CN101993708A - Catalytic cracking method and device - Google Patents
Catalytic cracking method and device Download PDFInfo
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- CN101993708A CN101993708A CN2009100657192A CN200910065719A CN101993708A CN 101993708 A CN101993708 A CN 101993708A CN 2009100657192 A CN2009100657192 A CN 2009100657192A CN 200910065719 A CN200910065719 A CN 200910065719A CN 101993708 A CN101993708 A CN 101993708A
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Abstract
The invention discloses a catalytic cracking method and a catalytic cracking device. The method comprises the following steps of: heating a catalyst from a regenerator at a mixing section; mixing the catalyst and heavy raw oil and adding the mixture into a riser reactor of a reactor I, a constant-velocity bed reactor and a settling vessel; introducing oil gases into a fractionating tower and adding the catalyst into the regenerator for regeneration; mixing the other part of catalyst from the regenerator and light raw oil and then adding the mixture into a reactor II; and introducing reaction oil gases and adding a catalyst compound into the settling vessel, introducing the oil gases into the fractionating tower, and adding the catalyst into the regenerator for regeneration, wherein the reactor I produces qualified gasoline and the reactor II produces olefins, so the requirements of producing gasoline and chemical raw materials can be met by one set of device.
Description
Technical field
The present invention relates under the situation that does not have hydrogen the catalytic cracking of hydrocarbon ils, a kind of especially catalytic cracking and device thereof.
Background technology
Catalytic cracking is the important secondary processing technology of oil heavy ends processing, occupies considerable status in petroleum refining industry.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 is subjected to 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 in China on April 1st, 2003, 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.Catalytic cracking unit 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; By 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, this technology is set up a gasoline rising pipe in parallel with the heavy oil riser tube on conventional catalytic cracking unit, but in the actual industrial implementation process, though reached the target of gasoline upgrading and propylene enhancing, but this method light oil reactor freshening amount is big, produce low warm more and be difficult to utilization, 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-CGP technological transformation " petrochemical technology and application, 2007.12, introduced Sinopec Qingdao petrochemical corporation (complex) and adopted voluminous isoparaffin-clean gasoline propylene enhancing technology (MIP-CGP), the 1.0Mt/a heavy oil catalytically cracking equipment has been undergone technological transformation.By increasing by second reaction zone, adopt special-purpose CGP 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, and this process using double lifting leg reacts a 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 catalyst cracking method, not only can obtain clean fuel but also can obtain industrial chemicals such as ethene, propylene with same production equipment.
The invention provides a kind of catalyst cracking method, concrete steps are:
1) be mixed into riser reactor, constant speed bed bioreactor and the settling vessel of reactor I from the catalyzer of revivifier at mixing section and heavy raw oil, reacted oil gas removes separation column, and catalyzer enters revivifier and regenerates;
2) catalyzer and the lightweight material oil from revivifier is mixed into reactor II, and reaction oil gas and catalyst mixture enter settling vessel, and reacted oil gas enters separation column, and catalyzer enters revivifier and regenerates.
The invention provides another kind of fluidized catalytic cracking method, concrete steps are:
1) from revivifier with from 2) catalyzer mixing section through behind the heat-obtaining with the riser reactor, constant speed bed bioreactor and the settling vessel that enter reactor I after heavy raw oil mixes, reacted oil gas removes separation column, catalyzer enters revivifier and regenerates;
2) catalyzer and the lightweight material oil from revivifier is mixed into reactor II, and reaction oil gas and catalyst mixture enter settling vessel, and oil gas enters fractionation, and catalyst member or all turn back to revivifier and regenerate some or all ofly gets back to 1).
Described is riser reactor, constant speed bed bioreactor and the settling vessel that is mixed into reactor I from the catalyzer of revivifier at mixing section behind heat-obtaining with heavy raw oil
Described riser reactor reaction conditions is: temperature is 450～580 ℃, pressure is 0.03～0.30MPa, the weight ratio of water vapor and stock oil is 0.01～1.00, be preferably 0.05～0.10, the weight ratio of catalyzer and stock oil is 2～20, be preferably 6～15, the reaction times is 0.1～2s, is preferably 0.5～1.5s;
Described constant speed bed bioreactor is inverted frustum, and reaction conditions is; 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 described reactor 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 ℃ hydro carbons, single component or its mixture of the heavy oil fraction that obtains as a kind of or its compound in decompressed wax oil, long residuum, vacuum residuum, the crude oil and by secondary processing etc.;
The lightweight material oil boiling range of described introducing reactor II is C
4～350 ℃ of cuts are as C
4A kind of or its compound in hydrocarbon, virgin naphtha cut, catalytic cracking naphtha fraction, delayed coking naphtha fraction, tube furnace steam cracking naphtha fraction, the thermal naphtha cut.
By fluidized catalytic cracking method of the present invention, heavy raw oil can obtain meeting the clean gasoline of new standard through reactor 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 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 the riser reactor of reactor I can regulated in a big way; The beds radial distribution of the constant speed bed bioreactor of reactor I is even, has improved oil gas contact effect, has improved the oil gas transformation efficiency.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.
The invention provides a kind of fluidized catalytic cracker, form by reactor I, reactor II, settling vessel and revivifier, it is characterized in that: reactor I is made up of mixing section, riser reactor and constant speed bed bioreactor, and the mixing section outlet links to each other with the riser reactor inlet, the riser reactor outlet links to each other with constant speed bed bioreactor inlet, the outlet of constant speed bed bioreactor links to each other with the settling vessel inlet.
Reactor II is one or more independently reactors, and reactor II is up lifting tubular type, descending tubular reactor, dense fluidized bed bioreactor or dense fluidized bed bioreactor.
Mixing section and constant speed bed bioreactor at described reactor I are provided with heat collector, and described heat collector is interior heat collector or external warmer.
The invention provides another kind of fluidized catalytic cracker is made up of reactor I, reactor II, settling vessel and revivifier, it is characterized in that: reactor I, reactor II outlet links to each other with different settling vessels respectively, and the settling vessel bottom that links to each other with reactor II outlet links to each other with the mixing section of revivifier with reactor 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 utilization of the present invention made heavy raw oil and catalyst mix at the heat collector of mixing section, 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.
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-target product, improve the productive rate of target product, realize maximizing the benefits.
Description of drawings
Fig. 1 is a kind of fluidized catalytic cracker figure of the present invention.
Fig. 2 is the another kind of fluidized catalytic cracker figure of the present invention.
1, mixing tank, 2, the constant speed bed bioreactor, 3, riser reactor, 4 second riser reactors, 5, first settling vessel, 6-revivifier, the 7-regenerator sloped tube, 8-regenerator sloped tube, 9-lightweight material oil, the 10-heavy raw oil, 11-second settling vessel, 12-pipe to be generated, 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 I provided by the invention and the shared settling vessel of reactor II.
Enter into the catalyst mix section 1 of reactor 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 riser reactor 3 desired reaction temperatures, contact with heavy raw oil 10 and to enter riser reactor 3 and catalytic cracking reaction takes place, the mixture flow of coming out from riser reactor 3 enters into constant speed bed bioreactor 2, heat-obtaining medium in this and heat collector 14 carries out heat exchange, reach the temperature of constant speed bed bioreactor 2 demands by control heat-obtaining amount control mixture flow temperature, catalytic cracking further takes place in mixture flow, reactions such as hydrogen transference, reactions such as isomerization, the mixture flow of coming out from constant speed bed bioreactor 2 enters settling vessel 5 by conduit 4, separate with the catalyzer of carbon deposit in settling vessel 5 reaction product, carbon deposited catalyst enters 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 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 II catalytic cracking reaction takes place, the reaction oil gas and the catalyzer that come out from reactor II enter settling vessel 5, separate with the catalyzer of carbon deposit in settling vessel 5 reaction product, carbon deposited catalyst enters 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 I provided by the invention and reactor II use the method flow synoptic diagram of settling vessel separately respectively.
Enter into the catalyst mix section 1 of reactor 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 riser reactor 3 desired reaction temperatures, contact with heavy raw oil and to enter riser reactor 3 and catalytic cracking reaction takes place, the mixture flow of coming out from riser reactor 3 enters into constant speed bed bioreactor 2, heat-obtaining medium in this and heat collector 14 carries out heat exchange, reach the temperature of constant speed bed bioreactor 2 demands by control heat-obtaining amount control mixture flow temperature, hydrogen transfer reactions further takes place in mixture flow, reactions such as isomerization, enter settling vessel 5 from the mixture flow of constant speed bed bioreactor 2 dischargings by pipeline 4, separate with the catalyzer of carbon deposit in settling vessel 5 reaction product, carbon deposited catalyst enters 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 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 II catalytic cracking reaction takes place, the reaction oil gas and the catalyzer that come out from reactor II enter settling vessel 11, separate with the catalyzer of carbon deposit in settling vessel 11 reaction product, the deposit carbon catalyzer is through the stripping rear section or all enter into the catalyst mix section 1 of reactor I through catalyst line 13, part enters revivifier 6 through pipe 12 to be generated carries out coke burning regeneration and recycles, and reaction product goes separation system to separate.
Further specify the present invention below by embodiment, do not limit the present invention.
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 I, and the temperature of reaction of the riser reactor among the reactor I is 515 ℃, and reaction pressure is 0.11Mpa (gauge pressure), and water-oil ratio is 0.05, and the reaction times is 1.1s, and agent-oil ratio is 9.5; The temperature of reaction of constant speed bed conversion zone is 500 ℃, and reaction pressure is 0.11MPa (gauge pressure), and reaction velocity is 1.5h
-1The lightweight material carbon 4 liquid gas reacts at lightweight material reactor II, and the temperature of reaction of reactor II is 610 ℃, and reaction pressure is 0.11Mpa (gauge pressure), and water-oil ratio is 0.02, and the reaction times is 3.2s, and agent-oil ratio is 20.Experimental result is listed in table 2, and the gasoline main character is listed in table 3.By table 2, table 3 as can be seen, propylene and gasoline yield be higher by 3.2% than Comparative Examples respectively, 3.55%, 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 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 is 500 ℃, and the temperature of reaction of lightweight material reactor is 610 ℃.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 520 ℃, the temperature of reaction of constant speed bed conversion zone is 505 ℃, and straight-run spirit carries out at the lightweight material reactor, and the temperature of reaction of lightweight material reactor is 620 ℃.Experimental result is listed in table 3, and the gasoline main character is listed in table 4.By table 3, table 4 as can be seen, propylene and gasoline yield be higher by 4.0% than Comparative Examples respectively, 1.5%, 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 is 620 ℃.Experimental result is listed in table 3, and the gasoline main character is listed in table 4.
Table 1 feedstock property
| Project | Raw material A | Straight-run spirit |
| Density (20 ℃)/g.cm -3 | 0.92 | 0.71 |
| Sulphur content/μ g.g -1 | 2400 | 350 |
| Nickel, μ g/g | 6.5 | / |
| Vanadium, μ g/g | 1.8 | / |
| Carbon residue, weight % | 4.1 | / |
| Octane value | / | 62 |
Table 2 material balance
| | Embodiment | 1 | Comparative Examples 1 |
| Product distributes, weight % | ||
| Dry gas | 4.0 | 5.9 |
| Liquefied gas | 27.10 | 22.0 |
| Propylene wherein | 10.9 | 7.70 |
| Gasoline fraction | 42.15 | 38.6 |
| Diesel oil distillate | 16.75 | 21.5 |
| Slurry oil | 2.50 | 4.0 |
| Coke+loss | 7.5 | 8.0 |
| Add up to | 100 | 100 |
Table 3 gasoline main character
Table 4 material balance
| | Embodiment | 2 | Comparative Examples 2 |
| Product distributes, weight % |
| Dry gas | 5.0 | 5.5 |
| Liquefied gas | 28.8 | 22.0 |
| Propylene wherein | 12.5 | 8.5 |
| Gasoline fraction | 38.40 | 36.5 |
| Diesel oil distillate | 17.50 | 23.4 |
| Slurry oil | 2.5 | 3.0 |
| Coke+loss | 7.8 | 9.6 |
| Add up to | 100 | 100 |
Table 5 gasoline main character
Claims (19)
1. catalyst cracking method is characterized in that:
1) from revivifier with from 2) catalyzer be mixed into riser reactor, constant speed bed bioreactor and the settling vessel of reactor I at mixing section heavy raw oil behind heat-obtaining, oil gas removes separation column, catalyzer enters revivifier and regenerates;
2) catalyzer and the lightweight material oil from revivifier is mixed into reactor II, and reaction oil gas and catalyst compound enter settling vessel, and oil gas enters separation column, catalyst member or all enter revivifier and regenerate, part gets back to 1).
2. according to a kind of catalyst cracking method shown in the claim 1, it is characterized in that: the riser reactor, constant speed bed bioreactor and the settling vessel that are mixed into reactor I from the catalyzer of revivifier at mixing section through heat-obtaining from the catalyzer of revivifier at mixing section and heavy raw oil
3. according to a kind of catalyst cracking method shown in the claim 1, it is characterized in that: the riser reactor reaction conditions is: temperature is 450～580 ℃, pressure is 0.03～0.30MPa, the weight ratio of water vapor and stock oil is 0.01～1.00, the weight ratio of catalyzer and stock oil is 2～20, and the reaction times is 0.1～2s.
4. according to a kind of catalyst cracking method shown in the claim 1, it is characterized in that: the riser reactor reaction conditions is: the weight ratio of water vapor and stock 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.
5. according to a kind of catalyst cracking method shown in the claim 1, it is characterized in that: constant speed bed bioreactor reaction conditions is; Temperature is 400～530 ℃, and pressure is 0.03～0.30MPa, and air speed is 0.1～3h
-1
6. according to a kind of catalyst cracking method shown in the claim 1, it is characterized in that: constant speed bed bioreactor reaction conditions air speed is 0.5～1.5h
-1
7. according to a kind of catalyst cracking method shown in the claim 1, it is characterized in that: the reaction conditions of reactor 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, reaction times is 0.5～10s, and catalyzer is 2～30 with lightweight material weight of oil ratio.
8. according to a kind of catalyst cracking method shown in the claim 1, it is characterized in that: the pressure of reactor 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.
9. according to a kind of catalyst cracking method shown in the claim 1, it is characterized in that: heavy raw oil is a boiling point greater than 350 ℃ hydro carbons.
10. according to a kind of catalyst 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.
11. a kind of catalyst cracking method according to shown in the claim 1 is characterized in that: lightweight material oil is that boiling range is C
4～350 ℃ of cuts.
12. a kind of catalyst cracking method according to shown in the claim 1 is characterized in that: lightweight material oil is C
4At least a in hydrocarbon, virgin naphtha cut, catalytic cracking naphtha fraction, delayed coking naphtha fraction, tube furnace steam cracking naphtha fraction, the thermal naphtha cut.
13. catalytic cracking unit, it is characterized in that: device is made up of reactor I, reactor II, settling vessel and revivifier, it is characterized in that: reactor I, reactor II outlet links to each other with different settling vessels respectively, and the settling vessel bottom that links to each other with reactor II outlet links to each other with the mixing section of revivifier with reactor I respectively.
14. a kind of catalytic cracking unit according to shown in the claim 13 is characterized in that: mixing section and constant speed bed bioreactor are provided with interior heat collector.
15. a kind of catalytic cracking unit according to shown in the claim 13 is characterized in that: mixing section and constant speed bed bioreactor are provided with external warmer.
16. a kind of catalytic cracking unit according to shown in the claim 13 is characterized in that: reactor II bottom is provided with external warmer.
17. a kind of catalytic cracking unit according to shown in the claim 13 is characterized in that: reactor II bottom is provided with interior heat collector.
18. a kind of catalytic cracking unit according to shown in the claim 13 is characterized in that: reactor II is one or more independently reactors.
19. a kind of catalytic cracking unit according to shown in the claim 13 is characterized in that: up lifting tubular reactor of reactor II or descending tubular reactor or dense fluidized bed bioreactor or dense fluidized bed bioreactor.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114149821A (en) * | 2021-12-20 | 2022-03-08 | 中国石油化工股份有限公司 | Method and device for producing more low-carbon olefins |
| CN115873623A (en) * | 2021-09-28 | 2023-03-31 | 中国石油化工股份有限公司 | Reaction system and method for producing low-carbon olefin and aromatic hydrocarbon by catalytic cracking |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1948440A (en) * | 2005-10-12 | 2007-04-18 | 洛阳石化设备研究所 | Catalytic conversion method of double reactor and its device |
| CN101104815A (en) * | 2007-07-13 | 2008-01-16 | 中国石油化工集团公司 | Upgrading method and device for gasoline |
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2009
- 2009-08-11 CN CN2009100657192A patent/CN101993708A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1948440A (en) * | 2005-10-12 | 2007-04-18 | 洛阳石化设备研究所 | Catalytic conversion method of double reactor and its device |
| CN101104815A (en) * | 2007-07-13 | 2008-01-16 | 中国石油化工集团公司 | Upgrading method and device for gasoline |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115873623A (en) * | 2021-09-28 | 2023-03-31 | 中国石油化工股份有限公司 | Reaction system and method for producing low-carbon olefin and aromatic hydrocarbon by catalytic cracking |
| CN114149821A (en) * | 2021-12-20 | 2022-03-08 | 中国石油化工股份有限公司 | Method and device for producing more low-carbon olefins |
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