally, the first turbulent bed regenerator 4 dilute phase section top can arrange 1��6 regenerator primary cyclone 20 and 1��6 regenerator secondary cyclone 21.
Second turbulent bed regenerator 5 is a column type cylinder, is provided with distributor pipe of cardinal wind 25 bottom it, and bottom is provided with end socket. Second turbulent bed regenerator 5 internal diameter and the first turbulent bed regenerator 4 close phase section internal diameter are identical. The outlet of semi-regeneration stand pipe 33 is positioned at bottom the second turbulent bed regenerator 5, and be coaxial therewith the trocar sheath that arranges by one and be arranged in the middle part of the second turbulent bed regenerator 5 or the semi regeneration catalyst dispenser 28 of bottom is connected, form annular space 55c between semi-regeneration stand pipe 22 and described trocar sheath.
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 and flood head piece form and stream bucket is flooded in setting. Heavy oil regenerator sloped tube 34, lighter hydrocarbons regenerator sloped tube 35, external warmer catalyst inlet pipe 36, low temperature catalyst circulation pipe 37 and low temperature catalyst conveying pipe 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 catalyst to walk short circuit, the distance between external warmer catalyst inlet pipe 36 entrance and low temperature catalyst circulation pipe 37 outlet is not less than 3 meters.
A kind of double; two settler Double-lifted pipe catalytic cracking devices of the present invention shown in Fig. 2, with the main difference part of a kind of single settler Double-lifted pipe catalytic cracking device of the present invention shown in Fig. 1 it is, in this device, set up special heavy oil reacting-settler 2 and light hydrogen cracking settler 3 respectively. Heavy oil reacting-settler 2 dilute phase section is positioned at above the first turbulent bed regenerator 4, heavy oil reacting-settler 2 and the first turbulent bed regenerator 4 and the second turbulent bed regenerator 5 are coaxially disposed, and light hydrogen cracking settler 3 and the first turbulent bed regenerator 4 and the second turbulent bed regenerator 5 height are set up in parallel. The close phase section of heavy oil reacting-settler 2 is heavy oil reclaimable catalyst stripping section 10, and heavy oil reclaimable catalyst stripping section 10 is positioned at the first turbulent bed regenerator 4 dilute phase section; The close phase section of light hydrogen cracking settler 3 is lighter hydrocarbons reclaimable catalyst stripping section 11. Heavy oil riser 7 horizontal segment enters heavy oil reacting-settler 2 dilute phase section top through wall. Lighter hydrocarbons riser 8 only vertical section, is coaxially disposed with light hydrogen cracking settler 3, and enters light hydrogen cracking settler 3 dilute phase section top through lighter hydrocarbons reclaimable catalyst stripping section 11; Three layers lighter hydrocarbons feed nozzle 13a, 13b, 13c is all arranged in the vertical section of lighter hydrocarbons riser 8. Heavy oil reaction collection chamber 18 and light hydrogen cracking collection chamber 19 lay respectively at heavy oil reacting-settler 2 and the top of light hydrogen cracking settler 3. It is provided with 1 heavy oil in heavy oil reacting-settler 2 and reacts thick cyclone separator 14 and 1 heavy oil reaction primary cyclone 16, in light hydrogen cracking settler 3, be provided with 1 thick cyclone separator 15 of light hydrogen cracking and 1 light hydrogen cracking primary cyclone 17. It is provided with distribution of steam pipe 23b bottom heavy oil reclaimable catalyst stripping section 10, and is connected with the first turbulent bed regenerator 4 close phase section top with old catalyst distrbutor 27 by heavy oil regeneration standpipe 30; It is provided with distribution of steam pipe 23c bottom lighter hydrocarbons reclaimable catalyst stripping section 11, and is connected with the first turbulent bed regenerator 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. Generally, heavy oil reacting-settler 2 dilute phase section top can arrange 1 heavy oil and react thick cyclone separator 14 and 1��4 heavy oil reaction primary cyclone 16, and light hydrogen cracking settler 3 dilute phase section top can arrange 1 thick cyclone separator 15 of light hydrogen cracking and 1��4 light hydrogen cracking primary cyclone 17.
Another kind of double; two settler Double-lifted pipe catalytic cracking devices of the present invention shown in Fig. 3, with the main difference part of a kind of pair of settler Double-lifted pipe catalytic cracking device of the present invention shown in Fig. 2 it is, in this device, heavy oil reacting-settler 2 and the first turbulent bed regenerator 4 and the second turbulent bed regenerator 5 height are set up in parallel. Heavy oil riser 7 only vertical section, is coaxially disposed with heavy oil reacting-settler 2, and enters heavy oil reacting-settler 2 dilute phase section top through heavy oil reclaimable catalyst stripping section 10; Three layers heavy oil feed nozzle 12a, 12b, 12c is all arranged in the vertical section of heavy oil riser 7. Heavy oil reclaimable catalyst stripping section 10 is connected with the first turbulent bed regenerator 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 pipe 37, low temperature catalyst conveying pipe 38, heavy oil riser 7, lighter hydrocarbons riser 8, public settler 1, heavy oil reacting-settler 2, light hydrogen cracking settler 3, first turbulent bed regenerator 4, second turbulent bed regenerator 5, external warmer 6, heavy oil reacts thick cyclone separator 14, the thick cyclone separator 15 of light hydrogen cracking, heavy oil reaction primary cyclone 16, light hydrogen cracking primary cyclone 17, regenerator primary cyclone 20, regenerator secondary cyclone 21 is internal is all lined with insulating and wearing-resistant lining. the model of lining and thickness are determined according to the operation temperature at each position and catalyst flowing linear speed and chips washing system. the internal diameter of equipment of the present invention or pipeline, for being provided with equipment or the pipeline of insulating and wearing-resistant lining, each means the internal diameter of corresponding insulating and wearing-resistant lining.
In the present invention, heavy oil riser 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 7 being composed in series by vertical section and horizontal segment shown in Fig. 1 and Fig. 2, vertical segment length is generally 30��55m, and the length of horizontal segment is generally 5��10m. For only including the heavy oil riser 7 of vertical section shown in Fig. 3, vertical segment length is generally 40��60m.
In the present invention, lighter hydrocarbons riser 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 8 being composed in series by vertical section and horizontal segment shown in Fig. 1, vertical segment length is generally 30��55m, and the length of horizontal segment is generally 5��10m. For only including the lighter hydrocarbons riser 8 of vertical section shown in Fig. 2 and Fig. 3, vertical segment length is generally 40��60m.
In the present invention, heavy oil riser 7 and lighter hydrocarbons riser 8 meet the general features of the riser that Conventional riser catalytic cracking unit adopts. The concrete length of its each several part can design linear speed according to design oil preparation time of contact of two risers, each several part respectively, the parameters such as the physical dimension of each settler and each regenerator and the pressure balance of whole catalytic cracking unit, adopt the design and calculation method of Conventional riser catalytic cracking unit riser to be determined. The concrete internal diameter of two riser each several parts respectively according to parameters such as the design linear speeds of the Design Treatment amount of each riser, water vapour and pre-lift medium consumption and two riser each several parts, can adopt the design and calculation method of Conventional riser catalytic cracking unit riser to be determined.
In the present invention, heavy oil feed nozzle and lighter hydrocarbons feed nozzle belong to existing conventional equipment, meet the general features 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 operating conditions such as the physical dimension of two risers, Design Treatment amount and atomizing steam amounts respectively. Position is specifically set can being calculated determining according to parameters such as the design linear speeds of the oil preparation time of contact required for each stock heavy oil feed and lighter hydrocarbons charging and each riser conversion zone respectively of each layer heavy oil feed nozzle and lighter hydrocarbons feed nozzle. The concrete material of heavy oil feed nozzle and lighter hydrocarbons feed nozzle can character and operating condition according to each stock heavy oil feed and lighter hydrocarbons charging be determined 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 pipe 37 internal diameter is generally 150��900mm, low temperature catalyst conveying pipe 38 internal diameter is generally 150��900mm.Above-mentioned several catalyst transports belong to existing conventional equipment, meet the general features of dense-phase catalyst conveyance conduit. Its concrete structure and size can adopt the design and calculation method of dense-phase catalyst conveyance conduit to be determined according to the space layout of the catalyst circulating load of each catalyst recycle circuit of device and device.
In the present invention, the first turbulent bed regenerator 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 regenerator 5 internal diameter is generally 2400��16000mm. First turbulent bed regenerator 4 and the second turbulent bed regenerator 5 meet the general features of the turbulent bed regenerator that Conventional riser catalytic cracking unit adopts. Can according to the design linear speed of the design coke-burning capacity of the first turbulent bed regenerator 4 with coke burning degree, the first each position of turbulent bed regenerator 4, and the Parameter Conditions such as the physical dimension of regenerator primary cyclone 20 and regenerator secondary cyclone 21 and mounting means, adopt the design and calculation method of existing catalytic cracking unit turbulent bed regenerator to determine the concrete structure size at the first each position of turbulent bed regenerator 4. The internal diameter of the second turbulent bed regenerator 5 and the internal diameter n of the first turbulent bed regenerator 4 close phase section are identical. Can according to the temperature range of the first turbulent bed regenerator 4 and the second turbulent bed regenerator 5, the concentration limit of the second turbulent bed regenerator flue gas entrained catalyst particles, the design linear speed of the second turbulent bed regenerator 5 and internal diameter, and the Parameter Conditions such as the physical dimension of distributor pipe of cardinal wind 25 and supporting construction, the total height of the second turbulent bed regenerator 5 is determined in conjunction with gas-solid direct heat transfer rule and transport disengaging height computational methods.
In the present invention, public settler 1, heavy oil reacting-settler 2 and light hydrogen cracking settler 3 belong to existing conventional equipment, meet the general features of conventional lift tubular type catalytic cracking unit settler. Its concrete structure size can adopt the design and calculation method of existing catalytic cracking unit settler to be determined according to the operating 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 operating condition of device.
In the present invention, heavy oil reacts thick cyclone separator 14, the thick cyclone separator of light hydrogen cracking 15, heavy oil reaction primary cyclone 16, light hydrogen cracking primary cyclone 17 and regenerator primary cyclone 20 and regenerator secondary cyclone 21 belongs to existing conventional equipment. Its concrete structure size and space layout can adopt the design and calculation method of existing cyclone separator to be determined according to the operating condition of device.
In the present invention, distribution of steam pipe 23a, 23b, 23c, 23d, 23e and distributor pipe of cardinal wind 25 can adopt dendriform distributor pipe or annular spread pipe, belong to existing conventional equipment. Its concrete structure size and space layout can adopt the design and calculation method of existing distribution of steam pipe and distributor pipe of cardinal wind to be determined according to the operating condition of device.
In the present invention, pre-lift medium spray head 26a, 26b belong to existing conventional equipment. Its concrete structure size, position and space layout are set the design and calculation method that pre existing promotes medium spray head can be adopted to be determined according to the operating condition of device.
In the present invention, flue gas distributor 24 can adopt dish, plate shaped or arch distribution grid, 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 operating condition of device.
In the present invention, the stream bucket that floods of semi-regeneration stand pipe 33, heavy oil regenerator sloped tube 34, lighter hydrocarbons regenerator sloped tube 35 and the setting of external warmer catalyst inlet pipe 36 porch 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 operating condition of device.
In the present invention, old catalyst distrbutor 27 and semi regeneration catalyst dispenser 28 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 operating 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 contact with catalyst heavy oil riser 7 in that to mix and carry out oil preparation be the catalytic cracking reaction of 0.2��1.5 second time of contact, and lighter hydrocarbons charging 48a, 48b, 48c contact with regeneration catalyzing agent in lighter hydrocarbons riser 8 and mix and carry out catalytic reforming reaction. Heavy oil reaction logistics and light hydrogen cracking logistics respectively enter public settler 1 and carry out gas solid separation, isolated heavy oil reaction oil gas and light hydrogen cracking oil gas respectively enter heavy oil reaction oil gas fractionating column and light hydrogen cracking oil gas fractionating column carries out fractional distillation, isolated heavy oil reclaimable catalyst and lighter hydrocarbons reclaimable catalyst entrance mixing reclaimable catalyst stripping section 9 and strips. The generation coke of the first turbulent bed regenerator 4 and the second turbulent bed regenerator flue gas counter current contacting burning-off more than 90% is entered through steam stripped mixing reclaimable catalyst (including heavy oil reclaimable catalyst and lighter hydrocarbons reclaimable catalyst). Semi regeneration catalyst enters the second turbulent bed regenerator 5, cools down with the remaining generation coke of main air 49 counter current contacting burning-off heat exchange, and regeneration catalyzing agent returns heavy oil riser 7 respectively and lighter hydrocarbons riser 8 recycles.
In above operating process, heavy oil riser 7 processes three kinds of heavy oil feed 47a, 47b, 47c simultaneously, and lighter hydrocarbons riser 8 processes three kinds of lighter hydrocarbons charging 48a, 48b, 48c simultaneously. According to reaction needed, three kinds of heavy oil feed 47a, 47b, 47c enter heavy oil riser 7 from three layers heavy oil feed nozzle 12a, 12b, 12c respectively, and three kinds of lighter hydrocarbons charging 48a, 48b, 48c enter lighter hydrocarbons riser 8 from three layers lighter hydrocarbons feed nozzle 13a, 13b, 13c respectively.
In above operating process, the regeneration catalyzing agent in the second turbulent bed regenerator 5 is divided into two parts. A portion enters bottom heavy oil riser 7 down through heavy oil regenerator sloped tube 34 bottom the second turbulent bed regenerator 5, first undertaken loosening and fluidizing by the water vapour 50 passed into through distribution of steam pipe 23d, then contacted with heavy oil feed 47a, 47b, 47c by after the pre-lift medium spray head 26a pre-lift medium 51 passed into promotes a up segment distance. Another part regeneration catalyzing agent enters bottom lighter hydrocarbons riser 8 down through lighter hydrocarbons regenerator sloped tube 35 bottom the second turbulent bed regenerator 5, first undertaken loosening and fluidizing by the water vapour 50 passed into through distribution of steam pipe 23e, then contacted with lighter hydrocarbons charging 48a, 48b, 48c by after the pre-lift medium spray head 26b pre-lift medium 51 passed into promotes a up segment distance.
In above operating process, heavy oil reaction logistics enters, through closed conduct, the heavy oil thick cyclone separator 14 of reaction being positioned at public settler 1 from heavy oil riser 7 horizontal segment and carries 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, through closed conduct, the thick cyclone separator 15 of light hydrogen cracking being positioned at public settler 1 from lighter hydrocarbons riser 8 horizontal segment 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 being stripped out and a small amount of catalyst carried secretly thereof) produced in stripping process is divided into two parts, 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 reaction thick cyclone separator 14 isolated heavy oil reclaimable catalyst, the isolated lighter hydrocarbons reclaimable catalyst of the thick cyclone separator of light hydrogen cracking 15 and heavy oil reaction primary cyclone 16 and light hydrogen cracking primary cyclone 17 isolated mixing reclaimable catalyst enter mixing reclaimable catalyst stripping section through each cyclone dip-leg, are stripped by through the distribution of steam pipe 23a water vapour 50 passed into. The hydro carbons oil gas that heavy oil reaction oil gas and a part are stripped out enters heavy oil reaction oil gas fractionating column as heavy oil reaction oil gas fractionating column charging 52 through heavy oil reaction collection chamber 18 and heavy oil reaction oil gas pipeline and carries out fractional distillation, and the hydro carbons oil gas that light hydrogen cracking oil gas and another part are stripped out enters light hydrogen cracking oil gas fractionating column as light hydrogen cracking oil gas fractionating column charging 53 through light hydrogen cracking collection chamber 19 and light hydrogen cracking oil-gas pipeline and carries out fractional distillation.
In above operating process, enter the first turbulent bed regenerator 4 close phase section top through steam stripped mixing reclaimable catalyst down through mixing regeneration standpipe 29 and old catalyst distrbutor 27, contact with the second turbulent bed regenerator flue gas entering the first turbulent bed regenerator 4 from flue gas distributor 24. First turbulent bed regenerator flue gas 54 and a small amount of catalyst granules carried secretly thereof carry out gas solid separation through regenerator primary cyclone 20 and regenerator secondary cyclone 21 successively, isolated catalyst granules returns the first close phase section of turbulent bed regenerator 4 through the dipleg of each cyclone separator of regenerator, 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 catalyst down through semi-regeneration stand pipe 33, upwards enter the second turbulent bed regenerator 5 through annular space 55c and semi regeneration catalyst dispenser 28 again, contacts with the main air 49 entering the second turbulent bed regenerator 5 from distributor pipe of cardinal wind 25 bottom the first close phase section of turbulent bed regenerator 4.
In above operating process, the heat balance of full device carries out auxiliary adjustment by external warmer 6, namely as required through external warmer catalyst inlet pipe 36, a part of semi regeneration catalyst is introduced heat collector 6 from the first close phase pars infrasegmentalis of turbulent bed regenerator 4 and cools down. Low temperature semi regeneration catalyst after external warmer 6 cools down can all return to the first turbulent bed regenerator 4 close phase section top through low temperature catalyst circulation pipe 37, or carries pipe 38 to fully enter bottom heavy oil riser 7 through low temperature catalyst. Low temperature semi regeneration catalyst after this cooling or be divided into two parts, a part returns to the first turbulent bed regenerator 4 close phase section top through low temperature catalyst circulation pipe 37, and another part carries pipe 38 to enter bottom heavy oil riser 7 through low temperature catalyst. The operating condition of external warmer 6, it is possible to adjust flexibly according to the change of heat-obtaining load.
Part or all of low temperature semi regeneration catalyst after external warmer 6 cools down is being returned to the first turbulent bed regenerator 5 close phase section top through low temperature catalyst circulation pipe 37, need to passing into a small amount of for carrying the main air of catalyst in low temperature catalyst circulation pipe 37, this strand of main air participates in burning by entering the first close phase section of turbulent bed regenerator 4.Being not belonging to above-mentioned situation, main air all enters the second turbulent bed regenerator 5 from distributor pipe of cardinal wind 25, and the first turbulent bed regenerator 4 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 complete regeneration burning-off.
The catalyst participating in reaction of the present invention, refer to the regeneration catalyzing agent entered bottom heavy oil riser 7 and bottom lighter hydrocarbons riser 8 or the mixed catalyst that the regeneration catalyzing agent bottom entrance heavy oil riser 7 and the low temperature semi regeneration catalyst after cooling form. Reclaimable catalyst (includes heavy oil reclaimable catalyst and lighter hydrocarbons reclaimable catalyst) in the first turbulent bed regenerator 5 after the generation coke of burning-off more than 90%, and the activity of the semi regeneration catalyst of generation is equivalent to more than the 95% of regeneration catalyzing agent activity.
In above operating process, the flow of the regeneration catalyzing agent entering heavy oil riser 7 and lighter hydrocarbons riser 8 from the second turbulent bed regenerator 5 is adjusted by heavy oil regeneration guiding valve 42 and lighter hydrocarbons regeneration guiding valve 43 respectively, the second turbulent bed regenerator 5 and external warmer 6 is entered from the first turbulent bed regenerator 4, the first turbulent bed regenerator 4 is returned from external warmer 6, the flow of semi regeneration catalyst of heavy oil riser 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 is adjusted.
The method that Double-lifted pipe catalytic cracking device shown in Fig. 2 carries out double lift pipe catalytic cracking of the present invention is adopted to carry out being differing primarily in of double lift pipe catalytic cracking method with adopting Fig. 1 shown device: lighter hydrocarbons charging carries out catalytic reforming reaction in the lighter hydrocarbons riser 8 of only vertical section. Heavy oil reaction logistics 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 settler 3. Heavy oil reclaimable catalyst strips at heavy oil reclaimable catalyst stripping section 10, and lighter hydrocarbons reclaimable catalyst strips at lighter hydrocarbons reclaimable catalyst stripping section 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 regenerator 4 close phase section top is entered down through heavy oil regeneration standpipe 30 and old catalyst distrbutor 27 through steam stripped heavy oil reclaimable catalyst; Entering the first turbulent bed regenerator 4 close phase section top through steam stripped lighter hydrocarbons reclaimable catalyst down through lighter hydrocarbons inclined tube to be generated 32 and old catalyst distrbutor 27, the flow of this strand of catalyst is adjusted by lighter hydrocarbons guiding valve 40 to be generated.
The method that Double-lifted pipe catalytic cracking device shown in Fig. 3 carries out double lift pipe catalytic cracking of the present invention is adopted to carry out being differing primarily in of double lift pipe catalytic cracking method with adopting Fig. 2 shown device: heavy oil feed carries out catalytic cracking reaction in the heavy oil riser 7 of only vertical section. Entering the first turbulent bed regenerator 4 close phase section top through steam stripped heavy oil reclaimable catalyst down through heavy oil inclined tube to be generated 31 and old catalyst distrbutor 27, the flow of this strand of catalyst is adjusted by heavy oil guiding valve 39 to be generated.
In the present invention, heavy oil riser 7 can process 1��5 kind of heavy oil feed simultaneously. Heavy oil feed includes reduced crude, decompression residuum, straight-run gas oil, wax tailings, deasphalted oil, hydrogenation tail oil, recycle oil, slurry oil, crude oil, shale oil, artificial oil, coal tar. Different types of heavy oil feed, according to reaction needed, enters heavy oil riser 7 from each layer heavy oil feed nozzle being axially disposed within diverse location along heavy oil riser 7, contacts with catalyst and react.Lighter hydrocarbons riser 8 can process 1��5 kind of lighter hydrocarbons charging simultaneously. Lighter hydrocarbons charging includes catalytically cracked gasoline, light FCC gasoline, coker gasoline, direct steaming gasoline, aerostatic press condensed oil. Different types of lighter hydrocarbons charging, according to reaction needed, enters lighter hydrocarbons riser 8 from each layer lighter hydrocarbons feed nozzle being axially disposed within diverse location along lighter hydrocarbons riser 8, contacts with catalyst and react. Catalyst used by the present invention, it is possible to be existing various catalytic cracking catalyst (such as CC-20D).
In the present invention, pre-lift medium 51 is steam or dry gas, it is possible to select on demand.
In the present invention, the prevailing operating conditions of heavy oil riser 7 is: reaction temperature (heavy oil riser 7 outlet temperature) is generally 460��560 DEG C, preferably 470��550 DEG C, it is desirable to be 480��540 DEG C; Oil preparation is generally 0.2��1.5s time of contact, preferably 0.4��1.2s, it is desirable to be 0.5��1.0s; Total oil ratio is generally 5��20, and preferably 6��15, it is desirable to be 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, it is desirable to be 65��70.
In the present invention, the prevailing operating conditions of lighter hydrocarbons riser 8 is: reaction temperature (lighter hydrocarbons riser 8 outlet temperature) is generally 450��600 DEG C, preferably 480��580 DEG C, it is desirable to be 500��550 DEG C; Oil preparation is generally 0.2��2.5s time of contact, preferably 0.5��2.0s, it is desirable to be 0.8��1.5s; Total oil ratio is generally 4��20, and preferably 6��15, it is desirable to be 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, it is desirable to be 65��70.
In the present invention, the prevailing operating conditions of public settler 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 settler 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 section 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/tcat(kg water steam/ton catalyst).
In the present invention, the prevailing operating conditions of heavy oil reclaimable catalyst stripping section 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/tcat��
In the present invention, the prevailing operating conditions of lighter hydrocarbons reclaimable catalyst stripping section 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/tcat��
In the present invention, the prevailing operating conditions of the first turbulent bed regenerator 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 adopting the device of plate shaped flue gas distributor, the first turbulent bed regenerator 4 height of dense phase refers to the distance of the first turbulent bed regenerator 4 level of dense bed and flue gas distributor 24, for adopting dish or the device of arch flue gas distributor, first turbulent bed regenerator 4 height of dense phase refers to the distance of the first turbulent bed regenerator 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 regenerator 4 dilute phase settling height refers to regenerator primary cyclone 20 entrance and the distance of the first turbulent bed regenerator 4 level of dense bed), coke burning degree is generally 70��180kg/ (t h), 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 regenerator 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 the 3��5m distance of the second turbulent bed regenerator 5 level of dense bed and distributor pipe of cardinal wind 25 lower surface (second turbulent bed regenerator 5 height of dense phase refer to), dilute phase linear gas velocity is generally 0.7��1.0m/s, dilute phase height is generally 5��8m (for adopting the device of plate shaped flue gas distributor, second turbulent bed regenerator 5 dilute phase height refers to the distance of the second turbulent bed regenerator 5 level of dense bed and flue gas distributor 24, for adopting dish or the device of arch flue gas distributor, second turbulent bed regenerator 5 dilute phase height refers to the distance of the second turbulent bed regenerator 5 level of dense bed and flue gas distributor 24 curved surface lower end), coke burning degree is generally 40��100kg/ (t h), and char length is generally 1.0��3.0min.
The percent that the present invention mentions, except represent regeneration catalyzing agent activity and represent except percentage by volume with v%, be percetage by weight.
Comparative example and embodiment
Comparative example
Conventional single settler double lift pipe catalytic cracking pilot-plant is tested. This pilot-plant arranges a turbulent bed regenerator, is not provided with external warmer. The Design Treatment amount of heavy oil riser is 60kg/d (kg/day), and the Design Treatment amount of lighter hydrocarbons riser is 24kg/d. Heavy oil riser and lighter hydrocarbons riser are respectively provided with one layer of heavy oil feed nozzle and one layer of lighter hydrocarbons feed nozzle.
In comparative example, the heavy oil feedstock of heavy oil riser processing is Daqing atmospheric residue, and the light hydrocarbon feedstocks of lighter hydrocarbons riser processing is attached most importance to the catalytic gasoline that oil riser produces, and catalyst adopts commercially available CC-20D catalytic cracking industry equilibrium catalyst. In comparative example, described charging refers to Daqing atmospheric residue and recycle oil for heavy oil riser, refers to the catalytic gasoline that heavy oil riser produces for lighter hydrocarbons riser. Heavy oil riser simulates the operation of full freshening, and heavy oil feedstock enters heavy oil riser through same layer heavy oil feed nozzle after mixing with recycle oil; Lighter hydrocarbons riser one-pass operation. The phosphorus content of regeneration catalyzing agent is 0.03%, and micro-activity is 62. The stripping fluid of mixing reclaimable catalyst stripping section is water vapour, and stripping temperature is 500 DEG C.
Heavy oil feedstock character is in Table 1, the prevailing operating conditions of comparative example and product slates in Table 2, and fluid product main character is in Table 3.
Embodiment
Embodiment 1��5 is tested being similar on the single settler double lift pipe catalytic cracking pilot-plant shown in Fig. 1 of the present invention. With Fig. 1 shown device the difference is that, in this pilot-plant, heavy oil riser arranges two-layer heavy oil feed nozzle, and lighter hydrocarbons riser arranges two-layer lighter hydrocarbons feed nozzle; It is not provided with external warmer, it does not have external warmer catalyst inlet pipe, external warmer entrance guiding valve, low temperature catalyst circulation pipe, low temperature catalyst circulation guiding valve, low temperature catalyst conveying pipe, low temperature catalyst conveying guiding valve. The Design Treatment amount of heavy oil riser is 60kg/d, and the Design Treatment amount of lighter hydrocarbons riser is 30kg/d. The internal diameter of heavy oil riser conversion zone and lighter hydrocarbons riser conversion zone can need to be modified according to technique.
In embodiment 1��5, the heavy oil feedstock of heavy oil riser processing is the Daqing atmospheric residue identical with comparative example, the light hydrocarbon feedstocks of lighter hydrocarbons riser processing is attached most importance to the catalytic gasoline that oil riser produces, and catalyst adopts the commercially available CC-20D catalytic cracking industry equilibrium catalyst identical with comparative example.In embodiment, described charging refers to Daqing atmospheric residue and recycle oil for heavy oil riser, refers to the catalytic gasoline that heavy oil riser produces for lighter hydrocarbons riser, and described raw material refers to Daqing atmospheric residue for heavy oil riser, refers to the catalytic gasoline that heavy oil riser produces for lighter hydrocarbons riser. Heavy oil riser simulates the operation of full freshening, and heavy oil feedstock and recycle oil are each respectively enters heavy oil riser from one layer of heavy oil feed nozzle; Lighter hydrocarbons riser one-pass operation, light hydrocarbon feedstocks enters lighter hydrocarbons riser from one layer of lighter hydrocarbons feed nozzle. The phosphorus content of regeneration catalyzing agent is 0.03%, and micro-activity is 62. The stripping fluid of mixing reclaimable catalyst stripping section is water vapour, and stripping temperature is 500 DEG C.
The prevailing operating conditions of embodiment 1 and product slates are in Table 4, and fluid product main character is in Table 5. The prevailing operating conditions of embodiment 2 and product slates are in Table 6, and fluid product main character is in Table 7. The prevailing operating conditions of embodiment 3 and product slates are in Table 8, and fluid product main character is in Table 9. The prevailing operating conditions of embodiment 4 and product slates are in Table 10, and fluid product main character is in Table 11. The prevailing operating conditions of embodiment 5 and product slates are in Table 12, and fluid 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), kg m-3 900.2
Carbon residue, % 4.2
Race forms, %
Saturated hydrocarbons 62.3
Aromatic hydrocarbons 22.6
Colloid+asphalitine 15.1
Sulfur content, �� g g-1 1450
Ni, �� g g-1 4.3
V, �� g g-1 0.2
The prevailing operating conditions of table 2 comparative example and product slates
The fluid product main character of table 3 comparative example
The prevailing operating conditions of table 4 embodiment 1 and product slates
The fluid product main character of table 5 embodiment 1
The prevailing operating conditions of table 6 embodiment 2 and product slates
The fluid product main character of table 7 embodiment 2
The prevailing operating conditions of table 8 embodiment 3 and product slates
The fluid product main character of table 9 embodiment 3
The prevailing operating conditions of table 10 embodiment 4 and product slates
The fluid product main character of table 11 embodiment 4
The prevailing operating conditions of table 12 embodiment 5 and product slates
The fluid product main character of table 13 embodiment 5

Claims (11)

1. a double lift pipe catalytic cracking method, heavy oil feed contacts mixing in heavy oil riser and carries out catalytic cracking reaction with catalyst, lighter hydrocarbons charging contacts mixing in lighter hydrocarbons riser and carries out catalytic reforming reaction with catalyst, heavy oil reaction logistics and light hydrogen cracking logistics enter each special cyclone separator 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 respectively enter each special fractionating column and carry out fractional distillation, heavy oil reclaimable catalyst and lighter hydrocarbons reclaimable catalyst carry out turbulent bed regeneration after stripping, regeneration catalyzing agent returns heavy oil riser respectively and lighter hydrocarbons riser recycles, it is characterized in that: oil preparation time of contact of heavy oil feed is 0.2��1.5s, the first turbulent bed regenerator is entered through steam stripped heavy oil reclaimable catalyst and lighter hydrocarbons reclaimable catalyst, with enter the second turbulent bed regenerator flue gas counter current contacting of the first turbulent bed regenerator the generation coke of burning-off more than 90% from flue gas distributor, semi regeneration catalyst is downwardly into the second turbulent bed regenerator, cool down with the remaining generation coke of main air counter current contacting burning-off heat exchange, regenerative process only directly carries main air to the second turbulent bed regenerator, main air is not directly carried to the first turbulent bed regenerator, main air amount is determined according to amount of burnt, meet the demand all generating coke with complete regeneration burning-off.
2. according to the double lift pipe catalytic cracking method described in claim 1, it is characterised in that: described heavy oil riser processes 1��5 kind of heavy oil feed simultaneously, and lighter hydrocarbons riser processes 1��5 kind of lighter hydrocarbons charging simultaneously.
3. according to the double lift pipe catalytic cracking method described in claim 1, it is characterized in that: a part of semi regeneration catalyst is introduced external warmer from the first close phase pars infrasegmentalis of turbulent bed regenerator and cools down, semi regeneration catalyst after cooling all returns to the first turbulent bed regenerator close phase section top or fully enters bottom heavy oil riser, or it is divided into two parts, a part returns to the first turbulent bed regenerator close phase section top, and another part enters bottom heavy oil riser.
4. according to the double lift pipe catalytic cracking method described in claim 1, it is characterized in that: the operating condition of described heavy oil riser is, reaction temperature is 460��560 DEG C, total 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 operating condition of lighter hydrocarbons riser is, reaction temperature is 450��600 DEG C, oil preparation time of contact is 0.2��2.5s, total 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 operating condition of the first turbulent bed regenerator 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/ (t h), char length is 5.0��10.0min, top absolute pressure is 0.22��0.40MPa, the operating condition of the second turbulent bed regenerator 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/ (t h), char length is 1.0��3.0min.
5. the Double-lifted pipe catalytic cracking device being used for the method described in claim 1 that realizes, mainly include heavy oil riser, lighter hydrocarbons riser, settler, regenerator, the outlet of heavy oil riser is connected with each special cyclone inlet respectively through closed conduct with the outlet of lighter hydrocarbons riser, cyclone separator is connected by the close phase section of dipleg and settler, the close phase section of settler is stripping section, it is characterized in that: heavy oil riser conversion zone length is 10��20m, regenerator includes the first turbulent bed regenerator and the second turbulent bed regenerator, first turbulent bed regenerator is positioned at above the second turbulent bed regenerator, both are coaxially disposed, separated by flue gas distributor, second turbulent bed regenerator is a column type cylinder, first turbulent bed regenerator close phase section is identical with the second turbulent bed regenerator internal diameter, it is connected with the first turbulent bed regenerator close phase section top by reclaimable catalyst conveying pipe bottom stripping section, it is connected by semi regeneration catalyst transport and the second turbulent bed regenerator bottom the first close phase section of turbulent bed regenerator, second turbulent bed regenerator bottoms is connected with bottom heavy oil riser and bottom lighter hydrocarbons riser with lighter hydrocarbons regenerated catalyst respectively through heavy oil regenerated catalyst, the bottom of the second turbulent bed regenerator is provided with distributor pipe of cardinal wind, first turbulent bed regenerator is not provided with distributor pipe of cardinal wind.
6. according to the Double-lifted pipe catalytic cracking device described in claim 5, it is characterised in that: described heavy oil riser is provided with 2��5 layers of heavy oil feed nozzle along its axially spaced-apart, and lighter hydrocarbons riser is provided with 2��5 layers of lighter hydrocarbons feed nozzle along its axially spaced-apart.
7. according to the Double-lifted pipe catalytic cracking device described in claim 5, it is characterized in that: described settler is public settler, regenerate with the first turbulent bed regenerator and the second turbulent bed and be coaxially disposed, public settler dilute phase section is positioned at above the first turbulent bed regenerator, the close phase section of public settler is mixing reclaimable catalyst stripping section, mixing reclaimable catalyst stripping section is positioned at the first turbulent bed regenerator dilute phase section, heavy oil riser and lighter hydrocarbons riser are composed in series by vertical section and horizontal segment all from bottom to top, heavy oil riser horizontal segment and lighter hydrocarbons riser horizontal segment are each passed through wall and enter public settler dilute phase section top, reclaimable catalyst conveying pipe 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 the Double-lifted pipe catalytic cracking device described in claim 5, it is characterized in that: described settler includes heavy oil reacting-settler and light hydrogen cracking settler, heavy oil reacting-settler and the first turbulent bed regenerator and the regeneration of the second turbulent bed are coaxially disposed, its dilute phase section is positioned at above the first turbulent bed regenerator, light hydrogen cracking settler and the first turbulent bed regenerator and the second turbulent bed regenerator height are set up in parallel, the close phase section of heavy oil reacting-settler is heavy oil reclaimable catalyst stripping section, the close phase section of light hydrogen cracking settler is lighter hydrocarbons reclaimable catalyst stripping sections, heavy oil reclaimable catalyst stripping section is positioned at the first turbulent bed regenerator dilute phase section, heavy oil riser is composed in series by vertical section and horizontal segment from bottom to top, heavy oil riser horizontal segment enters heavy oil reacting-settler dilute phase section top through wall, lighter hydrocarbons riser only has vertical section, it is coaxially disposed with light hydrogen cracking settler, and enter light hydrogen cracking settler dilute phase section top through lighter hydrocarbons reclaimable catalyst stripping section, reclaimable catalyst conveying pipe include bottom connection heavy oil reclaimable catalyst stripping section with the heavy oil regeneration standpipe on the first turbulent bed regenerator close phase section top and connect bottom lighter hydrocarbons reclaimable catalyst stripping section the lighter hydrocarbons inclined tube to be generated with the first turbulent bed regenerator close phase section top, 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 the Double-lifted pipe catalytic cracking device described in claim 5, it is characterized in that: described settler includes heavy oil reacting-settler and light hydrogen cracking settler, heavy oil reacting-settler and light hydrogen cracking settler are all set up in parallel with the first turbulent bed regenerator and the second turbulent bed regenerator height, the close phase section of heavy oil reacting-settler is heavy oil reclaimable catalyst stripping section, the close phase section of light hydrogen cracking settler is lighter hydrocarbons reclaimable catalyst stripping sections, heavy oil riser and lighter hydrocarbons riser all only have vertical section, it is coaxially disposed with heavy oil reacting-settler and light hydrogen cracking settler respectively, and it is each passed through heavy oil reclaimable catalyst stripping section and lighter hydrocarbons reclaimable catalyst stripping section enters heavy oil reacting-settler dilute phase section top and light hydrogen cracking settler dilute phase section top, reclaimable catalyst conveying pipe include bottom connection heavy oil reclaimable catalyst stripping section with the heavy oil inclined tube to be generated on the first turbulent bed regenerator close phase section top and connect bottom lighter hydrocarbons reclaimable catalyst stripping section the lighter hydrocarbons inclined tube to be generated with the first turbulent bed regenerator close phase section top, 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 the Double-lifted pipe catalytic cracking device described in claim 5, it is characterized in that: the first described turbulent bed regenerator is provided with external warmer, the first close phase pars infrasegmentalis of turbulent bed regenerator is connected with external warmer entrance by external warmer catalyst inlet pipe, and external warmer outlet is connected with bottom the first turbulent bed regenerator close phase section top and heavy oil riser with low temperature catalyst conveying pipe respectively through low temperature catalyst circulation pipe.
11. according to the Double-lifted pipe catalytic cracking device described in claim 5, it is characterized in that: described heavy oil riser 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, lighter hydrocarbons riser total length is 40��60m, wherein, conversion zone length is 10��30m, pre lift zone length is 10��50m, conversion zone internal diameter is 300��2000mm, pre lift zone internal diameter is 150��1000mm, first turbulent bed regenerator close phase section internal diameter n is 2400��16000mm, its dilute phase section internal diameter w is 3000��20000mm, second turbulent bed regenerator internal diameter is 2400��16000mm.
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CN111944558B (en) * 2020-08-23 2024-03-19 浙江工业大学 Reaction regeneration circulation device system in catalytic cracking
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