CN103571530B - Wax catalysis cracking is for the method for low-carbon alkene - Google Patents
Wax catalysis cracking is for the method for low-carbon alkene Download PDFInfo
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Abstract
The present invention relates to the method for a kind of wax catalysis cracking for low-carbon alkene; The method is by least comprising catalyst regenerator, settling vessel, riser reactor, and the device of separation column and gas separation unit composition completes, and it is characterized in that wax oil and freshening gasoline, C
4hydrocarbon adopts single reactor or double-reactor to prepare catalytic pyrolysis low-carbon alkene; The temperature of reaction of wax catalysis cracking reactor 550 ~ 650 DEG C, agent-oil ratio 9 ~ 12,2.0 ~ 3.0 seconds reaction times; The temperature of reaction of gasoline catalytic cracking reactor 550 ~ 650 DEG C, agent-oil ratio 10 ~ 15,2.0 ~ 3.0 seconds reaction times; The part or all of slurry oil product of catalytic pyrolysis is sprayed into the slurry oil-spent agent mixing zone being provided with axial annular baffle plate, enter revivifier emulsion zone combustion heat release subsequently, in order to thermal regeneration catalyzer, thus solve the problem that wax catalysis scission reaction coke output cannot meet Process Energy demand.
Description
Technical field
The present invention relates to the method for a kind of wax catalysis cracking for low-carbon alkene, especially provide a kind of by gasoline, C
4hydrocarbon freshening also combines the method that regeneration concurrent heating realizes catalytic pyrolysis increased low carbon olefine output.
Background technology
The low-carbon alkene such as ethene, propylene is important basic organic chemical industry raw material, but the output of low China carbon olefin but can not satisfy the demands far away, and the degree of self-sufficiency of 2009 is only 43%.Increased low carbon olefine output not only concerns national economy sustainable development, and contains huge economic benefit and social benefit, has important practical significance and long-range strategic importance.
At present, the ethene in the whole world more than 95% and the propylene of about 66% adopt tube furnace steam heat cracking technology to produce.But steam cracking process reaction needed high temperature, high to the requirement of equipment, energy consumption is large, and by product (hydrogen, methane, coke) yield is high, and propene yield is lower.Harsh reaction conditions makes the easier coking of boiler tube and shortens coke-burning cycle, and makes boiler tube easily damage due to carburizing, is therefore difficult to improve ethene, propene yield by the severity improving steam heat scission reaction again.The raw material mainly petroleum naphtha of China's steam heat cracker, raw material is too single, and the trend of crude oil in China in poor quality and heaviness is day by day serious at present, add domestic market also very large to the demand of gasoline, so will certainly cause steam heat cracker because of raw material in short supply, production cost increases, and is therefore badly in need of the Technology developing catalytic pyrolysis increased low carbon olefine output.
At present, the technological line utilizing Deep Catalytic Cracking process to produce low-carbon alkene becomes trend.Catalytic pyrolysis refers to the hydrocarbon cracking reaction carried out in the presence of a catalyst, features such as can reducing temperature of reaction, improve product yield and selectivity, have raw material wide accommodation simultaneously, product slates is easy to adjustment and energy consumption is low.At present, domestic and international insider develops the complete set technology of a series of increased low carbon olefine output in succession from aspects such as improving catalytic cracking reaction severity, such as, be the DCC technique, CPP technique, HCC technique etc. of reactor with riser tube and take double lifting leg as the MAXOFINTM technique, PetroFCC technique etc. of reactor.These results of study and patented technology are mostly the objects being reached volume increase by optimization reaction-recycled furnish and catalyzer, although all achieve good effect.These technology adopt the heavy feed stock of paraffinic base mostly, but there is coke, dry gas yied is high, and yield of light olefins is on the low side etc. not enough.
The hydrogen richness of the light ends such as wax oil, gasoline is high, containing a large amount of saturated parts, carbon residue is lower than 2.0wt%, and these are all the components being easy to be converted into low-carbon alkene under catalytic cracking reaction condition, therefore, this type of cut can be called " catalytic pyrolysis high quality raw material ".The Superflex technique of KBR company adopts the mixed C of refinery or ethylene unit
4or C
5, the technique such as light cracked gasoline and F-T synthesis low-carbon alkene be that raw material realizes low-carbon olefines high-output; The technology such as MGD, TMP are by the mode increased low carbon olefine output of gasoline reprocessing.
With conventional catalyst cracking technics comparing, there is the feature that coke yield is low, Process Energy demand is large in the lightweight material catalytic pyrolysis low-carbon olefines high-output techniques such as wax oil, thus cause reacting the problem that green coke cannot meet Process Energy demand.Therefore, the energy balance of catalytic pyrolysis process need be realized by heating or concurrent heating mode.Chinese Patent Application No. 200610076192.X and 200510017540.1 discloses a kind of coal of cheapness that utilizes and does the method that origin of heat realizes catalytic pyrolysis process concurrent heating.In the method, the ash content that coal combustion generates causes the dilution of catalyzer and poisons, thus reduces selectivity of light olefin.Chinese Patent Application No. 00124665.8 discloses a kind of stripping stage and then revivifier of being injected by slurry oil and to burn the method for concurrent heating, and the method to cause after slurry oil heavy constituent stripping condensation green coke in settling vessel, affects the long-period stable operation of transposition.Chinese Patent Application No. 200910082942.8 discloses a kind of by the mode of petroleum hydrocarbon raw material by hydrogen burning heating zone and the concurrent heating of hydrogen burning catalyst catalytic combustion.The method can cause the reduction of feed hydrogen utilization ratio, increases coke yield.US6558531 discloses a kind of by one or more snippets territory, injecting lift area under control of oil fuel, and oxygen-containing component multistage injects the method for this riser tube zonal combustion concurrent heating simultaneously, causes the consumption of part low-carbon alkene, affect the safe operation of device simultaneously after the method is inevitable.
Summary of the invention
The object of this invention is to provide the method for a kind of wax catalysis cracking for low-carbon alkene.In conjunction with gasoline, C
4hydrocarbon freshening and regeneration concurrent heating technology realize wax catalysis producing low-carbon olefins by cracking, improve ethene, propene yield, especially improve propene yield.
Wax catalysis cracking of the present invention is for the method for low-carbon alkene, and the method comprises:
Catalytic pyrolysis single reactor or catalytic pyrolysis double-reactor is adopted to complete the catalytic cracking reaction of wax oil and freshening component; During single reactor catalytic pyrolysis, freshening gasoline and C
4hydro carbons enters extension diameter section from the bottom of catalytic cracking reaction device extension diameter section together, and wax oil enters reactor extension diameter section from higher than the position bottom extension diameter section; The catalytic cracking gasoline cut of freshening can be the full cut of raw gasline, raw gasline lighting end (final boiling point≤80 DEG C) or raw gasline last running (initial boiling point >80 DEG C), and these cuts are set up B-grade condensation system to obtain in fractionator overhead.During double-reactor catalytic pyrolysis, freshening gasoline enters gasoline catalytic cracking reactor, C
4hydro carbons enters wax catalysis cracking reactor.
During double-reactor, on revivifier side, riser reactor is set as wax oil and C
4the reaction zone of raw material, makes wax oil and C
4raw material contacts in this riser reactor with the regenerated catalyst from revivifier, and catalytic cracking reaction occurs, and draws reactive system after reacted oil gas and catalyst separating, and the catalyzer after separation recycles through revivifier coke burning regeneration.
Separately establish gasoline catalytic cracking reactor as the reaction zone of freshening gasoline on revivifier side, regenerated catalyst from revivifier introduces this reactor from reactor bottom, the regenerated catalyst introduced with bottom while gasoline stocks is upwards flowed under lift gas effect contacts, and make this raw material and regenerated catalyst jointly increase, complete catalytic cracking reaction, draw reactive system after reacted oil gas and catalyst separating, the catalyzer after separation recycles through revivifier coke burning regeneration; Wax oil reactor can be communicated with an oil-gas separator respectively with the exit end of gasoline reactor, or riser reactor is communicated in same oil-gas separator after being connected with the exit end of gasoline reactor again.
Provided by the inventionly utilize wax catalysis cracking increased low carbon olefine output method, wax oil reactor feed adopts extension diameter section charging, and the height of extension diameter section is 2 ~ 10% of riser tube total height, is namely about 1 ~ 2 meter, and wax oil nozzle is positioned at above freshening component opening for feed.In extension diameter section, flow velocity is 0.5 ~ 5 meter per second, there is strong back-mixing effect in extension diameter section, realize each stock reaction raw materials abundant vaporization and with fully the contacting of catalyzer, thus to lay the foundation for the catalytic effect giving full play to catalyzer in follow-up riser reactor.
It is high that the lightweight material such as wax oil and gasoline has hydrogen richness, containing a large amount of saturated cuts, the feature transformed is easy under catalytic cracking reaction condition, the present invention adopts the reaction conditions of wax oil riser reactor to be preferably: temperature of reaction 550 ~ 650 DEG C, the weight ratio of agent-oil ratio 9 ~ 12(catalyzer and oil plant), 2.0 ~ 3.0 seconds reaction times, raw material preheating temperature 100 ~ 300 DEG C.The reaction conditions of gasoline rising pipe reactor is preferably: temperature of reaction 550 ~ 650 DEG C, the weight ratio of agent-oil ratio 10 ~ 15(catalyzer and oil plant), 2.0 ~ 3.0 seconds reaction times, raw material preheating temperature 100 ~ 300 DEG C.
Provided by the inventionly utilize wax catalysis cracking increased low carbon olefine output method, compared with the catalytic cracking technology of current industrial application, there is reaction coke output combustion heat release and be not enough to the problem meeting catalytic pyrolysis energy requirement.For this reason, the present invention proposes the method for the slurry oil-spent agent mixing zone combustion heat release part or all of slurry oil product of catalytic pyrolysis being sprayed into revivifier.
Through stripping stage stripping reclaim to carry secretly after oil gas reclaimable catalyst by governor valve control flow after, enter slurry oil-spent agent mixing zone along standpipe.Slurry oil-spent agent mixing zone is positioned at regenerator bottoms, installs ring baffle, realizes and the separating of the regenerated catalyst of bottom.The regeneration air that slurry oil-spent agent mixing zone need pass into about 10 ~ 50% is to realize fully mixing of slurry oil and reclaimable catalyst, and mixed catalyzer moves upward along the mixing zone of regenerator bottoms and enters the burning emulsion zone of revivifier under air-lift unit effect.The regeneration air of residue 50 ~ 90% enters burning emulsion zone by main air system of distribution, realizes the Thorough combustion heat release of coke and slurry oil.The revivifier of height block form cat-cracker needs for further adjustments, and spent agent inclined tube is extended to revivifier centre, and end installs one section of standpipe, and extends into slurry oil-spent agent mixing zone.
Accompanying drawing explanation
Fig. 1 is the process flow diagram of the embodiment of the present invention 1.
Fig. 2 is the process flow diagram of the embodiment of the present invention 2.
Embodiment
Embodiment 1
See the flow process of Fig. 1, the coaxial-type device coaxially arranged for settling vessel and revivifier in catalyst regenerator 5(the present invention of wax catalysis scission reaction device, also settling vessel can be adopted in production on riser reactor top but the height block form device be arranged in parallel with revivifier, the two is the conventional structure of this area) side arranges riser reactor 2, a part of high-temperature regenerated catalyst in catalyst regenerator 5 is entered riser reactor 2 by catalyst transport 6 and the regenerated catalyst slide valve 7 on it and is upwards flowed under the castering action of lift gas 8.To be a height be in the catalytic pyrolysis intake zone extension diameter section 1 of 1 ~ 2 meter, the gasoline of freshening and C
4component 9 enters the bottom of extension diameter section 1 by feed atomization system, wax oil raw material 10 from extension diameter section, top injects obliquely, angle 30 ~ 60 °.Maintaining gas speed in extension diameter section is 0.5 ~ 5 meter per second, is fast bed fluidized-bed form, forms the strong back-mixing of raw material and catalyzer, realizes raw material and contact abundant mixing of catalyzer.Be 100 ~ 300 DEG C and regenerated catalyst slide valve 7 aperture by regulating raw material preheating temperature, controlling the regenerated catalyst temperature before entering riser reactor 2 is 680 ~ 750 DEG C, make oil gas in riser reactor 2 temperature of reaction 550 ~ 650 DEG C, agent weight of oil, than 9 ~ 12, completes reaction under the condition of reaction times 2.0 ~ 3.0s.Reacted catalyzer and oil gas are through oil and gas separating system 11(gas-solid quick disconnector, also oil-gas separator is claimed, following examples are identical), settling vessel 3 and top revolve 12 be separated after oil gas draw catalytic-cracking reaction system (device), and catalyzer enters stripping stage 4 carries out stripping, after to enter the slurry oil-spent agent mixing zone 14 of catalyst regenerator through catalyzer ingress pipe 13.Slurry oil-spent agent mixing zone 14 is axially installed with ring-shaped baffle, and guarantee reclaimable catalyst is separated with regenerated catalyst.In slurry oil-spent agent mixing zone, concurrent heating is provided, the recycle stock 23 of heating evenly sprayed into by multiple nozzle 15, to ensure the recycle stock uniform temperature on reclaimable catalyst sprayed into, thus partial combustion heat release in regenerative process is avoided too much to cause catalyzer temperature runaway to sinter.The regeneration air 16 being about 10 ~ 50% enters revivifier by slurry oil-spent agent mixing zone, reclaimable catalyst is mixed, mixed reclaimable catalyst is promoted to regeneration emulsion zone simultaneously.Remaining regeneration air enters revivifier by main air system of distribution 17, realizes the combustion heat release of coke on reclaimable catalyst.
The bottom of the catalyst detergent desuperheating section being located at separation column 18 bottom is entered from the temperature of the settling vessel 3 Base top contact oil gas 32 that is 450 ~ 600 DEG C, in catalyst detergent desuperheating section, carry out the washing of catalyst fines with the slurry oil 22 through heat exchange attracted from former cat-cracker and carry out heat exchange, slurry oil 22 is introduced from the top of catalyst detergent desuperheating section.Then slurry oil 22 is drawn through oil-slurry pump 19 from fractionation column base and enters oil slurry steam generator 20 and reclaim heat of high temperature, enter interchanger 21 heat exchange again, part slurry oil returns the riser reactor of former cat-cracker, and the slurry oil temperature controlled before oil-slurry pump 19 is 280 ~ 350 DEG C.Set up the extraction line of diesel oil distillate at the middle part of separation column 18, extract diesel oil distillate 25 out by diesel oil pump 24.Oil-gas condenser 26 and catch pot 27 is set up at the top of separation column 18, to isolate rich gas 29 and naphtha fraction 28, rich gas 29 can enter rich gas compressor entrance, part naphtha fraction 31 returns to separation column 18 top as trim the top of column, and remainder naphtha fraction 30 enters the absorbing-stabilizing system of former catalytic cracking unit.Gaseous product after Vapor recovery unit enters gas separation system further, isolates ethene, the low-carbon alkenes such as propylene, obtains C4 hydrocarbon component simultaneously, separately/return catalytic pyrolysis riser reactor with the gasoline of part freshening from feed(raw material)inlet 9; The Vapor recovery unit of this part and gas separation unit can consult pertinent texts and patent.
Embodiment 2
See the flow process of Fig. 2, it is the height block form device be set up in parallel for settling vessel and revivifier in catalyst regenerator 5(the present invention of wax catalysis scission reaction device, also settling vessel and revivifier can be adopted in production coaxially to arrange, the two is the conventional structure of this area) side arranges wax oil riser reactor 2, and a part of high-temperature regenerated catalyst in catalyst regenerator 5 is entered riser reactor 2 by catalyst transport 6 and the regenerated catalyst slide valve 7 on it and is upwards flowed under the castering action of lift gas 8.To be a height be in the catalytic pyrolysis intake zone extension diameter section 1 of 1 ~ 2 meter, the C4 component 9 of freshening enters the bottom of extension diameter section 1 by feed atomization system, wax oil raw material 10 from extension diameter section, top injects obliquely, angle is 30 ~ 60 °.In extension diameter section, gas speed is 0.5 ~ 5 meter per second, is fast bed fluidized-bed form, forms the strong back-mixing of raw material and catalyzer, realizes raw material and contact abundant mixing of catalyzer.Be 100 ~ 300 DEG C and regenerated catalyst slide valve 7 aperture by regulating wax oil raw material preheating temperature, controlling the regenerated catalyst temperature before entering riser reactor 2 is 680 ~ 750 DEG C, make oil gas in riser reactor 2 temperature of reaction 550 ~ 650 DEG C, agent-oil ratio 9 ~ 12, completes reaction under the condition of reaction times 2.0 ~ 3.0s.Reacted catalyzer and oil gas are through oil and gas separating system 11(gas-solid quick disconnector, also oil-gas separator is claimed, following examples are identical), settling vessel 3 and top revolve 12 be separated after oil gas draw catalytic-cracking reaction system (device), and catalyzer enters stripping stage 4 carries out stripping, by entering the slurry oil-spent agent mixing zone 14 of catalyst regenerator after guiding valve 37 on reclaimable catalyst transport pipe through catalyzer ingress pipe 13.
The gasoline component 30 of freshening enters the bottom of gasoline catalytic cracking reactor 35 by feed atomization system 33, inject obliquely, and angle is 30 ~ 60 °.It is 680 ~ 750 DEG C that adjustment regenerated catalyst slide valve 34 aperture controls the regenerated catalyst temperature before entering riser reactor 35, make oil gas in riser reactor 35 temperature of reaction 550 ~ 650 DEG C, agent-oil ratio 10 ~ 15, completes reaction under the condition of reaction times 2.0 ~ 3.0s.Reacted catalyzer and oil gas through oil and gas separating system, settling vessel 32 and top revolve be separated after oil gas draw catalytic-cracking reaction system (device), and catalyzer enters stripping stage carries out stripping, by entering the slurry oil-spent agent mixing zone 14 of catalyst regenerator after guiding valve 36 on reclaimable catalyst transport pipe through catalyzer ingress pipe 13.
Slurry oil-spent agent mixing zone 14 is axially installed with ring-shaped baffle, and guarantee reclaimable catalyst is separated with regenerated catalyst.In slurry oil-spent agent mixing zone, concurrent heating is provided, the recycle stock 23 of heating evenly sprayed into by multiple nozzle 15, to ensure the recycle stock uniform temperature on spent agent sprayed into, thus partial combustion heat release in regenerative process is avoided too much to cause catalyzer temperature runaway to sinter.The regeneration air 16 being about 10 ~ 50% enters revivifier by slurry oil-spent agent mixing zone, spent agent is mixed, mixed spent agent is promoted to regeneration emulsion zone simultaneously.Remaining regeneration air enters revivifier by main air system of distribution 17, realizes the combustion heat release of coke on reclaimable catalyst.
Merging into one temperature from the high-temperature oil gas of settling vessel 3 top and settling vessel 32 Base top contact is the bottom that the oil gas 36 of 450 ~ 600 DEG C enters the catalyst detergent desuperheating section being located at separation column 18 bottom, in catalyst detergent desuperheating section, carry out the washing of catalyst fines with the slurry oil 22 through heat exchange attracted from former cat-cracker and carry out heat exchange, slurry oil 22 is introduced from the top of catalyst detergent desuperheating section.Then slurry oil 22 is drawn through oil-slurry pump 19 from fractionation column base and enters oil slurry steam generator 20 and reclaim heat of high temperature, then enters interchanger 21 heat exchange, and part slurry oil returns the riser reactor of former cat-cracker.Set up the extraction line of diesel oil distillate at the middle part of separation column 18, extract diesel oil distillate 25 out by diesel oil pump 24, controlling diesel oil draw out temperature is 220 ~ 250 DEG C.Oil-gas condenser 26 and catch pot 27 is set up at the top of separation column 18, to isolate rich gas 29 and naphtha fraction 28, rich gas 29 can enter rich gas compressor entrance, part naphtha fraction 31 returns to separation column 18 top as trim the top of column, and remainder naphtha fraction 30 enters the absorbing-stabilizing system of former catalytic cracking unit.Gaseous product after Vapor recovery unit can enter gas separation system further, isolates ethene, the low-carbon alkenes such as propylene, obtains C4 hydrocarbon component simultaneously, returns catalytic pyrolysis riser reactor from feed(raw material)inlet 9; The Vapor recovery unit of this part and gas separation unit can consult pertinent texts and patent.
Claims (8)
1. wax catalysis cracking is for a method for low-carbon alkene, and the method is by least comprising catalyst regenerator, settling vessel, riser reactor, and the device of separation column and gas separation unit composition completes, and it is characterized in that: wax oil and freshening gasoline, C
4hydrocarbon adopts single reactor or double-reactor to prepare catalytic pyrolysis low-carbon alkene;
When adopting single reactor, freshening gasoline and freshening C
4hydrocarbon enters extension diameter section from riser reactor extension diameter section bottom together, and wax oil opening for feed is the middle and upper part of extension diameter section;
When adopting double-reactor, freshening gasoline enters independently reactor and carries out catalytic cracking reaction; C
4hydrocarbon enters extension diameter section from wax oil reactor extension diameter section bottom, and wax oil opening for feed is the middle and upper part of extension diameter section;
The reaction conditions of wax catalysis cracking reactor is: temperature of reaction 550 ~ 650 DEG C, agent weight of oil than 9 ~ 12,2.0 ~ 3.0 seconds reaction times;
The reaction conditions of gasoline catalytic cracking reactor is: temperature of reaction 550 ~ 650 DEG C, agent weight of oil than 10 ~ 15,2.0 ~ 3.0 seconds reaction times;
Catalyst regeneration temperature is kept by slurry oil being sprayed into combustion heat release in revivifier.
2. wax catalysis cracking according to claim 1 is for the method for low-carbon alkene, it is characterized in that: the temperature of reaction of wax catalysis cracking reactor 580 ~ 620 DEG C, agent weight of oil than 9 ~ 12,2.0 ~ 3.0 seconds reaction times;
The temperature of reaction of gasoline catalytic cracking reactor 580 ~ 620 DEG C, agent weight of oil than 10 ~ 15,2.0 ~ 3.0 seconds reaction times.
3. wax catalysis cracking according to claim 1 is for the method for low-carbon alkene, it is characterized in that: the height of wax oil reactor extension diameter section is 2 ~ 10% of riser tube total height, and in extension diameter section, velocity of flow is 0.5 ~ 5 meter per second.
4. wax catalysis cracking according to claim 1 is for the method for low-carbon alkene, it is characterized in that: the gasoline fraction of freshening is the full cut of raw gasline, the raw gasline lighting end of final boiling point≤80 DEG C or the raw gasline last running of initial boiling point >80 DEG C, and these cuts are set up B-grade condensation system to obtain in fractionator overhead.
5. wax catalysis cracking according to claim 1 is for the method for low-carbon alkene, it is characterized in that: when adopting double-reactor, material and the material from gasoline reaction zone from wax oil reaction zone utilize being separated of oil-gas separation mechanism realization response oil gas and catalyzer respectively; Or make the described material from two reaction zones after converging, utilize being separated of an oil-gas separation mechanism realization response oil gas and catalyzer.
6. wax catalysis cracking according to claim 1 is for the method for low-carbon alkene, it is characterized in that: during double-reactor operation, described catalyst regenerator respectively with bottom wax oil pipe reactor, gasoline rising pipe reactor bottom is communicated with, and all arranges the guiding valve for controlling regenerated catalyst flow in each catalyst transport; The exit end of reactor is all communicated with the oil-gas separator in settling vessel.
7. wax catalysis cracking according to claim 1 is for the method for low-carbon alkene, it is characterized in that: reclaimable catalyst is by after governor valve control flow, slurry oil-spent agent mixing zone is entered along standpipe, slurry oil-spent agent mixing zone is positioned at regenerator bottoms, axially annular baffle arrangement is installed, realizes the separation with the regenerated catalyst of bottom.
8. wax catalysis cracking according to claim 1 is for the method for low-carbon alkene, it is characterized in that: in revivifier, spent agent inclined tube need extend to revivifier centre, and end installs one section of standpipe, and extends into slurry oil-spent agent mixing zone.
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| CN114341317A (en) * | 2019-08-05 | 2022-04-12 | 沙特基础工业全球技术公司 | Additional heat source for naphtha catalytic cracking |
| CN113717754B (en) * | 2021-09-24 | 2023-04-25 | 上海纳科助剂有限公司 | Catalytic cracking process for producing high aromatic hydrocarbon oil and high yield liquefied gas |
| CN113717753B (en) * | 2021-09-24 | 2023-04-25 | 上海纳科助剂有限公司 | High aromatic hydrocarbon oil material and preparation method and application thereof |
| CN113755208B (en) * | 2021-09-24 | 2023-04-25 | 上海纳科助剂有限公司 | High aromatic hydrocarbon oil material and preparation method and application thereof |
| CN113773874B (en) * | 2021-09-24 | 2023-04-25 | 上海纳科助剂有限公司 | High aromatic hydrocarbon oil material and preparation method and application thereof |
| CN113897220B (en) * | 2021-09-24 | 2023-04-25 | 上海纳科助剂有限公司 | High aromatic hydrocarbon oil material and preparation method and application thereof |
| CN113717752B (en) * | 2021-09-24 | 2023-04-25 | 上海纳科助剂有限公司 | High aromatic hydrocarbon oil material and preparation method and application thereof |
| CN115364775B (en) * | 2022-08-17 | 2024-04-12 | 山东高端化工研究院有限公司 | Device for controlling reaction temperature in olefin preparation by crude oil catalytic pyrolysis |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101456782A (en) * | 2007-12-13 | 2009-06-17 | 中国石油化工股份有限公司 | Method for improving propone output during catalytic conversion process |
| CN100509715C (en) * | 2002-10-10 | 2009-07-08 | 凯洛格·布朗及鲁特有限公司 | Catalyst regenerator with central well |
| CN101591562A (en) * | 2009-06-25 | 2009-12-02 | 中国石油化工集团公司 | A kind of fluidized catalytic cracking method and device thereof |
| CN102234531A (en) * | 2010-05-06 | 2011-11-09 | 中国石油天然气股份有限公司 | Device for catalytically cracking heavy oil in sections and application thereof |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100509715C (en) * | 2002-10-10 | 2009-07-08 | 凯洛格·布朗及鲁特有限公司 | Catalyst regenerator with central well |
| CN101456782A (en) * | 2007-12-13 | 2009-06-17 | 中国石油化工股份有限公司 | Method for improving propone output during catalytic conversion process |
| CN101591562A (en) * | 2009-06-25 | 2009-12-02 | 中国石油化工集团公司 | A kind of fluidized catalytic cracking method and device thereof |
| CN102234531A (en) * | 2010-05-06 | 2011-11-09 | 中国石油天然气股份有限公司 | Device for catalytically cracking heavy oil in sections and application thereof |
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