CN104513670B - A kind of catalyst cracking method and device - Google Patents
A kind of catalyst cracking method and device Download PDFInfo
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- CN104513670B CN104513670B CN201310474471.1A CN201310474471A CN104513670B CN 104513670 B CN104513670 B CN 104513670B CN 201310474471 A CN201310474471 A CN 201310474471A CN 104513670 B CN104513670 B CN 104513670B
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- revivifier
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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
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
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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
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
- C10G11/182—Regeneration
Abstract
The present invention discloses a kind of catalyst cracking method and the device of petroleum chemical industry. Catalyst cracking method comprises: adopting riser tube to carry out finish duration of contact is the heavy oil catalytic cracking reaction of 0.2��1.5s; Reaction logistics carries out gas solid separation by cyclonic separator; Reaction oil gas enters separation column and carries out fractionation; Reclaimable catalyst enters baffle pipe formula revivifier after stripping, main wind co-current contact burns the generation coke going more than 90% with baffling tubular type revivifier in the lump with after the cyclic regeneration catalyst mix without cooling, semi regeneration catalyzer enters turbulent bed revivifier and turbulent bed revivifier main wind counter current contact burning removes remaining generation coke, and regenerated catalyst returns riser tube and recycles. The present invention discloses the catalytic cracking unit for realizing above-mentioned catalyst cracking method. The present invention can be used for heavy oil fluid catalytic cracking.
Description
Technical field
The present invention relates to a kind of catalyst cracking method of petroleum chemical industry and device.
Background technology
At present, generally there is the shortcoming of following several respects in the conventional catalytic cracking unit that petroleum chemical industry uses: first, limiting 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 that the heavy oil feed making unit weight touches 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. 2nd, the time of heavy oil riser tube finish contact is longer (generally at about 4s, s is the second), this also exacerbates the secondary reaction of cracking resultant while improving feedstock conversion, making reacted gas (comprising dry gas and liquefied gas) higher with the product rate of coke, the receipts rate of vapour, diesel oil distillate is lower; Also make the inferior quality of catalytic diesel oil, it is not suitable as vehicle fuel blending group part. For many years, a large amount of research work has been done in the shortcoming existing for above-mentioned conventional catalytic cracking unit overcoming by domestic and international research institution.
The disclosed a kind of catalyst cracking method of Chinese patent CN100338185C and device, its main technology feature is: adopt double lift pipe catalytic cracking device, utilize the technical superiority of double lift pipe catalytic cracking device, by higher for part or all of remaining activity (being about equivalent to the 90% of regenerated catalyst activity), temperature lower (about 500 DEG C) and the catalyst mix device bottom steam stripped lighter hydrocarbons riser tube reclaimable catalyst feeding heavy oil riser tube, heavy oil riser tube is entered together with after mixing from the regenerated catalyst of 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, it is achieved that heavy oil riser tube " finish low temperature contact, high agent-oil ratio " operation, reduces dry gas, coke yield to a certain extent, it is to increase total liquid yield. This technology also exists some deficiency following: first, adopt the measure of lighter hydrocarbons riser tube reclaimable catalyst and regenerated catalyst hybrid cooling, the scheme causing this technology to reduce heavy oil riser tube finish Contact Temperature and rising agent oil ratio is only applicable to have the catalytic cracking unit of more than two riser tubes, and is not suitable for single riser fluid catalytic cracking. 2nd, 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, product slates and product property are brought disadvantageous effect. 3rd, what this technology adopted is traditional riser catalytic cracking reactor, and it is lower that nozzle arranges position, and in fact the finish of heavy oil riser tube can only be controlled to 2��4s duration of contact, and the reaction times being shorter than 2s is difficult to realize. Owing to 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 main technology feature is: arrange a regenerated catalyst water cooler in the lower section of revivifier, regenerated catalyst in revivifier enters wherein through regenerated catalyst, leads to the main wind mixed heat transfer of the cooling in regenerated catalyst water cooler with by cooling main air distributor. Regenerated catalyst after cooling enters riser tube, contacts with charging. The main wind of cooling heated upwards enters in revivifier through the annular space between sleeve pipe and regenerated catalyst, contacts with reclaimable catalyst and carries out coke burning regeneration. Due to above feature, this technology achieves heavy oil riser tube " finish low temperature contact, high agent-oil ratio " operation, reduces dry gas, coke yield to a certain extent, it is to increase 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 need to by cool main air distributor lead to into the main air quantity of cooling limit. Otherwise, the main wind of cooling heated is carried secretly, is upwards flowed in revivifier through the annular space between sleeve pipe and regenerated catalyst by the regenerated catalyst after cooling in a large amount of regenerated catalyst water cooler, forms catalyzer internal recycle, affects device normal running. Restricted owing to cooling main air quantity, thus can affect the cooling performance to high-temperature regenerated catalyst. 2nd, 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.
US Patent No. 6,059, the main feature of a kind of Catalytic Cracking Technique of Heavy Oil disclosed in 958 is: deliver to bottom heavy oil riser tube by part or all of regenerated catalyst after external warmer cools, mixing 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, adopting the measure of the regenerated catalyst after external warmer cools with the high-temperature regenerated catalyst hybrid cooling from 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.2nd, 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.
Chinese patent CN100338185C and US Patent No. 6,059, two kinds of catalytic cracking technologies disclosed in 958 do not make traditional turbulent bed revivifier of any improvement owing to adopting, and the raising of regenerator catalyst internal circulating load can make regenerator bed decrease in temperature and then reduce regeneration efficiency; It is so limited, all cannot improve the agent-oil ratio of heavy oil riser tube by directly improving the catalyst recirculation amount of revivifier, but the method participating in heavy oil catalytic cracking reaction directly by the regenerated catalyst after lighter hydrocarbons reclaimable catalyst and external warmer cool respectively carrys out rising agent oil ratio. Owing to the flow of above-mentioned two kinds of catalyzer is limited, the increase rate of agent-oil ratio is restricted.
Summary of the invention
It is an object of the invention to provide a kind of catalyst cracking method and device, to solve the reduction regenerated catalyst temperature existing for existing catalytic cracking process and to improve the measure scope of application narrower (be not suitable for single riser fluid catalytic cracking or be only applicable to have the catalytic cracking unit of superfluous heat) of heavy oil riser tube agent-oil ratio, underaction is regulated (to adopt main air cooling regenerated catalyst restricted and cooling performance is affected because cooling main air quantity, or by the regenerated catalyst after lighter hydrocarbons reclaimable catalyst or external warmer cool participate in directly method that heavy oil catalytic cracking reaction improves heavy oil riser tube agent-oil ratio due to the flow of two kinds of catalyzer limited and the increase rate of heavy oil riser tube agent-oil ratio is restricted), the catalyst activity lower (impact by lighter hydrocarbons reclaimable catalyst is mixed into) and being difficult to participating in heavy oil catalytic cracking reaction realizes 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 catalyst cracking method, heavy oil feed contacts with regenerated catalyst in riser tube and mixes and carry out catalytic cracking reaction, reaction logistics enters cyclonic separator from riser tube outlet through closed pipeline and carries out gas solid separation, the reaction oil gas isolated enters separation column and carries out fractionation, the reclaimable catalyst isolated carries out coke burning regeneration after stripping, regenerated catalyst returns riser tube and recycles, it is characterized in that: the finish duration of contact in riser tube is 0.2��1.5s, reclaimable catalyst enters baffle pipe formula revivifier after stripping, main wind co-current contact burns the generation coke going more than 90% with baffling tubular type revivifier in the lump with after the cyclic regeneration catalyst mix without cooling, semi regeneration catalyzer enters turbulent bed revivifier and turbulent bed revivifier main wind counter current contact burning removes remaining generation coke.
For realizing the catalytic cracking unit of aforesaid method, comprise riser tube, settling vessel, revivifier, riser tube outlet is connected by closed pipeline with cyclone inlet, 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: riser tube conversion zone length is 10��20m, revivifier comprises baffling tubular type revivifier and turbulent bed revivifier, it is connected with baffling tubular type regenerator bottoms by reclaimable catalyst transfer lime bottom stripping stage, baffling tubular type regenerator outlet is positioned at turbulent bed revivifier dilute phase section bottom, the close phase section of turbulent bed revivifier is connected by bottom regenerated catalyst circulation tube and regenerated catalyst and baffling tubular type regenerator bottoms and riser tube respectively.
Described riser tube can arrange 2��5 layers of feed nozzle along its axially spaced-apart.
A kind of catalytic cracking unit of the present invention, described baffling tubular type revivifier is nested with by inner and outer tubes and forms, and inner and outer tubes are all coaxially arranged with turbulent bed revivifier, interior pipe runs through whole turbulent bed revivifier, outer tube enters turbulent bed revivifier dilute phase section bottom through turbulent bed regenerator overhead end socket, circular channel is formed between interior pipe and outer tube, circular channel bottom end outlet is baffling tubular type regenerator outlet, settling vessel and turbulent bed revivifier are set up in parallel, riser tube and settling vessel are coaxially arranged, and enter settling vessel dilute phase section top through stripping stage, reclaimable catalyst transfer lime is inclined tube to be generated, regenerated catalyst is regenerator sloped tube, the total length of baffling tubular type revivifier is 40��70m, wherein, inner tube length p is 30��45m, outer length of tube q is 10��25m, inner tube diameter is 1200��8000mm, outer tube diameter is 1700��11300mm, turbulent bed revivifier close phase section internal diameter N is 1600��10800mm, turbulent bed revivifier dilute phase section internal diameter K is 3400��22800mm.
Another kind of catalytic cracking unit of the present invention, described baffling tubular type revivifier is by ascension pipe, level pipe and down pipe series winding composition, ascension pipe and down pipe are all vertically arranged, down pipe and turbulent bed revivifier are coaxially arranged, and enter turbulent bed revivifier dilute phase section bottom through turbulent bed regenerator overhead end socket, its bottom end outlet is baffling tubular type regenerator outlet, settling vessel and turbulent bed revivifier are set up in parallel, riser tube and settling vessel are coaxially arranged, and enter settling vessel dilute phase section top through stripping stage, reclaimable catalyst transfer lime is inclined tube to be generated, regenerated catalyst is regenerator sloped tube, the total length of baffling tubular type revivifier is 45��80m, wherein, ascension pipe length u is 30��45m, level pipe length v is 5��10m, down pipe length w is 10��25m, ascension pipe internal diameter is 1200��8000mm, level pipe internal diameter is 900��6000mm, down pipe internal diameter is 1200��8000mm, turbulent bed revivifier close phase section internal diameter n is 1000��7000mm, turbulent bed revivifier dilute phase section internal diameter k is 3300��21600mm.
Compared with existing catalytic cracking technology, adopt the present invention, there is following useful effect:
(1) owing to adopting baffling tubular type revivifier and turbulent bed revivifier series winding to combine to carry out burning and in baffling tubular type revivifier, burn, after reclaimable catalyst and the cyclic regeneration catalyst mix without cooling, the regeneration going 90% more than to generate coke, ensure that baffling tubular type revivifier has higher temperature in, make the coke burning degree that baffling tubular type revivifier can reach higher, thus the comprehensive coke burning degree (total comprehensive coke burning degree refers to the amount of burnt of all revivifiers included by a set of catalytic cracking unit within the unit time and the ratio of the total reserve of all regenerator catalyst) making whole catalytic cracking unit two revivifiers improves (be exactly turbulent bed revivifier is bigger with a catalyst inventory significantly distinguishing turbulent bed revivifier of tubular type revivifier compared with conventional turbulent bed regeneration techniques, thermal capacitance is also bigger, there is not coke and it is difficult to ignition problem. the catalyst inventory of tubular type revivifier is less, thermal capacitance is also less, and when catalyst inlet temperature is lower, coke is difficult to ignition. through the temperature of steam stripped reclaimable catalyst at about 500 DEG C, if directly entering tubular type revivifier, coke is difficult to ignition at this temperature, namely allowing to ignition, coke-burning rate is also lower. there is not this problem in the present invention).From catalytic cracking unit thermal equilibrium relation, catalyst recirculation amount is made to increase the temperature (being to reduce baffling tubular type regenerator outlet temperature and turbulent bed revivifier dense phase temperature for the present invention) that can directly reduce regenerator catalyst bed by changing pressure equilibrium, and this kind of adjustment is very flexibly. Therefore the present invention effectively reduces under can realizing the prerequisite improved in regeneration efficiency on single riser fluid catalytic cracking of any heavy oil feed of processing and flexible participates in the regenerated catalyst temperature of catalytic cracking reaction, thus realize keeping under the prerequisite participating in catalyzer (the being all regenerated catalyst) activity of reaction, carry out riser tube " contact of finish low temperature, high agent-oil ratio " operation, and then suppression heat cracking reaction, promote catalytic cracking reaction, reduce dry gas and coke yield; Make the control to catalytic cracking reaction condition more flexible simultaneously.
(2) owing to adopting the shorter riser reactor of conversion zone length, it is possible to realize shorter finish duration of contact, thus the character making catalytic cracking product slates and catalytic diesel oil is significantly improved.
The present invention can be used for heavy oil fluid catalytic cracking.
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 catalytic cracking unit of the present invention.
Fig. 2 is the schematic diagram of another kind of catalytic cracking unit of the present invention.
In Fig. 1 and Fig. 2, same reference numerals represents identical technology feature. Reference numeral represents: 1. settling vessel, 2. baffling tubular type revivifier, 2a. is nested with in the baffling tubular type revivifier 2 formed to manage by inner and outer tubes, 2b. is nested with the outer tube of the baffling tubular type revivifier 2 formed by inner and outer tubes, the circular channel that 2c. is formed between pipe and outer tube be nested with in the baffling tubular type revivifier 2 formed by inner and outer tubes in, the outlet of 2d. baffling tubular type revivifier 2, 2e. is by ascension pipe, the ascension pipe of the baffling tubular type revivifier 2 of level pipe and down pipe series winding composition, 2f. is by ascension pipe, the level pipe of the baffling tubular type revivifier 2 of level pipe and down pipe series winding composition, 2g. is by ascension pipe, the down pipe of the baffling tubular type revivifier 2 of level pipe and down pipe series winding composition, 3. turbulent bed revivifier, 4. external warmer, 5. riser tube, 6. stripping stage, 7a, 7b, 7c. feed nozzle, 8. thick cyclonic separator, 9. primary cyclone, 10. react collection chamber, 11. revivifier primary cyclones, 12. revivifier secondary cyclones, 13. flue gas collection chambers, 14a, 14b. steam distribution pipe, 15a, 15b. distributor pipe of cardinal wind, 16. pre-lift medium spray heads, 17. inclined tubes to be generated, 18. regenerator sloped tubes, 19. regenerated catalyst circulation tubes, 20. external warmer catalyst inlet pipes, the ring gap formed between the outlet conduit of 21. thick cyclonic separators 8 and the inlet duct of primary cyclone 9, 22. low temperature catalyst transfer limes, 23. guiding valves to be generated, 24. regeneration guiding valves, 25. reprocessing cycle guiding valves, 26. external warmer entrance guiding valves, 27. turbulent bed revivifiers discharge flue gases (generating flue gas and baffling tubular type revivifier by the turbulent bed revivifier isolating granules of catalyst through revivifier primary cyclone 11 and revivifier secondary cyclone 12 to generate flue gas and form), 28. low temperature catalyst conveying guiding valves, 29a, 29b, 29c. heavy oil feed, 30a. enters the baffling main wind of tubular type revivifier of baffling tubular type revivifier 2 by distributor pipe of cardinal wind 15a, 30b. enters the main wind of turbulent bed revivifier of turbulent bed revivifier 3 by distributor pipe of cardinal wind 15b, 31. water vapors, 32. pre-lift media, 33. separation column chargings.
Embodiment
A kind of catalytic cracking unit of the present invention shown in Fig. 1, mainly comprises riser tube 5, settling vessel 1, baffling tubular type revivifier 2 and turbulent bed revivifier 3. Baffling tubular type revivifier 2 is nested with (in namely, pipe 2a top is coaxially inner through outer tube 2b) by interior pipe 2a and outer tube 2b and forms, and interior pipe 2a and outer tube 2b is all coaxially arranged with turbulent bed revivifier 3. Settling vessel 1 and turbulent bed revivifier 3 are set up in parallel (be set up in parallel comprise height be set up in parallel or contour be set up in parallel). The close phase section of settling vessel 1 is stripping stage 6, is connected with bottom baffling tubular type revivifier 2 by inclined tube 17 to be generated bottom stripping stage 6 (in namely bottom pipe 2a). The outlet 2d of baffling tubular type revivifier 2 is positioned at turbulent bed revivifier 3 dilute phase section bottom. The close phase section of turbulent bed revivifier 3 is connected (in namely bottom pipe 2a) with bottom riser tube 5 with bottom baffling tubular type revivifier 2 with regenerator sloped tube 18 by regenerated catalyst circulation tube 19 respectively. Riser tube 5 outlet is positioned at settling vessel 1 dilute phase section top.
Turbulent bed revivifier 3 is the turbulent bed revivifier of existing structure. Turbulent bed revivifier 3 is also provided with external warmer 4, and external warmer 4 is upper intake lower outlet type. The close phase section of turbulent bed revivifier 3 is connected with external warmer 4 entrance by external warmer catalyst inlet pipe 20, and external warmer 4 is exported and is connected with bottom riser tube 5 by low temperature catalyst transfer lime 22.
Riser tube 5 top is provided with air cushion elbow, and bottom is provided with end socket, and bottom is provided with steam distribution pipe 14b, and bottom wall is provided with pre-lift medium spray head 16. Riser tube 5 arranges three layers of feed nozzle 7a, 7b, 7c along its axially spaced-apart. Riser tube 5 and settling vessel 1 are coaxially arranged, and enter settling vessel 1 dilute phase section top through stripping stage 6. Usually, riser tube 5 can arrange 2��5 layers of feed nozzle along its axially spaced-apart.
Settling vessel 1 dilute phase section top, is provided with 1 thick cyclonic separator 8 and 1 primary cyclone 9. Riser tube 5 is exported and is connected with thick cyclonic separator 8 entrance by closed pipeline. Thick cyclonic separator 8 outlet conduit external diameter is less than primary cyclone 9 inlet duct internal diameter, and thick cyclonic separator 8 outlet conduit insertion primary cyclone 9 inlet duct, fixing and centering with auxiliary inner member, the passage that the ring gap 21 formed between two pipelines enters primary cyclone 9 as stripping stream is connected with settling vessel 1 dilute phase section simultaneously. It is connected with stripping stage 6 by dipleg respectively with bottom primary cyclone 9 bottom thick cyclonic separator 8. Primary cyclone 9 is exported and is connected with reaction collection chamber 10 entrance being positioned at settling vessel 1 top by closed pipeline. Reaction collection chamber 10 is exported and is connected with separation column by reaction oil gas pipeline. Being provided with steam distribution pipe 14a bottom stripping stage 6, inclined tube 17 to be generated outlet exports with regenerated catalyst circulation tube 19 and is all connected with the bottom wall of pipe 2a in baffling tubular type revivifier 2. Usually, settling vessel 1 dilute phase section top can arrange 1 thick cyclonic separator 8 and 1��4 primary cyclone 9.
The interior pipe 2a of baffling tubular type revivifier 2 runs through whole turbulent bed revivifier 3; Interior pipe 2a top is uncovered, and bottom is provided with distributor pipe of cardinal wind 15a, and bottom is provided with end socket. The outer tube 2b of baffling tubular type revivifier 2 enters turbulent bed revivifier 3 dilute phase section bottom through turbulent bed revivifier 3 top end socket; Outer tube 2b top is provided with end socket and this end socket is positioned at pipe 2a top end, and bottom is uncovered. Forming circular channel 2c between interior pipe 2a and outer tube 2b, the bottom end outlet of circular channel 2c is the outlet 2d of baffling tubular type revivifier 2.The cross-sectional area of circular channel 2c is equal with the cross-sectional area (calculating by the internal diameter of interior pipe 2a) of interior pipe 2a.
Turbulent bed revivifier 3 dilute phase section top is provided with two revivifier primary cyclones 11 and two revivifier secondary cyclones 12. Wherein, revivifier primary cyclone 11 entrance is connected with turbulent bed revivifier 3 dilute phase section, revivifier primary cyclone 11 outlet is connected by closed pipeline with revivifier secondary cyclone 12 entrance, revivifier secondary cyclone 12 is exported and is connected with flue gas collection chamber 13 entrance by closed pipeline, and flue gas collection chamber 13 is exported and is connected with smoke energy recovering system by flue gas pipeline. Being provided with distributor pipe of cardinal wind 15b bottom the close phase section of turbulent bed revivifier 3, bottom is provided with end socket. Usually, the 2nd turbulent bed revivifier 3 dilute phase section top can arrange 1��6 revivifier primary cyclone 11 and 1��6 revivifier secondary cyclone 12.
Regenerator sloped tube 18, regenerated catalyst circulation tube 19 and external warmer catalyst inlet pipe 20 entrance all adopt and flood stream degree of lip-rounding formula, and stream bucket is flooded in setting. Inclined tube 17 to be generated, regenerator sloped tube 18, regenerated catalyst circulation tube 19, external warmer catalyst inlet pipe 20 and low temperature catalyst transfer lime 22 are respectively equipped with guiding valve 23 to be generated, regeneration guiding valve 24, reprocessing cycle guiding valve 25, external warmer entrance guiding valve 26, low temperature catalyst conveying guiding valve 28.
Another kind of catalytic cracking unit of the present invention shown in Fig. 2, it is: in this device that baffling tubular type revivifier 2 is contacted by ascension pipe 2e, level pipe 2f and down pipe 2g and formed with the main difference part of a kind of catalytic cracking unit of the present invention shown in Fig. 1 in integral arrangement and device structure; Ascension pipe 2e and down pipe 2g is all vertically arranged. Down pipe 2g and turbulent bed revivifier 3 are coaxially arranged, and enter turbulent bed revivifier 3 dilute phase section bottom through turbulent bed revivifier 3 top end socket. The bottom of ascension pipe 2e is the bottom of baffling tubular type revivifier 2. Inclined tube 17 to be generated is connected (inclined tube 17 to be generated outlet exports with regenerated catalyst circulation tube 19 and is all connected with the bottom wall of ascension pipe 2e) with regenerated catalyst circulation tube 19 with bottom ascension pipe 2e. Ascension pipe 2e top is provided with air cushion elbow, and bottom is provided with distributor pipe of cardinal wind 15a, and bottom is provided with end socket; Level pipe 2f exit end is provided with air cushion elbow; The bottom of down pipe 2g is uncovered, and this outlet is the outlet 2d of baffling tubular type revivifier 2. Ascension pipe 2e is identical with down pipe 2g internal diameter, and is greater than level pipe 2f internal diameter.
In the present invention, each equipment body and pipeline are metal material (being generally carbon steel or stainless steel). wherein, inclined tube 17 to be generated, regenerator sloped tube 18, regenerated catalyst circulation tube 19, external warmer catalyst inlet pipe 20, low temperature catalyst transfer lime 22, riser tube 5, settling vessel 1, baffling tubular type revivifier 2 (comprises the interior pipe 2a and outer tube 2b of the tubular type revivifier of baffling shown in Fig. 12, the ascension pipe 2e of the tubular type revivifier of baffling shown in Fig. 22, level pipe 2f and down pipe 2g), turbulent bed revivifier 3, external warmer 4, thick cyclonic separator 8, primary cyclone 9, revivifier primary cyclone 11, revivifier secondary cyclone 12 e-quipment and pipe such as grade, the surface contacted with catalyzer is equipped with insulating and wearing-resistant lining. the model of insulating and wearing-resistant lining and thickness are determined according to the constructional feature of the service temperature at each position and catalyst flow moving-wire speed and e-quipment and pipe. 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, riser tube 5 total length is generally 25��30m, and wherein, conversion zone length is generally 10��20m, and pre lift zone length is generally 5��20m;Conversion zone internal diameter is generally 400��2500mm, and pre lift zone internal diameter is generally 200��1300mm.
In the present invention, riser tube 5 meets the general feature of the riser tube that conventional riser fluid catalytic cracking adopts. The concrete length of its each several part according to the design lines speed of the design finish duration of contact of riser tube 5, each several part, settling vessel 1 and baffling tubular type revivifier 2 and the scantlings of the structure of turbulent bed revivifier 3 and the pressure equilibrium relation of whole catalytic cracking unit, can adopt the design and calculation method of conventional riser fluid catalytic cracking riser tube to be determined. The concrete internal diameter of riser tube 5 each several part according to the designing treatment amount of device, the parameter such as design lines speed of leading to the consumption of the water vapor 31 into riser tube 5 and the consumption of pre-lift medium 32 and riser tube 5 each several part through steam distribution pipe 14b, can adopt the design and calculation method of conventional riser fluid catalytic cracking riser tube to be determined.
In the present invention, feed nozzle belongs to existing conventional equipment, meets the general feature of conventional catalytic cracking feeding nozzle. Its concrete scantlings of the structure and space layout according to operational conditions such as the designing treatment amount of the scantlings of the structure of riser tube 5 and device and atomizing steam amounts, can adopt the design and calculation method of conventional catalytic cracking feeding nozzle to be determined. Position is specifically set can the carrying out calculating according to parameters such as the design lines speed of the finish duration of contact required for each stock heavy oil feed and riser tube 5 conversion zone and determine of each layer feed nozzle. The concrete material of feed nozzle can be determined according to the character of heavy oil feed and operational condition.
In the present invention, inclined tube 17 internal diameter to be generated is generally 300��1800mm, regenerator sloped tube 18 internal diameter is generally 300��1800mm, regenerated catalyst circulation tube 19 internal diameter is generally 200��2500mm, external warmer catalyst inlet pipe 20 internal diameter is generally 150��900mm, and low temperature catalyst transfer lime 22 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 size and space layout according to the space layout of the catalyst recirculation amount of each catalyst recirculation circuit of device and device, can adopt the design and calculation method of dense-phase catalyst transport pipe to be determined.
In the present invention, for adopting the catalytic cracking unit being nested with the baffling tubular type revivifier 2 formed by interior pipe 2a and outer tube 2b shown in Fig. 1, the total length (the length sum of interior pipe 2a and outer tube 2b) of baffling tubular type revivifier 2 is generally 40��70m, wherein, interior pipe 2a length p is generally 30��45m, and outer tube 2b length q is generally 10��25m (this length is the top of insulating and wearing-resistant lining lower surface in the end socket of the outer tube 2b top distance between outer tube 2b bottom end outlet); Interior pipe 2a internal diameter is generally 1200��8000mm, and outer tube 2b internal diameter is generally 1700��11300mm. Turbulent bed revivifier 3 close phase section internal diameter N is generally 1600��10800mm, and dilute phase section internal diameter K is generally 3400��22800mm.
In the present invention, for the catalytic cracking unit adopting the baffling tubular type revivifier 2 being composed in series by ascension pipe 2e, level pipe 2f and down pipe 2g shown in Fig. 2, the total length (the length sum of ascension pipe 2e, level pipe 2f and down pipe 2g) of baffling tubular type revivifier 2 is generally 45��80m, wherein, ascension pipe 2e length u is generally 30��45m, level pipe 2f length v is generally 5��10m, and down pipe 2g length w is generally 10��25m;Ascension pipe 2e internal diameter is generally 1200��8000mm, and level pipe 2f internal diameter is generally 900��6000mm, and down pipe 2g internal diameter is generally 1200��8000mm. Turbulent bed revivifier 3 close phase section internal diameter n is generally 1000��7000mm, and dilute phase section internal diameter k is generally 3300��21600mm.
In the present invention, the structure of baffling tubular type revivifier 2 is bigger with operating method difference compared with the turbulent bed revivifier that conventional riser fluid catalytic cracking adopts, it is necessary to adopt the design and calculation method of dilute phase tubular type revivifier to determine the concrete scantlings of the structure at its each position according to the design lines speed at the design carbon-burning capacity of the pressure equilibrium relation of whole catalytic cracking unit, baffling tubular type revivifier 2 and coke burning degree and each position thereof.
In the present invention, turbulent bed revivifier 3 meets the general feature of the turbulent bed revivifier that conventional riser fluid catalytic cracking adopts, according to the design carbon-burning capacity of turbulent bed revivifier 3 and coke burning degree, the design lines speed at its each position and the parameter condition such as the scantlings of the structure of revivifier primary cyclone 11 and revivifier secondary cyclone 12 and installation mode, the design and calculation method of existing catalytic cracking unit turbulent bed revivifier can be adopted to determine the concrete scantlings of the structure at its each position.
In the present invention, settling vessel 1 belongs to existing conventional equipment, meets the general feature of conventional riser fluid catalytic cracking settling vessel. Its concrete scantlings of the structure 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 4 belongs to existing conventional equipment. Its concrete scantlings of the structure 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, thick cyclonic separator 8, primary cyclone 9 and revivifier primary cyclone 11 and revivifier secondary cyclone 12 belong to existing conventional equipment. Its concrete scantlings of the structure 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 14a, 14b and distributor pipe of cardinal wind 15a, 15b can adopt dendriform distribution pipe or annular spread pipe, all belong to existing conventional equipment. Its concrete scantlings of the structure 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 16 belongs to existing conventional equipment. Its concrete scantlings of the structure, position is set and space layout can be determined according to the design and calculation method that the operational condition of device adopts pre existing to promote medium spray head.
In the present invention, regenerator sloped tube 18, regenerated catalyst circulation tube 19 and external warmer catalyst inlet pipe 20, the stream bucket that floods of its ingress setting all belongs to existing conventional equipment. Its concrete scantlings of the structure can adopt the existing design and calculation method flooding stream bucket to be determined according to the operational condition of device.
The catalytic cracking unit shown in Fig. 1 is adopted to carry out the method for catalytic cracking of the present invention as follows: heavy oil feed contacts with regenerated catalyst in riser tube 5 that to mix and carry out finish duration of contact be the catalytic cracking reaction of 0.2��1.5s. reactant flows to and carries out gas solid separation into settling vessel 1, and the reaction oil gas isolated enters separation column and carries out fractionation, and the reclaimable catalyst isolated enters stripping stage 6 and carries out stripping. baffling tubular type revivifier 2 is entered through steam stripped reclaimable catalyst, (first upwards flow in the lump in the interior pipe 2a of baffling tubular type revivifier 2 with baffling tubular type revivifier main wind 30a after reclaimable catalyst and cyclic regeneration catalyst mix with the baffling tubular type revivifier main wind 30a co-current contact entering baffling tubular type revivifier 2 by distributor pipe of cardinal wind 15a in the lump with after the cyclic regeneration catalyst mix without cooling of turbulent bed revivifier 3 close phase section, enter in baffling tubular type revivifier 2 in the circular channel 2c formed between pipe 2a and outer tube 2b through interior pipe 2a top again and flow downward in the lump) burn the generation coke going more than 90%, generate semi regeneration catalyzer.Semi regeneration catalyzer enters turbulent bed revivifier 3, with by distributor pipe of cardinal wind 15b enter turbulent bed revivifier 3 turbulent bed revivifier main wind 30b counter current contact (turbulent bed revivifier main wind 30b upwards flows, semi regeneration catalyzer flows downward) burn remove remaining generation coke. Regenerated catalyst returns riser tube 5 and recycles. In said process, described burning removes the percentage ratio generating coke, is all taking the weight of coke of heavy oil feed catalytic cracking reaction generation as benchmark. The present invention's main wind used is generally pressurized air.
In above operating process, riser tube 5 processes three kinds of heavy oil feed 29a, 29b, 29c simultaneously. According to reaction needed, three kinds of heavy oil feed 29a, 29b, 29c enter riser tube 5 from three layers of feed nozzle 7a, 7b, 7c respectively. A part of regenerated catalyst in turbulent bed revivifier 3 enters bottom riser tube 5 through regenerator sloped tube 18 downwards from the close phase section of turbulent bed revivifier 3, first by through steam distribution pipe 14b lead to into water vapor 31 carry out loosening and fluidisation, then contact with heavy oil feed 29a, 29b, 29c after promoting upper row one segment distance by the pre-lift medium 32 led to through pre-lift medium spray head 16.
In above operating process, reaction logistics enters thick cyclonic separator 8 from riser tube 5 outlet through closed pipeline and carries out gas solid separation, and the gaseous stream isolated enters primary cyclone 9 and carries out further gas solid separation. The stripping stream (the hydrocarbon-type oil gas gone out by stripping and a small amount of catalyzer carried secretly thereof) produced in stripping process enters primary cyclone 9 through ring gap 21 and carries out gas solid separation. The reclaimable catalyst that thick cyclonic separator 8 and primary cyclone 9 are isolated enters stripping stage 6 through each cyclone dip-leg, by through steam distribution pipe 14a lead to into water vapor 31 carry out stripping. Reaction oil gas and the hydrocarbon-type oil gas gone out by stripping enter separation column as separation column charging 33 through reaction collection chamber 10 and reaction oil gas pipeline and carry out fractionation.
In above operating process, entering bottom the interior pipe 2a of baffling tubular type revivifier 2 through inclined tube 17 to be generated downwards through steam stripped reclaimable catalyst, a part of regenerated catalyst in turbulent bed revivifier 3 close phase section enters bottom interior pipe 2a through regenerated catalyst circulation tube 19 downwards as cyclic regeneration catalyzer. Contact with the main wind 30a of baffling tubular type revivifier after above-mentioned two bursts of catalyst mix.
In above operating process, semi regeneration catalyzer and baffling tubular type revivifier generate flue gas and enter turbulent bed revivifier 3 dilute phase section downwards by the circular channel 2c bottom end outlet (the outlet 2d as baffling tubular type revivifier 2) of baffling tubular type revivifier 2. Semi regeneration catalyzer continues descending until entering turbulent bed revivifier 3 close phase section wind 30b main with turbulent bed revivifier and contacting under gravity; Baffling tubular type revivifier generates flue gas and then makes line speed much slower due to the rapid expansion of actual internal area, and is entrained with a small amount of granules of catalyst together with turbulent bed revivifier generation flue gas and carries out gas solid separation through revivifier primary cyclone 11 and revivifier secondary cyclone 12 successively. The granules of catalyst isolated returns the close phase section of turbulent bed revivifier 3 through the dipleg of each revivifier cyclonic separator, and the flue gas 27 isolated enters smoke energy recovering system through flue gas collection chamber 13 and flue gas pipeline.
In above operating process, the heat balance of full device carries out auxiliary adjustment by external warmer 4, namely as required through external warmer catalyst inlet pipe 20, part regenerated catalyst being introduced external warmer 4 from the close phase section of turbulent bed revivifier 3 to cool, the low-temp recovery catalyzer after external warmer 4 cools all enters bottom riser tube 5 through low temperature catalyst transfer lime 22.The operational condition of external warmer 4, it is possible to adjust flexibly according to the change of heat-obtaining load.
In above operating process, the flow of the regenerated catalyst entering riser tube 5, baffling tubular type revivifier 2 and external warmer 4 from turbulent bed revivifier 3 is regulated by regeneration guiding valve 24, reprocessing cycle guiding valve 25 and external warmer entrance guiding valve 26 respectively. The flow of the regenerated catalyst entering riser tube 5 from external warmer 4 carries guiding valve 28 to regulate by low temperature catalyst, and the flow of the reclaimable catalyst entering baffling tubular type revivifier 2 from stripping stage 6 is regulated by guiding valve 23 to be generated.
The main difference part of the method that the method adopting the catalytic cracking unit shown in Fig. 2 to carry out catalytic cracking of the present invention carries out catalytic cracking with employing Fig. 1 shown device is: the coke burning regeneration carrying out catalyzer in the baffling tubular type revivifier 2 formed of contacting by ascension pipe 2e, level pipe 2f and down pipe 2g. Enter bottom ascension pipe 2e through steam stripped reclaimable catalyst with without the cyclic regeneration catalyzer of cooling. (first upwards flow in the lump in ascension pipe 2e with the main wind 30a of baffling tubular type revivifier after reclaimable catalyst and cyclic regeneration catalyst mix with baffling tubular type revivifier main wind 30a co-current contact in the lump after above-mentioned two bursts of catalyst mix, enter in level pipe 2f horizontal flow in the lump again, finally enter in down pipe 2g and flow downward in the lump). The semi regeneration catalyzer generated enters turbulent bed revivifier 3 downwards from down pipe 2g bottom end outlet (the outlet 2d as baffling tubular type revivifier 2).
In the present invention, riser tube 5 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 riser tube 5 from each layer feed nozzle being axially disposed within different positions along riser tube 5, contacts with catalyzer and react. The catalyzer that the present invention is used, it is possible to be existing various catalytic cracking catalyst (such as CC-20D).
In the present invention, pre-lift medium 32 is water vapor or dry gas, it is possible to select on demand.
In the present invention, the prevailing operating conditions of riser tube 5 is: the temperature of regenerated catalyst participating in reaction is generally 580��700 DEG C [during for over not heat collector 4, this temperature refers to enter the temperature of the regenerated catalyst bottom riser tube 5 through regenerated catalyst (specifically regenerator sloped tube 18), is generally 620��700 DEG C; For over heat collector 4 in the case of, this temperature refers to enter the regenerated catalyst bottom riser tube 5 and the mixing temperature entering the regenerated catalyst bottom riser tube 5 from low temperature catalyst transfer lime 22 through regenerated catalyst (specifically regenerator sloped tube 18), is generally 580��650 DEG C]; Temperature of reaction (outlet temperature of riser) 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, it is preferably 7��12; Oil gas average line speed is generally 8.0��15.0m/s; The activity of regenerated catalyst is generally 58��75, and preferably 62��72, it is preferably 65��70.
In the present invention, the prevailing operating conditions of settling vessel 1 is: dilute phase temperature is generally 470��550 DEG C, and top absolute pressure is generally 0.22��0.40MPa.
In the present invention, the prevailing operating conditions of stripping stage 6 is: stripping temperature is generally 480��560 DEG C, and stripping time is generally 1.0��3.0min, and stripped vapor consumption is generally 2��5kg/tcat(kg water steam/ton catalyzer).
In the present invention, the prevailing operating conditions of baffling tubular type revivifier 2 is: the ratio of the cyclic regeneration catalyzer and the weight rate through steam stripped reclaimable catalyst that enter baffling tubular type revivifier 2 is generally 0.5:1��2:1, the temperature in of baffling tubular type revivifier 2 is generally 560��640 DEG C the mixing temperature of cyclic regeneration catalyzer and reclaimable catalyst and the main wind 30a three of baffling tubular type revivifier entering baffling tubular type revivifier 2 (baffling tubular type revivifier 2 temperature ins be), temperature out is generally 630��750 DEG C, average gas line speed is generally 3.0��5.0m/s, coke burning degree is generally 300��1000kg/ (t h), char length is generally 30��60s. the amount of the main wind 30a of baffling tubular type revivifier is determined according to the amount of burnt of baffling tubular type revivifier 2, meets and burns, in holomorphosis mode, the demand that more than 90% generates coke.
In the present invention, the prevailing operating conditions of turbulent bed revivifier 3 is: dense phase temperature is generally 620��740 DEG C, and (during for over not heat collector 4, this temperature is generally 620��700 DEG C, for over heat collector 4 in the case of, this temperature is generally 650��740 DEG C), dense phase gases line speed is generally 0.7��1.0m/s, height of dense phase is generally 5��8m (turbulent bed revivifier 3 height of dense phase refers to turbulent bed revivifier 3 level of dense bed and the distance of distributor pipe of cardinal wind 15b lower surface), dilute phase linear gas velocity is generally 0.4��0.6m/s, dilute phase settling height is generally 7��10m (turbulent bed revivifier 3 dilute phase settling height refers to revivifier primary cyclone 11 entrance and the distance of turbulent bed revivifier 3 level of dense bed), coke burning degree is generally 50��200kg/ (t h), char length is generally 1.0��3.0min, top absolute pressure is generally 0.20��0.38MPa. the amount of the main wind 30b of turbulent bed revivifier is determined according to the amount of burnt of turbulent bed revivifier 3, meets and burns residue generation coke in holomorphosis mode and maintain the demand of the turbulent bed revivifier 3 normal fluidisation of inner catalyst.
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 riser 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 riser tube is 60kg/d (kg/day), arranges one layer of feed nozzle.
The heavy oil feedstock of comparative example processing is grand celebration long residuum, and catalyzer adopts commercially available CC-20D catalytic cracking industry equilibrium catalyst. In comparative example, heavy oil feed refers to grand celebration long residuum and recycle stock. In comparative example, riser tube simulation is complete returns refining operation, and heavy oil feedstock enters riser tube through same layer feed nozzle after mixing with recycle stock. The carbon content of regenerated catalyst is 0.03%, and micro-activity is 62. The stripping fluid of stripping stage is water vapor, 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 liquid product main character is in table 3.
Embodiment
Embodiment 1��5 is tested on the catalytic cracking pilot plant being similar to Fig. 1 shown device of the present invention. With Fig. 1 shown device the difference is that, the riser tube of this pilot plant arranges two layers of feed nozzle.The designing treatment amount of riser tube is 60kg/d, and the length of the interior pipe of the internal diameter of riser tube conversion zone, baffling tubular type revivifier and outer tube and internal diameter all can be changed according to test needs. Heat collector in process of the test.
The heavy oil feedstock that embodiment 1��5 is processed is the grand celebration long residuum identical with comparative example, and catalyzer adopts the commercially available CC-20D catalytic cracking industry equilibrium catalyst identical with comparative example. In embodiment, heavy oil feed refers to grand celebration long residuum and recycle stock. In embodiment, riser tube simulation is complete returns refining operation, and heavy oil feedstock and recycle stock respectively enter riser tube from one layer of feed nozzle respectively. The carbon content of regenerated catalyst is 0.03%, and micro-activity is 62. The stripping fluid of stripping stage is water vapor, and stripping temperature is 540 DEG C.
The prevailing operating conditions of embodiment 1��5 and product slates are in table 4. The liquid product main character of embodiment 1 is in table 5, and the liquid product main character of embodiment 2 is in table 6, and the liquid product main character of embodiment 3 is in table 7, and the liquid product main character of embodiment 4 is in table 8, and the liquid product main character of embodiment 5 is in table 9.
Table 1 heavy oil feedstock character (comparative example, embodiment 1��5)
| Heavy oil feedstock | Grand celebration long residuum |
| Density (20 DEG C), kg m-3 | 900.2 |
| Carbon residue, % | 4.2 |
| Group composition, % | |
| Stable hydrocarbon | 62.3 |
| Aromatic hydrocarbons | 22.6 |
| Colloid+bituminous matter | 15.1 |
| Sulphur 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
| Prevailing operating conditions | |
| Temperature of reaction, DEG C | 510 |
| Heavy oil feed preheating temperature, DEG C | 230 |
| Heavy oil feed finish duration of contact, s | 3.25 |
| Settling vessel top pressure (absolute pressure), MPa | 0.21 |
| Total agent-oil ratio | 6.5 |
| Recycle ratio | 0.20 |
| Revivifier dense phase temperature, DEG C | 690 |
| Revivifier coke burning degree, kg/ (t h) | 124 |
| Product slates, % | |
| Dry gas | 4.21 |
| Liquefied gas | 16.56 |
| Gasoline (IBP��180 DEG C) | 44.60 |
| Diesel oil (180��360 DEG C) | 26.35 |
| Coke | 7.90 |
| Loss | 0.38 |
| Add up to | 100 |
| Light oil yield | 70.95 |
The liquid product main character of table 3 comparative example
The prevailing operating conditions of table 4 embodiment 1��5 and product slates
The liquid product main character of table 5 embodiment 1
The liquid product main character of table 6 embodiment 2
The liquid product main character of table 7 embodiment 3
The liquid product main character of table 8 embodiment 4
The liquid product main character of table 9 embodiment 5
Claims (8)
1. a catalyst cracking method, heavy oil feed contacts with regenerated catalyst in riser tube and mixes and carry out catalytic cracking reaction, reaction logistics enters cyclonic separator from riser tube outlet through closed pipeline and carries out gas solid separation, the reaction oil gas isolated enters separation column and carries out fractionation, the reclaimable catalyst isolated carries out coke burning regeneration at stripping stage after stripping, regenerated catalyst returns riser tube and recycles, it is characterized in that: the finish duration of contact in riser tube is 0.2��1.5s, reclaimable catalyst enters baffle pipe formula revivifier after stripping, main wind co-current contact burns the generation coke going more than 90% with baffling tubular type revivifier in the lump with after the cyclic regeneration catalyst mix without cooling, semi regeneration catalyzer enters turbulent bed revivifier and turbulent bed revivifier main wind counter current contact burning removes remaining generation coke,
It is connected with baffling tubular type regenerator bottoms by reclaimable catalyst transfer lime bottom stripping stage, baffling tubular type regenerator outlet is positioned at turbulent bed revivifier dilute phase section bottom, and the close phase section of turbulent bed revivifier is connected by bottom regenerated catalyst circulation tube and regenerated catalyst and baffling tubular type regenerator bottoms and riser tube respectively;
Baffling tubular type revivifier has two kinds, the first baffling tubular type revivifier is nested with by inner and outer tubes and forms, and inner and outer tubes are all coaxially arranged with turbulent bed revivifier, interior pipe runs through whole turbulent bed revivifier, outer tube enters turbulent bed revivifier dilute phase section bottom through turbulent bed regenerator overhead end socket, circular channel is formed between interior pipe and outer tube, circular channel bottom end outlet is baffling tubular type regenerator outlet, it it is baffling tubular type regenerator bottoms bottom interior pipe, the total length of baffling tubular type revivifier is 40��70m, wherein, inner tube length p is 30��45m, outer length of tube q is 10��25m, inner tube diameter is 1200��8000mm, outer tube diameter is 1700��11300mm,
2nd kind of baffling tubular type revivifier is by ascension pipe, level pipe and down pipe series winding composition, ascension pipe and down pipe are all vertically arranged, down pipe and turbulent bed revivifier are coaxially arranged, and enter turbulent bed revivifier dilute phase section bottom through turbulent bed regenerator overhead end socket, down pipe bottom end outlet is baffling tubular type regenerator outlet, it it is baffling tubular type regenerator bottoms bottom ascension pipe, the total length of baffling tubular type revivifier is 45��80m, wherein, ascension pipe length u is 30��45m, level pipe length v is 5��10m, down pipe length w is 10��25m, ascension pipe internal diameter is 1200��8000mm, level pipe internal diameter is 900��6000mm, down pipe internal diameter is 1200��8000mm.
2. according to catalyst cracking method according to claim 1, it is characterised in that: described riser tube processes 1��5 kind of heavy oil feed simultaneously.
3. according to catalyst cracking method according to claim 1, it is characterised in that: from turbulent bed revivifier close phase section, part regenerated catalyst being introduced external warmer and cools, the regenerated catalyst after cooling all enters bottom riser tube.
4. according to catalyst cracking method according to claim 1, it is characterized in that: the operational condition of described riser tube is, the temperature of the regenerated catalyst participating in reaction is 580��700 DEG C, temperature of reaction is 460��560 DEG C, total agent-oil ratio is 5��20, oil gas average line speed is 8.0��15.0m/s, the activity of regenerated catalyst is 58��75, the operational condition of baffling tubular type revivifier is, the ratio of the cyclic regeneration catalyzer and the weight rate through steam stripped reclaimable catalyst that enter baffling tubular type revivifier is 0.5: 1��2: 1, the temperature in of baffling tubular type revivifier is 560��640 DEG C, temperature out is 630��750 DEG C, average gas line speed is 3.0��5.0m/s, coke burning degree is 300��1000kg/ (t h), char length is 30��60s, the operational condition of turbulent bed revivifier is, dense phase temperature is 620��740 DEG C, dense phase gases line speed is 0.7��1.0m/s, height of dense phase is 5��8m, dilute phase linear gas velocity is 0.4��0.6m/s, dilute phase settling height is 7��10m, coke burning degree is 50��200kg/ (t h), char length is 1.0��3.0min, top absolute pressure is 0.20��0.38MPa.
5. one kind for realizing the catalytic cracking unit of method described in claim 1, comprise riser tube, settling vessel, revivifier, riser tube outlet is connected by closed pipeline with cyclone inlet, 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: riser tube conversion zone length is 10��20m, revivifier comprises baffling tubular type revivifier and turbulent bed revivifier, it is connected with baffling tubular type regenerator bottoms by reclaimable catalyst transfer lime bottom stripping stage, baffling tubular type regenerator outlet is positioned at turbulent bed revivifier dilute phase section bottom, the close phase section of turbulent bed revivifier is connected by bottom regenerated catalyst circulation tube and regenerated catalyst and baffling tubular type regenerator bottoms and riser tube respectively,
Baffling tubular type revivifier has two kinds, the first baffling tubular type revivifier is nested with by inner and outer tubes and forms, and inner and outer tubes are all coaxially arranged with turbulent bed revivifier, interior pipe runs through whole turbulent bed revivifier, outer tube enters turbulent bed revivifier dilute phase section bottom through turbulent bed regenerator overhead end socket, circular channel is formed between interior pipe and outer tube, circular channel bottom end outlet is baffling tubular type regenerator outlet, it it is baffling tubular type regenerator bottoms bottom interior pipe, the total length of baffling tubular type revivifier is 40��70m, wherein, inner tube length p is 30��45m, outer length of tube q is 10��25m, inner tube diameter is 1200��8000mm, outer tube diameter is 1700��11300mm,
2nd kind of baffling tubular type revivifier is by ascension pipe, level pipe and down pipe series winding composition, ascension pipe and down pipe are all vertically arranged, down pipe and turbulent bed revivifier are coaxially arranged, and enter turbulent bed revivifier dilute phase section bottom through turbulent bed regenerator overhead end socket, down pipe bottom end outlet is baffling tubular type regenerator outlet, it it is baffling tubular type regenerator bottoms bottom ascension pipe, the total length of baffling tubular type revivifier is 45��80m, wherein, ascension pipe length u is 30��45m, level pipe length v is 5��10m, down pipe length w is 10��25m, ascension pipe internal diameter is 1200��8000mm, level pipe internal diameter is 900��6000mm, down pipe internal diameter is 1200��8000mm.
6. according to catalytic cracking unit according to claim 5, it is characterised in that: described riser tube arranges 2��5 layers of feed nozzle along its axially spaced-apart.
7. according to catalytic cracking unit according to claim 5, it is characterized in that: described turbulent bed revivifier is provided with external warmer, the close phase section of turbulent bed revivifier is connected with external warmer entrance by external warmer catalyst inlet pipe, and external warmer outlet is connected with bottom riser tube by low temperature catalyst transfer lime.
8. according to catalytic cracking unit according to claim 5, it is characterised in that: the total length of described riser tube is 25��30m, and wherein, pre lift zone length is 5��20m, and conversion zone internal diameter is 400��2500mm, and pre lift zone internal diameter is 200��1300mm.
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