CN102746887A - Catalytic cracking method - Google Patents
Catalytic cracking method Download PDFInfo
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- CN102746887A CN102746887A CN2011100967942A CN201110096794A CN102746887A CN 102746887 A CN102746887 A CN 102746887A CN 2011100967942 A CN2011100967942 A CN 2011100967942A CN 201110096794 A CN201110096794 A CN 201110096794A CN 102746887 A CN102746887 A CN 102746887A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
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Abstract
The invention discloses a catalytic cracking method. The method comprises steps of: introducing dry gas and C4 hydrocarbon into a middle and lower part of a stripping section of a sub-precipitator to react with a gasoline coked catalyst; introducing the oil gas after reaction into a sub-fractionating column; introducing part of the coked catalyst treated with steam stripping into a regenerator for regeneration, and introducing the other part of the coked catalyst treated with steam stripping into a pre-lifting mixer and mixing with a regenerative agent from the regenerator; and returning the mixed catalyst to a heavy oil riser reactor. The method can reduce yield of dry gas by 0.3-1.5 percentage, reduce yield of liquefied gas (not including propylene) by 2.0-8.0 percentage, increase yield of gasoline by 1-4 percentage, and increase yield of propylene by 0.5-2.5 percentage.
Description
Technical field
The invention belongs under the situation that does not have hydrogen the catalytic cracking field of hydrocarbon ils, particularly a kind of catalyst cracking method that improves light oil yield and propylene.
Background technology
When paying attention to environment protection, the maximization of economic benefit is the target that enterprise is pursued forever.Gently receipts, high productivity of propylene are the important means that catalytic cracking technology is increased economic efficiency always and hang down dry gas yied, height.In recent years, domestic each research institution has carried out fruitful research aspect the distribution of catalytic cracking product being devoted to improve, and the technology of exploitation mainly contains following several:
The US of Uop Inc. 5451313 disclosed " X design ", this new design has been invented in nineteen ninety-five by Uop Inc., its objective is the rising agent oil ratio, improves product and distributes.Be characterized in being provided with a catalyst mix device between reactor drum and the revivifier, spent agent mixes in mixing tank with regenerator, and the partial confounding mixture flows into riser tube and raw material contact reacts, and remaining mixture flows into revivifier and regenerates.The benefit of this structure is the mixture temperature that gets into riser tube than next low of revivifier, and the catalyst recirculation amount is increased, and agent-oil ratio improves, so thermal response minimizings, catalyzed reaction increase, coke and dry gas yied reduction, gasoline yield increase.But it is very low that this design shortcoming is exactly a spent agent activity in the mixed catalyst, makes the active on the low side of mixture, is unfavorable for the cracking of raw oil.
The IsoCat technology of Petrobras company (US 6059958) is characterized in that one returns regenerator bed with being divided into two strands through external warmer refrigerative catalyzer, and another strand mixes the back and get into riser tube and raw oil reaction with the regenerated catalyst of heat.Obviously, the temperature of mixed regeneration catalyzer is lower than the temperature of conventional regenerated catalyst.Similar with " X design " reason of Uop Inc., IsoCat technology can reduce coke and dry gas yied, and two strands of catalyzer of IsoCat technology are regenerated catalyst, and the activity of mixture is higher, more helps catalyzed reaction.But this technology implements comparatively complicated, and the mixed catalyst difficult control of temperature.
CN 1288933 disclosed regenerator sloped tube catalyzer cooling technologies, this method is exactly that a cooling water jecket directly is set outside regenerator sloped tube, lowers the regenerated catalyst temperature of entering riser reactor through water coolant.Though this method has obtained good effect on pilot plant, dry gas and coke yield are significantly descended, bring very big difficulty in industrial practice, for the control of temperature of reaction, that is to say that this method seems simply, it is bigger to put into practice difficulty.
China University Of Petroleum Beijing has proposed novel multi-region and has assisted control heavy oil MZCC catalytic cracking technology (" oil Refining Technologies and engineering " the 12nd phase in 2008); The MZCC technology promotes that with the heat that mixes of regenerator the cracking of hydro carbons macromole, minimizing dry gas and coke are the technology basis to optimize heavy oil, has proposed the strong back-mixing of charging, the propelling of reaction advection, the ultrafast separation of product and chemical steam stripped subregion Collaborative Control new concept.This technology is intended a newly-increased root regeneration inclined tube and air-lift unit pipe, and on this newly-increased regenerator sloped tube, catalyst cooler is set, and cooled catalyzer mixes with the thermocatalyst that former regenerator sloped tube comes; The regenerator and the raw material that mix the back lesser temps carry out contact reacts; This technology can reduce the finish mixing temperature, and the rising agent oil ratio is improved product and distributed; But should show complicated slightly by technology regenerator cooling measure, it is more to set up equipment.
The double lift pipe catalytic cracking technology that CN1710029 is disclosed; This technology is adopted double lifting leg and is set up petrol sediment bulb and secondary separation column by the exploitation of Luoyang Petrochemical engineering corporation, and simultaneously that the part relative temperature is lower gasoline rising pipe reclaimable catalyst is introduced raw oil riser tube catalyzer and promoted mixing tank in advance; Mix the back with the high temperature regeneration agent and get into the raw oil riser tube; So both reduce the finish contact temperature of raw oil riser tube, made full use of the remaining activity of gasoline rising pipe reclaimable catalyst again, improved the agent-oil ratio and the product selectivity of raw oil riser catalytic cracking; Reduce dry gas and coke yield, improve propene yield and propylene selectivity.But should technology in the actual industrial implementation process, though reached gasoline upgrading, propylene enhancing and improved the purpose that product distributes because the dry gas that gasoline upgrading brought is more; Cause the total dry gas yied of device still higher; Light oil yield is relatively low, and the liquefied gas yield of removing behind the propylene is higher, and market value is lower; Therefore still need carry out technological improvement, the overall benefit of device is further improved.
Summary of the invention
The present invention mainly is a kind of reduction double lift pipe catalytic cracking technology dry gas and liquefied gas (the not containing propylene) productive rate that provides to double lift pipe catalytic cracking technology dry gas and liquefied gas (not containing propylene) productive rate height, improves the new catalyst cracking method of light oil and productivity of propylene simultaneously.
A kind of catalyst cracking method of the present invention is characterized in that comprising the steps:
1) raw oil gets into double lift pipe catalytic cracking device heavy oil riser reactor bottom; With catalyzer contact reacts from preparatory lifting mixing tank; Reacted oil gas separates with reclaimable catalyst; Isolated reaction oil gas gets into main fractionating tower, and isolated reclaimable catalyst gets into main settling vessel stripping stage and behind stripping, gets into revivifier regeneration;
2) raw gasline gets into double lift pipe catalytic cracking device gasoline rising pipe reactor lower part; With catalyzer contact reacts from revivifier; Reacted oil gas separates with reclaimable catalyst, and isolated reaction oil gas gets into secondary separation column, and isolated reclaimable catalyst gets into secondary settling vessel stripping stage;
3) dry gas and C
4Hydrocarbon gets into secondary settling vessel stripping stage middle and lower part and gasoline spent agent contact reacts; Reacted oil gas gets into secondary separation column; Reclaimable catalyst part behind stripping gets into revivifier regeneration; Another part gets into and to promote mixing tank in advance and mix with regenerator from revivifier, and mixed catalyzer turns back to step 1).
Described reacted oil gas separates with reclaimable catalyst, and isolated reaction oil gas isolates further that catalyst fines is laggard goes into main fractionating tower or secondary separation column.
Described dry gas and C
4Hydrocarbon gets into secondary settling vessel stripping stage middle and lower part and gasoline spent agent contact reacts, dry gas and C respectively or simultaneously
4Hydrocarbon is self-produced or from other device for this device, described C
4Hydrocarbon be in the liquefied gas C
4Hydrocarbon.
Described a kind of catalyst cracking method, dry gas and C
4Hydrocarbon gets into secondary settling vessel stripping stage middle and lower part and gasoline spent agent contact reacts, and temperature of reaction is 300～600 ℃, is preferably 350～580 ℃, is preferably 380～560 ℃; The dry gas weight hourly space velocity is 0.05～1.0h
-1, be preferably 0.1～0.8h
-1, be preferably 0.15～0.5h
-1C
4The hydro carbons weight hourly space velocity is 0.1～3.0h
-1, be preferably 0.3～2.5h
-1, be preferably 0.8～2.0h
-1The reaction absolute pressure is 0.15～0.40MPa, is preferably 0.20～0.36MPa, is preferably 0.22～0.33MPa.
Said heavy oil riser reactor outlet temperature of reaction is 450～560 ℃, is preferably 460～540 ℃, is preferably 470～530 ℃; Reaction times is 0.5～5 second, is preferably 1.0～4.5 seconds, is preferably 1.5～4.0 seconds; The agent weight of oil is 3～20 than (catalyst recirculation amount and inlet amount weight ratio, the catalyst recirculation amount is by riser tube outlet internal circulating load), is preferably 5～18, is preferably 7～15; The reaction absolute pressure is 0.15～0.40MPa, is preferably 0.20～0.36MPa, is preferably 0.22～0.33MPa; It is 550～700 ℃ that raw oil riser reactor bottom promotes mixer temperature in advance, is preferably 580～670 ℃, is preferably 590～660 ℃; The regeneration temperature of revivifier is 650～750 ℃, and the carbon content of regenerated catalyst is 0.02～0.2 weight %, and the regenerated catalyst micro-activity is generally 55～70.
Said gasoline rising pipe reactor outlet temperature of reaction is 320～630 ℃, is preferably 350～600 ℃, is preferably 370～580 ℃; Reaction times is 0.5～5 second, is preferably 1.0～4.5 seconds, is preferably 1.5～4.0 seconds; The agent weight of oil is 3～20 than (catalyst recirculation amount and inlet amount weight ratio, the catalyst recirculation amount is by riser tube outlet internal circulating load), is preferably 4～18, is preferably 5～15; The reaction absolute pressure is 0.15～0.40MPa, is preferably 0.20～0.36MPa, is preferably 0.22～0.33MPa; Said gasoline rising pipe reactor feed contains a kind of in petroleum naphtha or the heavy petrol of catalytically cracked gasoline, catalytic cracking gasoline, pressure gasoline, cracking ethylene preparation gasoline, coker gasoline, straight-run spirit and above gasoline at least.
The present invention improves existing double lift pipe catalytic cracking method, with C in dry gas and the liquefied gas
4Hydro carbons is introduced secondary settling vessel stripping stage middle and lower part and the higher gasoline spent agent contact reacts of remaining activity respectively or simultaneously, through C in ethene, the liquefied gas in the dry gas
4Reactions such as that alkene takes place is superimposed, alkylation, aromizing and hydrogen transference generate gasoline, the disproportionation reaction that takes place of ethene and 2-butylene simultaneously, generation propylene.Through above reaction process, can obviously reduce dry gas and liquefied gas (not containing propylene) productive rate, improve gasoline and productivity of propylene.Vapour, diesel oil character are constant basically.
Compare with existing double lift pipe catalytic cracking method, beneficial effect of the present invention is:
(1) the device dry gas yied descends 0.3～1.5 percentage point, and liquefied gas (not containing propylene) productive rate descends 2.0～8.0 percentage points.
(2) gasoline yield improves 1.0～4.0 percentage points, and productivity of propylene improves 0.5～2.5 percentage point.
Utilize embodiment that the present invention is further explained below, but do not limit the scope of the invention.
Embodiment
Embodiment 1 (Comparative Examples)
On the double lift pipe catalytic cracking testing apparatus, make an experiment, the charging of raw oil riser tube is for mixing heavy oil, and main character is listed in table 1, and treatment capacity is 30 kg/day; The gasoline rising pipe charging is the self-produced gasoline of device, and treatment capacity is 12 kg/day.The test catalyst system therefor is a MLC-500 industry poiser, and the equilibrium catalyst micro-activity is 62, and carbon content is 0.05w%.The main operational condition of double lift pipe catalytic cracking testing apparatus, product distribute and list in table 2.
Embodiment 2 (Comparative Examples)
Press embodiment 1, different is that the gasoline rising pipe temperature of reaction is 520 ℃, and main operational condition, product distribute and list in table 2.
Embodiment 3 (Comparative Examples)
Press embodiment 1, different is that the gasoline rising pipe temperature of reaction is 500 ℃, and main operational condition, product distribute and list in table 2.
Embodiment 4
Press embodiment 1, that different is the C in self-produced dry gas of device and the liquefied gas
4Hydro carbons gets into secondary settling vessel stripping stage middle and lower part, and main operational condition, product distribute and list in table 3.
Embodiment 5
Press embodiment 2, that different is the C in self-produced dry gas of device and the liquefied gas
4Hydro carbons gets into secondary settling vessel stripping stage middle and lower part, and main operational condition, product distribute and list in table 3.
Embodiment 6
Press embodiment 3, that different is the C in self-produced dry gas of device and the liquefied gas
4Hydro carbons gets into secondary settling vessel stripping stage middle and lower part, and main operational condition, product distribute and list in table 3.
The main character of table 1 raw oil riser reactor charging
| Project | Embodiment 1～6 |
| The raw oil title | Mix heavy oil |
| Density (20 ℃)/kg.m -3 | 923.6 |
| Carbon residue/% | 3.50 |
| Molecular weight | 450 |
| Boiling range/℃ | |
| IBP | 320 |
| 10％ | 375 |
| 30％ | / |
| 50％ | 450 |
| 70％ | / |
| 90％ | 589 |
| C/ weight % | 86.65 |
| H/ weight % | 12.25 |
| S/ weight % | 0.65 |
| N/ weight % | 0.14 |
| Group composition/weight % | |
| Stable hydrocarbon | 54.26 |
| Aromatic hydrocarbons | 32.10 |
| Colloid+bituminous matter | 13.64 |
| Metal content/μ g.g -1 | |
| Ni | 4.4 |
| V | 9.0 |
| Fe | 1.7 |
| Na | 1.5 |
Main operational condition of table 2 and product distribute
| Project | Embodiment 1 | Embodiment 2 | Embodiment 3 |
| Catalyzer | MLC-500 | MLC-500 | MLC-500 |
| Main operational condition | |||
| The riser tube temperature out/℃ * | 520/550 | 520/520 | 520/500 |
| Reaction pressure (gauge pressure) */MPa | 0.20/0.20 | 0.20/0.20 | 0.20/0.20 |
| Agent-oil ratio * | 9.8/12.1 | 9.8/10.2 | 9.8/8.0 |
| Reaction times */s | 2.92/3.01 | 2.90/3.05 | 2.96/3.10 |
| Product distribution/weight % | |||
| Dry gas | 4.29 | 4.08 | 3.95 |
| Liquefied gas (not containing propylene) | 15.25 | 14.59 | 13.79 |
| Propylene | 9.00 | 8.28 | 7.75 |
| Gasoline | 31.13 | 32.64 | 34.09 |
| Diesel oil | 26.97 | 27.14 | 27.23 |
| Slurry oil | 5.00 | 5.00 | 5.00 |
| Coke | 7.86 | 7.77 | 7.69 |
| Loss | 0.50 | 0.50 | 0.50 |
| Add up to | 100 | 100 | 100 |
| Light oil yield (gasoline+diesel oil) | 58.10 | 59.78 | 61.32 |
*/preceding be raw oil riser tube parameter ,/back be the gasoline rising pipe parameter.
Main operational condition of table 3 and product distribute
*/preceding be raw oil riser tube parameter ,/back be the gasoline rising pipe parameter.
Claims (11)
1. a catalyst cracking method is characterized in that comprising the steps:
1) raw oil gets into double lift pipe catalytic cracking device heavy oil riser reactor bottom; With catalyzer contact reacts from preparatory lifting mixing tank; Reacted oil gas separates with reclaimable catalyst; Isolated reaction oil gas gets into main fractionating tower, and isolated reclaimable catalyst gets into main settling vessel stripping stage and behind stripping, gets into revivifier regeneration;
2) raw gasline gets into double lift pipe catalytic cracking device gasoline rising pipe reactor lower part; With catalyzer contact reacts from revivifier; Reacted oil gas separates with reclaimable catalyst, and isolated reaction oil gas gets into secondary separation column, and isolated reclaimable catalyst gets into secondary settling vessel stripping stage;
3) dry gas and C
4Hydrocarbon gets into secondary settling vessel stripping stage middle and lower part and gasoline spent agent contact reacts; Reacted oil gas gets into secondary separation column; Reclaimable catalyst part behind stripping gets into revivifier regeneration; Another part gets into and to promote mixing tank in advance and mix with regenerator from revivifier, and mixed catalyzer turns back to step 1).
2. according to the described a kind of catalyst cracking method of claim 1, it is characterized in that: described dry gas and C
4Hydrocarbon gets into secondary settling vessel stripping stage middle and lower part and gasoline spent agent contact reacts respectively or simultaneously.
3. according to the described a kind of catalyst cracking method of claim 1, it is characterized in that: described dry gas and C
4Hydrocarbon is that device is self-produced or from other device.
4. according to the described a kind of catalyst cracking method of claim 1, it is characterized in that: described C
4Hydrocarbon be in the liquefied gas C
4Hydrocarbon.
5. according to the described a kind of catalyst cracking method of claim 1, it is characterized in that: described dry gas and C
4Hydrocarbon gets into secondary settling vessel stripping stage middle and lower part and gasoline spent agent contact reacts, and temperature of reaction is 300～600 ℃, and the dry gas weight hourly space velocity is 0.05～1.0h
-1, C
4The hydro carbons weight hourly space velocity is 0.1～3.0h
-1, the reaction absolute pressure is 0.15～0.40MPa.
6. according to the described a kind of catalyst cracking method of claim 1, it is characterized in that: described dry gas and C
4Hydrocarbon gets into secondary settling vessel stripping stage middle and lower part and gasoline spent agent contact reacts, and temperature of reaction is 380～560 ℃, and the dry gas weight hourly space velocity is 0.15～0.5h
-1, C
4The hydro carbons weight hourly space velocity is 0.8～2.0h
-1, the reaction absolute pressure is 0.22～0.33MPa.
7. according to the described a kind of catalyst cracking method of claim 1; It is characterized in that: described heavy oil riser reactor outlet temperature of reaction is 450～560 ℃; Reaction times is 0.5～5 second, and agent weight of oil ratio is 3～20, and the reaction absolute pressure is 0.15～0.40MPa; Promoting mixer temperature in advance is 550～700 ℃, and the regeneration temperature of revivifier is 650～750 ℃.
8. according to the described a kind of catalyst cracking method of claim 1; It is characterized in that: described heavy oil riser reactor outlet temperature of reaction is 470～530 ℃; Reaction times is 1.5～4.0 seconds; Agent weight of oil ratio is 7～15, and the reaction absolute pressure is 0.22～0.33MPa, and promoting mixer temperature is 590～660 ℃.
9. according to the described a kind of catalyst cracking method of claim 1; It is characterized in that: said gasoline rising pipe reactor outlet temperature of reaction is 320～630 ℃; Reaction times is 0.5～5 second, and agent weight of oil ratio is 3～20, and the reaction absolute pressure is 0.15～0.40MPa.
10. according to the described a kind of catalyst cracking method of claim 1, it is characterized in that: said gasoline rising pipe reactor outlet temperature of reaction is for being 370～580 ℃, and the reaction times is 1.5～4.0 seconds; Agent weight of oil ratio is 5～15, and the reaction absolute pressure is 0.22～0.33MPa.
11. according to the described a kind of catalyst cracking method of claim 1, it is characterized in that: said raw gasline is at least a in petroleum naphtha or the heavy petrol of catalytically cracked gasoline, catalytic cracking gasoline, pressure gasoline, cracking ethylene preparation gasoline, coker gasoline, straight-run spirit and above gasoline.
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| CN2011100967942A CN102746887A (en) | 2011-04-19 | 2011-04-19 | Catalytic cracking method |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104046387A (en) * | 2013-03-11 | 2014-09-17 | 中石化洛阳工程有限公司 | Catalytic cracking technology and device |
| CN109694725A (en) * | 2017-10-20 | 2019-04-30 | 中国石油化工股份有限公司 | A kind of catalyst cracking method producing high-knock rating gasoline |
| CN110295059A (en) * | 2018-03-22 | 2019-10-01 | 中国石油化工股份有限公司 | Catalyst cracking method and system |
| CN112552956A (en) * | 2019-09-25 | 2021-03-26 | 中国石油化工股份有限公司 | Method for cyclic catalytic conversion of hydrocarbons |
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| US6287522B1 (en) * | 1998-10-05 | 2001-09-11 | Uop Llc | FCC apparatus with dual riser |
| CN1401742A (en) * | 2002-09-16 | 2003-03-12 | 中国石油化工集团公司 | Method and apparatus for catalytic upgrading poor gasoline |
| CN1710029A (en) * | 2005-07-01 | 2005-12-21 | 中国石油化工集团公司 | Catalytic cracking method and apparatus |
| CN101724432A (en) * | 2008-10-31 | 2010-06-09 | 中国石油化工股份有限公司 | Method for producing high-octane gasoline by light hydrocarbon non-hydrogenation modification |
-
2011
- 2011-04-19 CN CN2011100967942A patent/CN102746887A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6287522B1 (en) * | 1998-10-05 | 2001-09-11 | Uop Llc | FCC apparatus with dual riser |
| CN1401742A (en) * | 2002-09-16 | 2003-03-12 | 中国石油化工集团公司 | Method and apparatus for catalytic upgrading poor gasoline |
| CN1710029A (en) * | 2005-07-01 | 2005-12-21 | 中国石油化工集团公司 | Catalytic cracking method and apparatus |
| CN101724432A (en) * | 2008-10-31 | 2010-06-09 | 中国石油化工股份有限公司 | Method for producing high-octane gasoline by light hydrocarbon non-hydrogenation modification |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104046387A (en) * | 2013-03-11 | 2014-09-17 | 中石化洛阳工程有限公司 | Catalytic cracking technology and device |
| CN109694725A (en) * | 2017-10-20 | 2019-04-30 | 中国石油化工股份有限公司 | A kind of catalyst cracking method producing high-knock rating gasoline |
| CN109694725B (en) * | 2017-10-20 | 2021-02-09 | 中国石油化工股份有限公司 | Catalytic cracking method for producing high-octane gasoline |
| CN110295059A (en) * | 2018-03-22 | 2019-10-01 | 中国石油化工股份有限公司 | Catalyst cracking method and system |
| CN110295059B (en) * | 2018-03-22 | 2021-06-08 | 中国石油化工股份有限公司 | Catalytic cracking process and system |
| CN112552956A (en) * | 2019-09-25 | 2021-03-26 | 中国石油化工股份有限公司 | Method for cyclic catalytic conversion of hydrocarbons |
| CN112552956B (en) * | 2019-09-25 | 2021-12-17 | 中国石油化工股份有限公司 | Method for cyclic catalytic conversion of hydrocarbons |
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Application publication date: 20121024 |