CN101591562B - Fluid catalytic cracking method and device thereof - Google Patents
Fluid catalytic cracking method and device thereof Download PDFInfo
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- CN101591562B CN101591562B CN200910065264A CN200910065264A CN101591562B CN 101591562 B CN101591562 B CN 101591562B CN 200910065264 A CN200910065264 A CN 200910065264A CN 200910065264 A CN200910065264 A CN 200910065264A CN 101591562 B CN101591562 B CN 101591562B
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Abstract
The invention discloses a method and a device for fluid catalytic cracking. The method comprises the following steps that: a catalyst from a regenerator is heated at a mixing section, is mixed with heavy raw oil, and enters a riser reactor, a quick-speed bed reactor and a settler of a reactor I, oil gas enters a fractionating tower, and the catalyst enters the regenerator to perform regeneration;and the other part of the catalyst from the regenerator is mixed with light raw oil and enters a reactor II, reaction oil gas and a catalyst compound enter the settler, then the oil gas enters the fractionating tower and the catalyst enters the regenerator to perform regeneration, wherein the reactor I generates qualified gasoline; and the reactor II generates olefin, thus one set of device satisfies the needs of producing the gasoline and a chemical raw material.
Description
Technical field
The present invention relates under the situation that does not have hydrogen, the catalytic cracking of hydrocarbon ils, the method for clean gasoline and lower carbon number hydrocarbons is produced in a kind of especially hydrocarbon ils FCC.
Background technology
Catalytic cracking is the important secondary processing technology of oil heavy ends processing, in petroleum refining industry, occupies considerable status.Catalytically cracked gasoline is the important source of commodity motor spirit.In riser fluid catalytic cracking; Pyrolytic cracking and condensation reaction take place in oil heavy ends (comprising decompressed wax oil, wax tailings, long residuum, vacuum residuum, solvent deasphalting wet goods) under the effect of catalytic cracking catalyst, generate dry gas, liquefied gas, gasoline, diesel oil, heavy oil (comprising recycle stock and slurry oil) and coke.
Along with rapid economy development, the processed oil consumption increases day by day, and the problem of environmental pollution that motor vehicle exhaust brought also more and more receives common people's attention.Improving the processed oil quality product, alleviating environmental pollution is the task of top priority." the motor spirit objectionable impurities control criterion " of State Environmental Protection Administration's promulgation implemented on April 1st, 2003 in China; This standard-required vehicle gasoline and sulfur content in vehicle gasoline is lower than 0.08 weight %; Olefin(e) centent is not more than 35 volume %, and aromatic hydrocarbons and benzene content are lower than 40 volume % and 2.5 volume % respectively.And motor spirit will come into effect the new quality index of the gasoline that satisfies emission standard III after 31 days December in 2009; The new quality index of gasoline that satisfies emission standard III requires sulphur content to be not more than 150 μ g/g; The content of gasoline olefin is not more than 30 volume %, and aromatic hydrocarbons and benzene content are not more than 40 volume % and 1.0 volume % respectively.
Catalytic cracking process is the topmost heavy oil upgrading means of China's oil refining enterprise, and at present, China's catalytically cracked gasoline accounts for more than 75% of gasoline product total amount.CCU is not if take to reduce the measure of content of olefin in gasoline and sulphur content generally speaking, and between 40v～60v%, sulphur content is also higher relatively usually for catalytic cracking gasoline olefine content.Therefore, realize that the finished product quality of gasoline is up to standard, the quality problems of resolving catalytically cracked gasoline are particularly crucial.
According to another foreign literature prediction, the whole world will be with annual 5% speed increase to the demand of propylene from now on, and the average speed of growth of oil fuel product has only about 1.9%.According to State Economic and Trade Commission prediction, the equivalent demand of China's propylene will be respectively with 9.6% speed increment, expect 2010, the equivalent demand of propylene will reach 1,448 ten thousand tons.Above data show that it is quite urgent to the demand of industrial chemicals such as propylene to reach following domestic and international market at present.
Ethene and propylene all are important petrochemical complex basic materials, and the existing manufacturing technique method has: lighter hydrocarbons tube furnace preparing ethylene by steam cracking and propylene, its productivity of propylene are generally about 60% of ethene; Through catalytic cracking or Deep Catalytic Cracking process, can obtain a certain amount of propylene and a spot of ethene.Along with continually developing of propylene Application Areas, market is increasing to the demand of propylene, the situation that existing production of propylene can not satisfy market demands occurred.Catalytic cracking or Deep Catalytic Cracking process are to serve as that main holding concurrently produced the technology of ethene to produce propylene, and more valuable is that this technology has adaptability to raw material widely, has product modulation ability flexibly, therefore receives much concern, and has emerged in large numbers many patented technologies.
In order to satisfy the needs of producing clean gasoline; ZL02139064.9 and ZL02139065.7 have proposed to utilize double lift pipe catalytic cracking technology (FDFCC technology) to inferior gasoline upgrading and propylene enhancing, and this technology is set up a gasoline rising pipe parallelly connected with the heavy oil riser tube on conventional CCU, but in the actual industrial implementation process; Though reached the target of gasoline upgrading and propylene enhancing; But this method light oil reactor drum freshening amount is big, and the low-temperature heat of generation is more and be difficult to utilization, and benzene content is higher in the gasoline products; During producing in high-yield olefin, sacrifice oil product output.
Wang Meizheng; Liu Yingchun " heavy oil catalytically cracking equipment MIP-CGPP technological transformation " petrochemical technology and application; 2007.12; Introduced Sinopec Qingdao petrochemical corporation (complex) and adopted voluminous isoparaffin-clean gasoline propylene enhancing technology (MIP-CGPP), the 1.0Mt/a heavy oil catalytically cracking equipment has been undergone technological transformation.Through increasing by second reaction zone, adopt special-purpose CGPP catalyzer, the control cracking level is realized falling alkene and taking into account increasing production of liquid gas and the effect of propylene.But the MIP-CGP technology is owing to be to utilize the bed that reduces the temperature of reaction increase residence time to react to reduce alkene, so coking yield is higher relatively, it is less that the MIP guiding valve is regulated leeway; Diesel quality is poor; The diesel and gasoline ratio amplitude of accommodation is little; Agent-oil ratio can not flexible.Benzene content is higher in the gasoline products; During producing in high-yield olefin, sacrifice oil product output.
Patent CN19122065 has proposed a kind of catalysis conversion method of propylene enhancing, this process using double lifting leg reaction-regeneration system, and a riser tube advances heavy oil; The C4 liquefied gas that another riser tube freshening heavy oil riser tube generates, the riser tube of freshening C4 liquefied gas is established two reaction zones, and first reaction zone is liquefied gas building-up reactions district, and second reaction zone is liquefied gas catalytic cracking and dehydrating alkanes reaction zone.The process more complicated of this technology freshening C4 liquefied gas is established liquefied gas building-up reactions district and is improved the two no dependency of productivity of propylene.
Summary of the invention:
Main purpose of the present invention provides a kind of fluidized catalytic cracking method, not only can obtain clean fuel but also can obtain industrial chemicals such as ethene, propylene with same production equipment.
The present invention provides a kind of fluidized catalytic cracking method, and concrete steps are:
1) be mixed into first riser reactor, fast bed reactor drum and the settling vessel of reactor drum I from the catalyzer of revivifier through mixing section and heavy raw oil, isolating oil gas removes separation column, and catalyzer gets into revivifier and regenerates;
2) catalyzer and the lightweight material oil from revivifier is mixed into reactor drum, and reaction oil gas and catalyst mixture get into settling vessel, and isolated oil gas gets into separation column, and catalyzer turns back to revivifier and regenerates.
The present invention provides another kind of fluidized catalytic cracking method, and concrete steps are:
1) from revivifier with from 2) catalyzer through mixing section with first riser reactor that gets into reactor drum I after heavy raw oil mixes, fast bed reactor drum with get into settling vessel, isolating oil gas removes separation column, catalyzer gets into revivifier and regenerates;
2) catalyzer and the lightweight material oil from revivifier is mixed into reactor drum II; Reaction oil gas and catalyst mixture get into settling vessel; Isolated oil gas gets into separation column, and catalyst member or all turn back to revivifier and regenerate some or all ofly gets back to 1).
Described first riser reactor, fast bed reactor drum and the settling vessel that is mixed into reactor drum I from the catalyzer of revivifier at mixing section through heat-obtaining and heavy raw oil.
The said first riser reactor reaction conditions is: temperature is 450～580 ℃; Pressure is 0.03～0.30MPa, and the weight ratio of water vapor and raw oil is 0.01～1.00, is preferably 0.05～0.10; The weight ratio of catalyzer and raw oil is 2～20; Be preferably 6～15, the reaction times is 0.1～2s, is preferably 0.5～1.5s;
Said fast bed reactor reaction condition does; Temperature is 400～530 ℃, and pressure is 0.03～0.30MPa, and air speed is 0.1～3h
-1, be preferably 0.5～1.5h
-1
The reaction conditions of said reactor drum II is: temperature is 530～730 ℃, and pressure is 0.03～0.20MPa, is preferably 0.03～0.10Mpa, and water and lightweight material oil ratio are 0.01～1.00, are preferably 0.02～0.50; Reaction times is 0.5～10s, is preferably 1～5s; Catalyzer is 2～30 with lightweight material weight of oil ratio, is preferably 4～25.
Described heavy raw oil is a boiling point greater than 350 ℃ hydrocarbon, single component or its mixture of the heavy oil fraction that obtains like a kind of or its compound in decompressed wax oil, long residuum, vacuum residuum, the crude oil and through secondary processing etc.;
The lightweight material oil boiling range of said introducing reactor drum II is C
4～350 ℃ of cuts are like C
4A kind of or its compound in hydrocarbon, catalytic cracking naphtha fraction, delayed coking naphtha fraction, tube furnace steam cracking naphtha fraction, the thermal naphtha cut.
The present invention provides a kind of fluidized catalystic cracker; Form by reactor drum I, reactor drum II, settling vessel and revivifier; It is characterized in that: reactor drum I is made up of mixing section, first riser reactor and fast bed reactor drum, and the mixing section outlet links to each other with first riser reactor inlet, the outlet of first riser reactor links to each other with the fast bed reactor inlet, the fast bed reactor outlet links to each other with the settling vessel inlet.
Reactor drum II is one or more independently reactor drums, and reactor drum II is up lifting tubular type, descending tubular reactor, fluidized-bed reactor or dense, fluidized bed bioreactor.
Mixing section and fast bed reactor drum at described reactor drum I are provided with heat collector, and described heat collector is interior heat collector or external warmer.
The present invention provides another kind of fluidized catalystic cracker to be made up of reactor drum I, reactor drum II, settling vessel and revivifier; It is characterized in that: reactor drum I, reactor drum II outlet link to each other with different settling vessels respectively, and the settling vessel bottom that links to each other with reactor drum II outlet links to each other with the mixing section of revivifier with reactor drum I respectively.
The described device II bottom of answering is provided with catalyzer heat-obtaining section, and heat collector is external warmer or interior heat collector.Utilization answers device II bottom to be provided with catalyzer heat-obtaining section, the agent-oil ratio in the conditioned reaction device II, the temperature of reaction of controlling reactor II.Compared with prior art: when the heat collector that the present invention is utilized in mixing section made heavy raw oil and catalyst mix, the temperature of catalyzer was relatively low, can reduce heat cracking reaction, obtained more satisfactory product and distributed and required petrol and diesel oil product.
Through fluidized catalytic cracking method of the present invention, heavy raw oil can obtain meeting the clean gasoline of new standard through reactor drum I processing, and just the alkene of gasoline less than volume 1%, and can obtain 6%～10% propylene less than 30 volume %, benzene content; Raw material through reactor drum II processing can maximum be produced ethene, propylene, and ethylene yield can reach 6～15%, and productivity of propylene is to reach 15～35%.
Outstanding advantage of the present invention: the agent-oil ratio of first riser reactor of reactor drum I can regulated in a big way; But the bed temperature independent regulation of the fast bed reactor drum of reactor drum I, handiness is big.Quality of gasoline can meet the clean gasoline standard of new standard, diesel quality and conventional catalyst cracking technology diesel oil character basically identical; When employing another advantage of the present invention is the gasoline yield that can obtain maximum, can produce more ethene, propylene, ethylene yield can reach 6～15 weight %, and productivity of propylene is to reach 8～35 weight %, in raw material.
Because the temperature of catalyzer is relatively low; When raw material and catalyst mix, can take bigger agent-oil ratio, there is more catalyst active center to offer the raw material that need react; Can improve raw material generation catalytic cracking reaction efficient; Can reduce the productive rate of non-title product, improve the productive rate of title product, realize maximizing the benefits.
Description of drawings
Fig. 1 is a kind of fluidized catalystic cracker figure of the present invention.
Fig. 2 is the another kind of fluidized catalystic cracker figure of the present invention.
1, mixing tank, 2, fluidized-bed reactor, 3, first riser reactor, 4 second riser reactors; 5, first settling vessel, 6-revivifier, 7-regenerator sloped tube, 8-regenerator sloped tube; 9-lightweight material oil, 10-heavy raw oil, 11-second settling vessel, 12-pipe to be generated; The 13-catalyst line, 14, the 15-heat collector
Embodiment
Further specify the present invention below in conjunction with accompanying drawing, but do not limit the present invention.
As shown in Figure 1:
The method flow synoptic diagram of reactor drum I provided by the invention and the shared settling vessel of reactor drum II.
Enter into the catalyst mix section 1 of reactor drum I bottom through catalyst regeneration inclined tube 7 from the high temperature catalyst of revivifier 6; High temperature catalyst this be arranged on heat-obtaining medium in the heat collector 15 of catalyst mix section 1 and carry out heat exchange and regulate the cooling of catalyzer and reach first riser reactor, 3 desired reaction temperatures; Contact entering first riser reactor 3 with heavy raw oil and catalytic cracking reaction takes place; The mixture flow of coming out from first riser reactor 3 enters into fast bed reactor drum 2; Heat-obtaining medium in this and heat collector 14 carries out heat exchange, reaches the temperature of fast bed reactor drum 2 demands through control heat-obtaining amount control mixture flow temperature, and reactions such as hydrogen transfer reactions, isomerizing further take place mixture flow; Get into second riser reactor 4 from the mixture flow of fast bed reactor drum 2 dischargings; React, get into settling vessel 5, separate with the catalyzer of carbon deposit in settling vessel 5 reaction product from second riser reactor, 4 mixture flow; Carbon deposited catalyst gets into revivifier 6 behind stripping carries out coke burning regeneration and recycles, and reaction product goes separation system to separate;
The bottom that enters into reactor drum II from the high temperature catalyst of revivifier 6 through catalyst regeneration inclined tube 8 mixes with lightweight material oil 9 closely to go into reactor drum II catalytic cracking reaction takes place; The reaction oil gas and the catalyzer that come out from reactor drum II get into settling vessel 5; Separate with the catalyzer of carbon deposit in settling vessel 5 reaction product; Carbon deposited catalyst gets into revivifier 6 behind stripping carries out coke burning regeneration and recycles, and reaction product goes separation system to separate.
As shown in Figure 2, reactor drum I provided by the invention and reactor drum II use the method flow synoptic diagram of settling vessel separately respectively.
Enter into the catalyst mix section 1 of reactor drum I bottom through catalyst regeneration inclined tube 7 from the high temperature catalyst of revivifier 6; High temperature catalyst this be arranged on heat-obtaining medium in the heat collector 15 of catalyst mix section 1 and carry out heat exchange and regulate the cooling of catalyzer and reach first riser reactor, 3 desired reaction temperatures; Contact entering first riser reactor 3 with heavy raw oil and catalytic cracking reaction takes place; The mixture flow of coming out from first riser reactor 3 enters into fast bed reactor drum 2; Heat-obtaining medium in this and heat collector 14 carries out heat exchange, reaches the temperature of fast bed reactor drum 2 demands through control heat-obtaining amount control mixture flow temperature, and reactions such as hydrogen transfer reactions, isomerizing further take place mixture flow; Get into second riser reactor 4 from the mixture flow of fast bed reactor drum 2 dischargings; React, get into settling vessel 5, separate with the catalyzer of carbon deposit in settling vessel 5 reaction product from second riser reactor, 4 mixture flow; Carbon deposited catalyst gets into revivifier 6 behind stripping carries out coke burning regeneration and recycles, and reaction product goes separation system to separate;
The bottom that enters into reactor drum II from the high temperature catalyst of revivifier 6 through catalyst regeneration inclined tube 8 mixes with lightweight material oil 9 closely to go into reactor drum II catalytic cracking reaction takes place; The reaction oil gas and the catalyzer that come out from reactor drum II get into settling vessel 11; Separate with the catalyzer of carbon deposit in settling vessel 11 reaction product; The deposit carbon catalyzer perhaps all enters into the catalyst mix section 1 of reactor drum I through catalyst line 13 through the stripping rear section; Part gets into revivifiers 6 through pipe to be generated 12 carries out coke burning regeneration and recycles, and reaction product goes separation system to separate.
Further specify the present invention through embodiment below, do not limit the present invention.
Embodiment 1
The main character of used heavy raw oil A is listed in table 1, and lightweight material is the liquefied gas that heavy raw oil A cracking generates.The operating method that experiment adopts one way to pass through, experiment is carried out at the device of Fig. 1, and catalyzer is RSC-2006.Heavy raw oil A carries out in reactor drum I, and the temperature of reaction of first riser reactor among the reactor drum I is 510 ℃, and reaction pressure is 0.12Mpa (gauge pressure), and WOR is 0.05, and the reaction times is 1s, and agent-oil ratio is 10; The temperature of reaction of fast bed conversion zone is 500 ℃, and reaction pressure is 0.12MPa (gauge pressure), and reaction velocity is 1.2h
-1The lightweight material carbon 4 liquid gas reacts at lightweight material reactor drum II, and the temperature of reaction of reactor drum II is 600 ℃, and reaction pressure is 0.12Mpa (gauge pressure), and WOR is 0.01, and the reaction times is 3s, and agent-oil ratio is 18.Experimental result is listed in table 2, and the gasoline main character is listed in table 3.Can find out that by table 2, table 3 propylene and gasoline yield be higher by 0.57% than Comparative Examples respectively, 2.1%, and quality of gasoline reaches the quality standard of clean gasoline.Comparative Examples 1
The main difference of Comparative Examples and embodiment 1 is, the heavy feed stock reactor drum is one not with the riser reactor of any additional structure.Catalyzer is RSC-2006, and the temperature of reaction of heavy feed stock reactor drum is 500 ℃, and the temperature of reaction of lightweight material reactor drum is 600 ℃.Experimental result is listed in table 2, and the gasoline main character is listed in table 3.
Test used heavy feed stock A, lightweight material is that the main character of straight-run spirit is listed in table 1.The operating method that experiment adopts one way to pass through, experiment is carried out at the experimental installation of similar Fig. 2, and catalyzer is the producing in high-yield olefin catalyzer of the special company of Engelhardt.Heavy raw oil A carries out in the heavy feed stock oil reactor; The temperature of reaction of the riser tube conversion zone in the heavy feed stock oil reactor is 515 ℃; The temperature of reaction of fast bed conversion zone is 505 ℃, and straight-run spirit carries out at the lightweight material reactor drum, and the temperature of reaction of lightweight material reactor drum is 610 ℃.Experimental result is listed in table 3, and the gasoline main character is listed in table 4.Can find out that by table 3, table 4 propylene and gasoline yield be higher by 2.87% than Comparative Examples respectively, 4.89%, and quality of gasoline reaches the quality standard of clean gasoline.
Comparative Examples 2
The main difference of Comparative Examples and embodiment 2 is, the heavy feed stock oil reactor is one not with the riser reactor of any additional structure.Catalyzer is identical with embodiment 2, and the temperature of reaction of heavy feed stock oil reactor is 505 ℃, and the temperature of reaction of lightweight material reactor drum is 610 ℃.Experimental result is listed in table 3, and the gasoline main character is listed in table 4.
Table 1 feedstock property
| Raw material A | Straight-run spirit | |
| Density, 20 ℃, g/cm3 | 0.91 | 0.71 |
| Sulphur content, μ g/g | 2000 | 400 |
| Nickel, μ g/g | 6.98 | / |
| Vanadium, μ g/g | 2.40 | / |
| Carbon residue, % | 5.21 | / |
| Octane value | / | 60 |
Table 2 material balance
| Embodiment 1 | Comparative Examples 1 | |
| Product distribution/m% | ||
| Dry gas | 5.29 | 6.2 |
| Liquefied gas | 23.14 | 23.0 |
| Propylene wherein | 8.37 | 7.70 |
| Gasoline fraction | 39.52 | 37.4 |
| Diesel oil distillate | 20.15 | 21.5 |
| Slurry oil | 3.53 | 4.0 |
| Coke+loss | 7.87 | 7.9 |
| Add up to | 100 | 100 |
Table 3 gasoline main character
Table 4 material balance
| |
Comparative Examples 2 | |
| Product distribution/m% | ||
| Dry gas | 6.05 | 7.4 |
| Liquefied gas | 19.06 | 21.0 |
| Propylene wherein | 11.47 | 8.6 |
| Gasoline fraction | 40.79 | 35.9 |
| Diesel oil distillate | 21.67 | 22.5 |
| Slurry oil | 3.0 | 3.0 |
| Coke+loss | 9.43 | 9.6 |
| Add up to | 100 | 100 |
Table 5 gasoline main character
Claims (28)
1. fluidized catalytic cracking method is characterized in that:
1) behind heat-obtaining, be mixed into first riser reactor, fast bed reactor drum and the settling vessel of reactor drum I from the catalyzer of revivifier with heavy raw oil at mixing section, isolating oil gas removes separation column, and catalyzer gets into revivifier and regenerates;
2) catalyzer and the lightweight material oil from revivifier is mixed into reactor drum II, and reaction oil gas and catalyst compound get into settling vessel, and isolated oil gas gets into separation column, and catalyzer turns back to revivifier and regenerates.
2. according to a kind of fluidized catalytic cracking method shown in the claim 1; It is characterized in that: the first riser reactor reaction conditions is: temperature is 450～580 ℃; Pressure is 0.03～0.30MPa; The weight ratio of water vapor and raw oil is 0.01～1.00, and the weight ratio of catalyzer and raw oil is 2～20, and the reaction times is 0.1～2s.
3. according to a kind of fluidized catalytic cracking method shown in the claim 1; It is characterized in that: the first riser reactor reaction conditions is: the weight ratio of water vapor and raw oil is 0.05～0.10; The weight ratio of catalyzer and heavy raw oil is 6～15, and the reaction times is 0.5～1.5s.
4. according to a kind of fluidized catalytic cracking method shown in the claim 1, it is characterized in that: fast bed reactor reaction condition does; Temperature is 400～530 ℃, and pressure is 0.03～0.30MPa, and air speed is 0.1～3h
-1
5. according to a kind of fluidized catalytic cracking method shown in the claim 1, it is characterized in that: fast bed reactor reaction condition air speed is 0.5～1.5h
-1
6. according to a kind of fluidized catalytic cracking method shown in the claim 1; It is characterized in that: the reaction conditions of reactor drum II is: temperature is 530～730 ℃; Pressure is 0.03～0.20MPa; Water is 0.01～1.00 with lightweight material weight of oil ratio, and the reaction times is 0.5～10s, and catalyzer is 2～30 with lightweight material weight of oil ratio.
7. according to a kind of fluidized catalytic cracking method shown in the claim 1, it is characterized in that: the pressure of reactor drum II is 0.03～0.10MPa, and water is 0.02～0.50 with lightweight material weight of oil ratio; Reaction times is 1～5s, and catalyzer and lightweight material weight of oil are 4～25.
8. according to a kind of fluidized catalytic cracking method shown in the claim 1, it is characterized in that: heavy raw oil is a boiling point greater than 350 ℃ hydrocarbon.
9. according to a kind of fluidized catalytic cracking method shown in the claim 1, it is characterized in that: heavy raw oil is at least a in the heavy oil fraction that obtains of decompressed wax oil, long residuum, vacuum residuum, crude oil and secondary processing.
10. according to a kind of fluidized catalytic cracking method shown in the claim 1, it is characterized in that: lightweight material oil is C
4At least a in hydrocarbon, catalytic cracking naphtha fraction, delayed coking naphtha fraction, tube furnace steam cracking naphtha fraction, the thermal naphtha cut.
11. a fluidized catalytic cracking method is characterized in that:
1) from revivifier with from 2) catalyzer behind heat-obtaining, be mixed into first riser reactor, fast bed reactor drum and the settling vessel of reactor drum I at mixing section with heavy raw oil, isolating oil gas removes separation column, catalyzer gets into revivifier and regenerates;
2) catalyzer and the lightweight material oil from revivifier is mixed into reactor drum II, and reaction oil gas and catalyst compound get into settling vessel, and isolated oil gas gets into separation column, and catalyst member perhaps all turns back to revivifier and regenerates, and part gets back to 1).
12. according to a kind of fluidized catalytic cracking method shown in the claim 11; It is characterized in that: the first riser reactor reaction conditions is: temperature is 450～580 ℃; Pressure is 0.03～0.30MPa; The weight ratio of water vapor and raw oil is 0.01～1.00, and the weight ratio of catalyzer and raw oil is 2～20, and the reaction times is 0.1～2s.
13. according to a kind of fluidized catalytic cracking method shown in the claim 11; It is characterized in that: the first riser reactor reaction conditions is: the weight ratio of water vapor and raw oil is 0.05～0.10; The weight ratio of catalyzer and heavy raw oil is 6～15, and the reaction times is 0.5～1.5s.
14. according to a kind of fluidized catalytic cracking method shown in the claim 11, it is characterized in that: fast bed reactor reaction condition does; Temperature is 400～530 ℃, and pressure is 0.03～0.30MPa, and air speed is 0.1～3h
-1
15. according to a kind of fluidized catalytic cracking method shown in the claim 11, it is characterized in that: fast bed reactor reaction condition air speed is 0.5～1.5h
-1
16. according to a kind of fluidized catalytic cracking method shown in the claim 11; It is characterized in that: the reaction conditions of reactor drum II is: temperature is 530～730 ℃; Pressure is 0.03～0.20MPa; Water is 0.01～1.00 with lightweight material weight of oil ratio, and the reaction times is 0.5～10s, and catalyzer is 2～30 with lightweight material weight of oil ratio.
17. according to a kind of fluidized catalytic cracking method shown in the claim 11, it is characterized in that: the pressure of reactor drum II is 0.03～0.10MPa, water is 0.02～0.50 with lightweight material weight of oil ratio; Reaction times is 1～5s, and catalyzer and lightweight material weight of oil are 4～25.
18. a kind of fluidized catalytic cracking method according to shown in the claim 11 is characterized in that: heavy raw oil is a boiling point greater than 350 ℃ hydro carbons.
19. a kind of fluidized catalytic cracking method according to shown in the claim 11 is characterized in that: heavy raw oil is at least a in the heavy oil fraction that obtains of decompressed wax oil, long residuum, vacuum residuum, crude oil and secondary processing.
20. a kind of fluidized catalytic cracking method according to shown in the claim 11 is characterized in that: lightweight material oil is C
4At least a in hydrocarbon, catalytic cracking naphtha fraction, delayed coking naphtha fraction, tube furnace steam cracking naphtha fraction, the thermal naphtha cut.
21. fluidized catalystic cracker; Form by reactor drum I, reactor drum II, settling vessel and revivifier; It is characterized in that: reactor drum I is made up of mixing section, first riser reactor, fast bed reactor drum; The mixing section outlet links to each other with first riser reactor inlet, the outlet of first riser reactor links to each other with the fast bed reactor inlet, the fast bed reactor outlet links to each other with the settling vessel inlet, and reactor drum II bottom is provided with catalyzer heat-obtaining section.
22. according to a kind of fluidized catalystic cracker shown in the claim 21, it is characterized in that: mixing section and fast bed reactor drum are provided with interior heat collector.
23. according to a kind of fluidized catalystic cracker shown in the claim 21, it is characterized in that: mixing section and fast bed reactor drum are provided with external warmer.
24. according to a kind of fluidized catalystic cracker shown in the claim 21, it is characterized in that: reactor drum II is up lifting tubular reactor or fluidized-bed reactor.
25. fluidized catalystic cracker; Form by reactor drum I, reactor drum II, settling vessel and revivifier; It is characterized in that: reactor drum I, reactor drum II outlet link to each other with different settling vessels respectively, and the settling vessel bottom that links to each other with reactor drum II outlet links to each other with the mixing section of revivifier with reactor drum I respectively.
26. according to a kind of fluidized catalystic cracker shown in the claim 25, it is characterized in that: mixing section and fast bed reactor drum are provided with interior heat collector.
27. according to a kind of fluidized catalystic cracker shown in the claim 25, it is characterized in that: mixing section and fast bed reactor drum are provided with external warmer.
28. a kind of fluidized catalystic cracker according to shown in the claim 25 is characterized in that: up lifting tubular reactor of reactor drum II or fluidized-bed reactor.
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| CN102102029B (en) * | 2009-12-17 | 2014-01-22 | 中国石油大学(北京) | Catalytic cracking fractional and divisional transformation method and device for heavy oil |
| CN102102028B (en) * | 2009-12-17 | 2014-01-22 | 中国石油大学(北京) | Fractional and divisional catalytic cracking method and device for heavy oil |
| CN102102030B (en) * | 2009-12-17 | 2014-01-22 | 中国石油大学(北京) | Heavy oil catalytic cracking method and device by double-area coupling and catalyst tandem |
| CN102191080B (en) * | 2010-03-11 | 2014-04-30 | 中国石油化工股份有限公司 | Method for lowering sulfur and olefin content in gasoline |
| CN102234531B (en) * | 2010-05-06 | 2014-02-05 | 中国石油天然气股份有限公司 | Heavy oil zone catalytic cracking device and application |
| CN102286291B (en) * | 2010-06-18 | 2014-04-30 | 中国石油化工股份有限公司 | Catalytic conversion method of shale oil |
| CN102827635B (en) * | 2011-06-15 | 2014-04-02 | 石宝珍 | Catalytic cracking method and device thereof |
| CN103571530B (en) * | 2012-08-02 | 2015-11-18 | 中国石油天然气股份有限公司 | Method for preparing low-carbon olefin by catalytic cracking of wax oil |
| CN106440870B (en) * | 2016-09-20 | 2019-01-22 | 洛阳明远石化技术有限公司 | External warmer |
| CN108794292B (en) * | 2017-07-21 | 2020-03-17 | 青岛京润石化设计研究院有限公司 | Catalytic conversion method for producing more propylene |
| JP2020531603A (en) | 2017-08-28 | 2020-11-05 | サウジ アラビアン オイル カンパニーＳａｕｄｉ Ａｒａｂｉａｎ Ｏｉｌ Ｃｏｍｐａｎｙ | Chemical loop process for catalytic hydrocarbon decomposition |
| CN110540861B (en) * | 2018-05-28 | 2021-11-16 | 中国石油化工股份有限公司 | Catalytic cracking process and system |
| CN110724553B (en) * | 2018-07-16 | 2021-04-06 | 中国石油化工股份有限公司 | Method and system for catalytic cracking by adopting dilute phase conveying bed and rapid fluidized bed |
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