CN101205476B - Modified fluidization catalytic conversion reactor - Google Patents
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- CN101205476B CN101205476B CN2006101695126A CN200610169512A CN101205476B CN 101205476 B CN101205476 B CN 101205476B CN 2006101695126 A CN2006101695126 A CN 2006101695126A CN 200610169512 A CN200610169512 A CN 200610169512A CN 101205476 B CN101205476 B CN 101205476B
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Abstract
The invention provides an improved fluidization catalytic conversion reactor, comprising a pre-lifted section, a first reaction area and a second reaction area which are coaxial and orderly arranged from bottom to top along the axial direction, wherein, the diameter of the second reaction area is bigger than that of the first reaction area; the improvement of the invention is that: a pore distribution plate is arranged between the first and the second reaction areas. The reactor is provided with a mixing area arranged between the first and the second reaction areas, the pore distribution plate is arranged in the mixing area, which makes even distribution of the catalyst in the second reaction area and is favorable for full contact between the reaction oil-gas and the catalyst. The reactor of the invention can improve the product mass distribution of catalytic cracking devices, which embodies in improving the conversion rate, lowering the dry gas yield, increasing the light liquid yield, reducing the alkene content of the gasoline and increasing the isoalkane content of the gasoline.
Description
Technical field
The invention belongs to a kind of under the situation that does not have hydrogen the catalyticing conversioning equipment of hydrocarbon ils.
Background technology
In order to reduce motor spirit burning institute discharge tail gas pollution on the environment degree, a lot of countries have all formulated strict gasoline quality standard.For example, the new controlling index of motor spirit of China's formulation is: alkene is not more than 35v%, and aromatic hydrocarbons is not more than 40v%, and benzene is not more than 2.5v%, and sulphur is not more than 0.08m%.The oil Refining Technologies structures shape of China the gasoline produced of CCU occupy bigger ratio (approaching 80%) in the gasoline product being in harmonious proportion.Because the raw oil character that China's CCU is processed relatively poor (showing that mainly density is big and carbon residue is high) is so the olefin(e) centent in the gasoline products that CCU is produced is higher, usually between 40v%～65v%.This must cause the gasoline new quality standard of mediation finished product olefin content in gasoline apparently higher than NEPA's defined.Therefore, the olefin(e) centent that reduces in the gasoline products that CCU produces is an important content that traditional catalytic cracking process is carried out technology innovation.
The catalytic cracking reaction of petroleum hydrocarbon is in the riser reactor of catalytic cracking process, to realize.Riser reactor is a vertical hollow circular-tube, and its diameter is about 1m, highly usually between 20m～60m.Liquid raw material oil by four components such as stable hydrocarbon, aromatic hydrocarbons, colloid and bituminous matter are formed sprays into from the riser tube bottom at a certain angle obliquely.When with after the mobile high-temperature regenerated catalyst contacts vertically upward, vaporization takes place rapidly and also begins to take place catalytic cracking reaction in liquid raw material oil.The reaction that has just begun to take place is called as primary first-order equation, mainly is the C-C cleavage reaction of each component of raw oil.One of product of these primary first-order equations is an alkene.Because the reactive behavior of alkene is higher, various secondary reactions take place in immediately, as: cracking, cyclisation, isomerizing, alkylation, hydrogen transference and superimposed, or the like.Obviously, the better method that reduces olefin(e) centent in the gasoline is optionally to strengthen some secondary reactions of alkene, like hydrogen transference and isomerizing, makes alkene be converted into isoparaffin and aromatic hydrocarbons as much as possible.
But conventional riser reactor diameter is that its inlet fluid speed is 4～5 meter per seconds uniformly.Along with the carrying out of catalytic cracking reaction, reactive system generates more small molecules.Molecule expands fluid velocity is vertically upward sharply increased, and reaches 15～18 meter per seconds, and the reaction times significantly reduces, and has only 2～3 seconds.This is unfavorable for that obviously some can improve the carrying out of the alkene secondary reaction that quality product distributes.The Perfected process that addresses this problem is exactly to carry out hole enlargement at section place, middle and upper part of the riser reactor of homogeneous diameter, makes alkene can have the longer time to participate in secondary reaction.CN1237477A, CN1232069A disclose the structure of this reactor drum respectively and use the process method of this reactor drum.Adopt the full scale plant operation result of this reactor drum to show, this reactor drum can significantly reduce olefin content in gasoline, and the total liquid of product is received and increased, the coke selectivity grow, and dry gas and slurry oil productive rate descend.But the expansion of second reaction zone diameter causes the fluid velocity of second reaction zone sharply to reduce, and is incorporated into the reclaimable catalyst of second reaction zone from settling vessel, since the influence of shock resistance, skewness in second reaction zone.Giving inlet zone near reclaimable catalyst, catalyst concentration is bigger, and less in other regional inner catalyst concentration.This uneven distribution of catalyzer has reduced the contact effect of reaction oil gas with catalyzer, has influenced the twice transformation level of response of alkene.
Summary of the invention
The objective of the invention is to design on the basis of existing technology a kind of improved fluidization catalytic conversion reactor, so that the catalyst distribution in second reaction zone is even.
The improved fluidization catalytic conversion reactor constructional feature of the present invention's design is:
Reactor drum comprises second reaction zone that co-axial pre lift zone, first reaction zone, diameter have enlarged than first reaction zone from bottom to up successively along axis direction, and improvements are to lay grid distributor with holes in the space between first reaction zone and second reaction zone.
Space between said first reaction zone and second reaction zone can be near the truncated cone-shaped combining site that forms naturally between first reaction zone and second reaction zone, also a mixing zone can be set between first reaction zone and second reaction zone.Said mixing zone be shaped as cylinder or truncated cone-shaped tube, with the whole reactor coaxial arrangement, the inlet of mixing zone links to each other with the outlet of first reaction zone, the outlet of mixing zone links to each other with the inlet of second reaction zone, above-mentioned two connecting portions are truncated cone-shaped.The diameter ratio of the diameter of said mixing zone and first reaction zone is 1.0～2.0: 1, and the height of mixing zone is 0.1～0.8: 1 with the ratio of the height of first reaction zone.
The shape of said grid distributor with holes can be watch-glass, truncated cone-shaped tube, Polygons, but is not limited to these shapes.
Wherein watch-glass shape grid distributor is similar to the watch-glass to lower recess, is the big hole of an opening in the middle of the grid distributor, and its diameter is 0.5～1 times of the first reaction zone exit diameter; Several apertures around the grid distributor, the perforated area of aperture is 0.01～0.5 times of the first reaction zone outlet area.
The bottom of truncated cone-shaped tubular grid distributor is a macropore, and the diameter of bottom macropore is 0.5～1 times of first reaction zone diameter; The top also is a macropore, and the diameter of top macropore is 0.5～1 times of second reaction zone diameter.On such grid distributor sidewall, have some apertures, the perforated area of aperture is 0.5～1.2 times of the first reaction zone outlet area.
The Polygons grid distributor can be trilateral, tetragon or the five limits Polygons of above (comprising five limits), the wherein preferred rectangle of tetragon.On the Polygons grid distributor, have some apertures, perforated area is 0.5～1.5 times of the first reaction zone outlet area.The Polygons grid distributor tilts to be positioned in the mixing tank district, and the angle of the longitudinal axis of Polygons grid distributor and mixing zone is 10～170 °.In the mixing zone, place at least one Polygons grid distributor, preferably place 2-4 Polygons grid distributor.
The diameter ratio of the diameter of said second reaction zone and first reaction zone is that the ratio of height and the height of first reaction zone of 1.5～5.0: 1, the second reaction zone is 0.1～1.0: 1.
The outlet of second reaction zone of said reactor drum can link to each other with settling vessel through level pipe, also can be above the outlet of second reaction zone coaxial the outlet area that diameter has dwindled than second reaction zone be set, and the terminal level pipe that passes through of outlet area links to each other with settling vessel.The similar of said outlet area is in the equal diameter riser reactor top exit part of routine, and the diameter ratio of its diameter and first reaction zone is 0.8～1.5: 1.
Be provided with the catalyst inlet pipe in the bottom of pre lift zone, the combining site between the pre lift zone and first reaction zone is provided with raw material nozzles.
Other constitutional features of said reactor drum is referring to the Chinese patent CN1237477A of the applicant's application.
The raw oil that said reactor drum is suitable for is selected from the mixture of one or more (comprising two kinds) in oil hydrocarbon ils, other MO, the synthetic oil, wherein the mixture of one or more (comprise two kind) of petroleum hydrocarbon grease separation in gasoline, diesel oil, vacuum gas oil, coker gas oil, deasphalted oil, hydrogenation tail oil, long residuum, vacuum residuum, crude oil; Other MO is liquefied coal coil, tar sand oil, shale oil; Synthetic oil is that coal, Sweet natural gas or pitch are through the synthetic distillate that obtains of F-T.
Said reactor drum is suitable for all types of catalytic cracking catalysts; For example active ingredient is selected from the Y that contains or do not contain rare earth or HY type zeolite, the ultrastable Y that contains or do not contain rare earth, ZSM-5 series zeolite or the supersiliceous zeolite that makes with other method with five-membered ring structure in a kind of, two or three catalyzer, and amorphous silicon aluminium catalyzer.
Reactor drum of the present invention can be used to produce the technology of various objectives product, for example produces Trimethylmethane and the gasoline that is rich in isoparaffin; Produce an amount of propylene, Trimethylmethane and be rich in the gasoline of isoparaffin; Produce the gas alkene and the gasoline that is rich in aromatic hydrocarbons of maximum yield; Produce the diesel oil of maximum yield; Produce the Deep Catalytic Cracking process of propylene; Produce the catalytic pyrolysis technology of ethene etc.
The present invention improves existing fluidization catalytic conversion reactor; Between first reaction zone and second reaction zone, the mixing zone is set; And in mixing, lay grid distributor with holes, and make the catalyst distribution in second reaction zone even, help fully contacting of reaction oil gas and catalyzer.The quality product that the reactor drum that adopts the present invention to design can improve CCU distributes; Be embodied in transformation efficiency and improve, dry gas yied descends, light weight fluid (gasoline and solar oil) gain in yield; Olefin content in gasoline reduces, and the isoparaffin content in the gasoline increases.
Description of drawings
The improved fluidization catalytic conversion reactor structural representation that Fig. 1 designs for the present invention.
The vertical view of the watch-glass shape grid distributor that Fig. 2 designs for the present invention.
The side-view of the truncated cone-shaped tubular grid distributor that Fig. 3 designs for the present invention.
Fig. 4 is placed on the synoptic diagram in the mixing zone for the rectangular profile plate that the present invention designs.
Embodiment
Further specify below in conjunction with the improved fluidization catalytic conversion reactor structure of accompanying drawing the present invention's design.
The improved fluidization catalytic conversion reactor structural representation that Fig. 1 designs for the present invention.
The improved fluidization catalytic conversion reactor preferred construction of the present invention's design is following:
Be followed successively by from bottom to up along reactor drum longitudinal axis direction: pre lift zone 1, first reaction zone 2, mixing zone 3, second reaction zone 4, outlet area 5, the end of outlet area 5 links to each other with the settling vessel (not shown) through level pipe 6.Be provided with catalyst inlet pipe 7 in the bottom of pre lift zone 1, the combining site between the pre lift zone 1 and first reaction zone 2 is provided with raw material nozzles 8, and 3 bottom is provided with catalyst inlet pipe 9 in the mixing zone, in mixing zone 3, places grid distributor 10 with holes.
Use the fluidized catalytic process for transforming typical process of this reactor drum following:
Promote the bottom entering reactor drum of medium in advance from pre lift zone 1; The regenerated catalyst of heat gets into first reaction zone 2 through catalyst inlet pipe 7 from flowing into pre lift zone 1 and being moved upward by the castering action of preparatory lifting medium; Raw oil after the preheating and atomizing steam spray into first reaction zone 2 through raw material nozzles 8, contact and generation scission reaction on the regenerated catalyst of heat; From settling vessel or/and the reclaimable catalyst of stripper (not shown) is introduced in mixing zone 3 through catalyst inlet pipe 9.After mixing, cold shock agent or other reactant flow can carry out secondary reaction or work to reduce by second reaction zone temperature from the combining site injecting reactor (not shown) between the mixing zone 3 and second reaction zone 4; The end reaction oil gas product of reactor drum and reclaimable catalyst get into follow-up settling vessel, stripper, catalyst regeneration system and product fractionation stabilization system (not shown) by level pipe 6 after outlet area 5 quickens.
As previously mentioned, except the external geometrical dimension of mixing zone, its built-in distributing plate structure also is an important factor that influences catalyzer uniform distribution situation.The structure of grid distributor has a variety of, and Fig. 2～Fig. 4 has just listed employed three kinds of distributing plate structures among the present invention, but they do not limit the present invention.
The vertical view of the watch-glass shape grid distributor that Fig. 2 designs for the present invention.
The side-view of the truncated cone-shaped tubular grid distributor that Fig. 3 designs for the present invention.
Fig. 4 is placed on the synoptic diagram in the mixing zone for the rectangular profile plate that the present invention designs.
Following embodiment will further specify the present invention, but therefore not limit the present invention.
The character of employed fcc raw material oil and catalyzer is listed in table 1 and table 2 respectively in embodiment and the Comparative Examples.Catalyzer in the table 2 is produced by catalyzer branch office of Sinopec Group Shandong catalyst plant.
Embodiment 1
The present embodiment explanation is on the riser reactor of the medium-sized voluminous isoparaffin catalytic cracking process that the mixing zone is installed, and the process condition of isoparaffin gasoline is rich in raw oil production in the catalyzer processing table 1 in the use table 2.
The pre lift zone of reactor drum, first reaction zone, mixing zone, second reaction zone and outlet area total height are 16 meters, and wherein the pre lift zone diameter is 0.25 meter, highly are 1.5 meters; First reaction zone diameter is 0.25 meter, highly is 4 meters; The mixing zone diameter is 0.50 meter, highly is 1 meter; Second reaction zone diameter is 1 meter, highly is 6.5 meters; The outlet area diameter is 0.25 meter, highly is 3 meters; The side line of the longitudinal section isosceles trapezoid of first reaction zone and mixing zone combining site and the angle of axis are 30 °; The side line of the longitudinal section isosceles trapezoid of the mixing zone and the second reaction zone combining site and the angle of axis are 45 °, and the side line of the longitudinal section isosceles trapezoid of second reaction zone and outlet area combining site and the angle of axis are 60 °.The built-in grid distributor in mixing zone adopts watch-glass shape and structure shown in Figure 2, is the big hole of an opening in the middle of the grid distributor, and its diameter is 0.8 times of the first reaction zone exit diameter; Several apertures around the grid distributor, the perforated area of aperture is 0.45 times of the first reaction zone outlet area.
Operational condition, product distribute and the gasoline main character is listed in table 3.
Compare with embodiment 1, the grid distributor of present embodiment in the mixing zone, the second reaction zone conditions difference, all the other are all identical with embodiment 1.The built-in grid distributor in present embodiment mixing zone adopts truncated cone-shaped tubular structure shown in Figure 3, and the diameter of grid distributor bottom macropore is 0.8 times of first reaction zone diameter; The top also is a macropore, and the diameter of top macropore is 0.8 times of second reaction zone diameter.On such grid distributor sidewall, have some apertures, the perforated area of aperture is 0.8 times of the first reaction zone outlet area.
Operational condition, product distribute and the gasoline main character is listed in table 3.
Compare with embodiment 1, the grid distributor of present embodiment in the mixing zone, the second reaction zone conditions difference, all the other are all identical with embodiment 1.Built-in 2 the rectangular profile plates shown in Figure 4 in present embodiment mixing zone, the perforated area of each grid distributor is 0.6 times of the first reaction zone outlet area.The rectangular profile plate tilts to be positioned in the mixing tank district, and the angle of the longitudinal axis of rectangular profile plate and mixing zone is 60 °.
Operational condition, product distribute and the gasoline main character is listed in table 3.
Comparative Examples
The explanation of this Comparative Examples is on the riser reactor of the medium-sized voluminous isoparaffin catalytic cracking process of routine, and the process condition of isoparaffin gasoline is rich in raw oil production in the catalyzer processing table 1 in the use table 2.Compare with embodiment 1, this Comparative Examples does not have the mixing zone distribution-free plate, the second reaction zone conditions difference except that reactor drum yet, and all the other are all identical with embodiment 1.
The pre lift zone of reactor drum, first reaction zone, mixing zone, second reaction zone and outlet area total height are 15 meters, and wherein the pre lift zone diameter is 0.25 meter, highly are 1.5 meters; First reaction zone diameter is 0.25 meter, highly is 4 meters; Second reaction zone diameter is 1 meter, highly is 6.5 meters; The outlet area diameter is 0.25 meter, highly is 3 meters; The side line of the longitudinal section isosceles trapezoid of first reaction zone and the second reaction zone combining site and the angle of axis are 45 °, and the side line of the longitudinal section isosceles trapezoid of second reaction zone and outlet area combining site and the angle of axis are 60 °.
Operational condition, product distribute and the gasoline main character is listed in table 3.
Can find out that from table 3 the Trimethylmethane productive rate in the liquefied gas of embodiment 1-3 all is higher than Comparative Examples, light weight fluid (gasoline and solar oil) productive rate all is higher than Comparative Examples, and dry gas yied all is lower than Comparative Examples; Olefin content in gasoline all is lower than Comparative Examples, and the isoparaffin content in the gasoline all is higher than Comparative Examples.
Table 1
| Raw oil character | Numerical value |
| Density (20 ℃), kilogram/rice 3 | 890.5 |
| Kinematic viscosity, millimeter 2/ second | |
| 80℃ | 7.93 |
| 100℃ | 5.08 |
| Carbon residue, heavy % | 0.70 |
| Condensation point, ℃ | 40 |
| Total nitrogen, heavy % | 0.16 |
| Sulphur, heavy % | 0.53 |
| Carbon, heavy % | 85.00 |
| Hydrogen, heavy % | 12.62 |
| Heavy metal content, μ g/g | |
| Nickel | 0.16 |
| Vanadium | 0.15 |
| Iron | - |
| Copper | - |
| Sodium | 0.45 |
| Boiling range, ℃ | |
| Over point | 278 |
| 10％ | 385 |
| 30％ | 442 |
| 50％ | 499 |
| 70％ | - |
| 90％ | - |
| Final boiling point | - |
Table 2
| Trade names | ZCM-7 |
| Zeolite type | USY |
| Chemical constitution, heavy % | |
| Aluminum oxide | 46.4 |
| Sodium oxide | 0.22 |
| Red stone | 0.32 |
| Apparent density, kilogram/rice 3 | 690 |
| Pore volume, milliliter/gram | 0.38 |
| Specific surface area, rice 2/ gram | 164 |
| Abrasion index, %/hour | - |
| Size composition, heavy % | |
| 0～40 micron | 4.8 |
| 40～80 microns | 47.9 |
| ＞80 microns | 47.3 |
Table 3
| Embodiment 1 | |
|
Comparative Examples | |
| Structure of reactor | The mixing zone is arranged | The mixing zone is arranged | The mixing zone is arranged | No mixing zone |
| The grid distributor shape | Watch-glass | The truncated cone-shaped tube | Rectangle | The distribution-free plate |
| Processing condition | ||||
| Temperature of reaction, ℃ | ||||
| First reaction zone | 545 | 545 | 545 | 545 |
| Second reaction zone | 485 | 488 | 491 | 495 |
| Reaction times, second | 6.2 | 5.8 | 5.4 | 5.0 |
| First reaction zone | 1.0 | 1.0 | 1.0 | 1.0 |
| Second reaction zone | 4.7 | 4.3 | 3.9 | 3.5 |
| Outlet area | 0.5 | 0.5 | 0.5 | 0.5 |
| Agent-oil ratio | 4.5 | 4.5 | 4.5 | 4.5 |
| WOR | 0.05 | 0.05 | 0.05 | 0.05 |
| Product distributes, heavy % | ||||
| Dry gas | 1.52 | 1.61 | 1.73 | 1.83 |
| Liquefied gas | 17.44 | 17.12 | 16.58 | 16.11 |
| Trimethylmethane | 5.98 | 5.71 | 5.77 | 5.65 |
| Gasoline | 48.88 | 48.06 | 47.64 | 46.86 |
| Solar oil | 24.32 | 24.11 | 23.69 | 23.44 |
| Heavy gas oil | 3.29 | 4.82 | 6.32 | 7.77 |
| Coke | 4.13 | 4.08 | 3.96 | 3.88 |
| Loss | 0.42 | 0.20 | 0.08 | 0.11 |
| Gasoline is formed, heavy % | ||||
| Aromatic hydrocarbons | 23.06 | 22.34 | 32.56 | 23.60 |
| Alkene | 23.93 | 22.60 | 16.14 | 25.17 |
| Alkane | 44.01 | 46.03 | 41.99 | 42.97 |
| Normal paraffin | 7.6 | 9.14 | 4.02 | 7.12 |
| Isoparaffin | 36.41 | 36.89 | 37.97 | 35.85 |
| Naphthenic hydrocarbon | 9.00 | 9.03 | 9.31 | 8.26 |
| The octane value of gasoline | ||||
| RON | 87.4 | 87.3 | 90.8 | 88.2 |
| MON | 78.1 | 77.7 | 79.8 | 78.0 |
Claims (12)
1. improved fluidization catalytic conversion reactor; This reactor drum comprises successively from bottom to up that along axis direction co-axial pre lift zone, first reaction zone, diameter than second reaction zone that first reaction zone has enlarged, is characterized in that laying grid distributor with holes in the space between first reaction zone and second reaction zone.
2. according to the reactor drum of claim 1, it is characterized in that the space between said first reaction zone and second reaction zone is the mixing zone.
3. according to the reactor drum of claim 2; What it is characterized in that said mixing zone is shaped as cylinder or truncated cone-shaped tube, and with the whole reactor coaxial arrangement, the inlet of mixing zone links to each other with the outlet of first reaction zone; The outlet of mixing zone links to each other with the inlet of second reaction zone; Above-mentioned two connecting portions are truncated cone-shaped, and the diameter ratio of the diameter of said mixing zone and first reaction zone is 1.0～2.0: 1, and the height of mixing zone is 0.1～0.8: 1 with the ratio of the height of first reaction zone.
4. according to the reactor drum of claim 1, it is characterized in that in the middle of the said grid distributor be the big hole of an opening, its diameter is 0.5～1 times of the first reaction zone exit diameter; Several apertures around the grid distributor, the perforated area of aperture is 0.01～0.5 times of the first reaction zone outlet area.
5. according to the reactor drum of claim 1, the bottom that it is characterized in that said grid distributor is a macropore, and the diameter of bottom macropore is 0.5～1 times of first reaction zone diameter; The top also is a macropore, and the diameter of top macropore is 0.5～1 times of second reaction zone diameter, on such grid distributor sidewall, has some apertures, and the perforated area of aperture is 0.5～1.2 times of the first reaction zone outlet area.
6. according to the reactor drum of claim 1; It is characterized in that said grid distributor is the above Polygons in trilateral, tetragon or five limits; On the Polygons grid distributor, have some apertures, perforated area is 0.5～1.5 times of the first reaction zone outlet area, and the Polygons grid distributor tilts to be positioned in the mixing tank district; The angle of the longitudinal axis of Polygons grid distributor and mixing zone is 10～170 °, in the mixing zone, places at least one Polygons grid distributor.
7. according to the reactor drum of claim 6, it is characterized in that said tetragon grid distributor is the rectangular profile plate, in the mixing zone, place 2-4 grid distributor.
8. according to the reactor drum of claim 1, the diameter ratio that it is characterized in that diameter and first reaction zone of said second reaction zone is that the ratio of height and the height of first reaction zone of 1.5～5.0: 1, the second reaction zone is 0.1～1.0: 1.
9. according to the reactor drum of claim 1, it is characterized in that second reaction zone outlet of this reactor drum links to each other with settling vessel through level pipe.
10. according to the reactor drum of claim 1, it is characterized in that this reactor drum is coaxial above the outlet of second reaction zone outlet area that diameter has dwindled than second reaction zone is set that outlet area is terminal links to each other with settling vessel through level pipe.
11. according to the reactor drum of claim 1, it is characterized in that being provided with the catalyst inlet pipe in the bottom of pre lift zone, the combining site between the pre lift zone and first reaction zone is provided with raw material nozzles.
12., it is characterized in that the diameter of said outlet area and the diameter ratio of first reaction zone are 0.8～1.5: 1 according to the reactor drum of claim 10.
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| CN2006101695126A CN101205476B (en) | 2006-12-22 | 2006-12-22 | Modified fluidization catalytic conversion reactor |
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| CN101205476B true CN101205476B (en) | 2012-07-18 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| WO2012041007A1 (en) * | 2010-09-27 | 2012-04-05 | 中国石油化工股份有限公司 | Catalytic conversion method for improving product distribution |
| CN102690675B (en) * | 2012-05-24 | 2015-05-06 | 中国石油天然气股份有限公司 | Catalytic cracking pre-raiser with cold and hot catalyst rapid mixing function |
| CN102827629B (en) * | 2012-08-30 | 2014-11-05 | 中国石油大学(华东) | Catalytic cracking reaction device fed with combination of light raw materials and heavy oil |
| CN105289140B (en) * | 2015-11-24 | 2017-05-24 | 张家港市艾尔环保工程有限公司 | Pneumatic conveyor with ceramic air flow distribution plates |
| CN112569875A (en) * | 2019-09-30 | 2021-03-30 | 中国石油化工股份有限公司 | Reducing fluidized bed reactor |
| CN113926394A (en) * | 2020-06-29 | 2022-01-14 | 中国石油化工股份有限公司 | Aromatization reactor and method for producing aromatic hydrocarbon |
| CN118272118A (en) * | 2022-12-30 | 2024-07-02 | 中国石油天然气股份有限公司 | Heavy oil catalytic device and method |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5851380A (en) * | 1996-08-01 | 1998-12-22 | Phillips Petroleum Company | Process and apparatus for fluidized catalytic cracking of a hydrocarbon feed |
| CN1657150A (en) * | 2004-12-16 | 2005-08-24 | 中国石油化工集团公司 | Riser reactor for hydrocarbon fluidized catalytic conversion |
-
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- 2006-12-22 CN CN2006101695126A patent/CN101205476B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5851380A (en) * | 1996-08-01 | 1998-12-22 | Phillips Petroleum Company | Process and apparatus for fluidized catalytic cracking of a hydrocarbon feed |
| CN1657150A (en) * | 2004-12-16 | 2005-08-24 | 中国石油化工集团公司 | Riser reactor for hydrocarbon fluidized catalytic conversion |
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