CN1191322C - Improved catalytic racking stripper - Google Patents
Improved catalytic racking stripper Download PDFInfo
- Publication number
- CN1191322C CN1191322C CNB011154888A CN01115488A CN1191322C CN 1191322 C CN1191322 C CN 1191322C CN B011154888 A CNB011154888 A CN B011154888A CN 01115488 A CN01115488 A CN 01115488A CN 1191322 C CN1191322 C CN 1191322C
- Authority
- CN
- China
- Prior art keywords
- stripper
- reaction zone
- stripping
- distributor
- lighter hydrocarbons
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to an improved catalytic cracking stripper composed of an upper reaction region and a lower stripping region, wherein a light hydrocarbon feeding distributor and a steam distributor forming a concave surface shape are coaxially arranged in the upper reaction region from top to bottom. The stripper can improve the quality of light petroleum products and obtain ideal stripping effects.
Description
Technical field
The invention belongs to the catalyticing conversioning equipment of petroleum hydrocarbon under the situation that does not have hydrogen, more particularly, is a kind of improved FCC stripper that has the hydrocarbon oil conversion function concurrently.
Background technology
Catalytic cracking is one of main heavy oil lighting process of oil refining enterprise, can make macromolecular heavy petroleum hydrocarbon be cracked into micromolecular high price petroleum products on thermocatalyst by this process.Its key step is as follows: hydrocarbon raw material contacts with the regenerated catalyst of heat and carry out catalytic cracking reaction under 460～560 ℃; The mixture of reaction oil gas and reclaimable catalyst enters settling vessel by riser reactor; In settling vessel, oil gas and reclaimable catalyst are separated; Oil gas enters follow-up fractionating system; Reclaimable catalyst contacts with steam counter-flow in stripper, removes the hydrocarbons of being carried secretly; Catalyst transport behind the stripping is used oxygen-containing gas in revivifier, be generally air, and coke burning regeneration under 600～800 ℃ high temperature makes catalyzer recover active; Catalyzer after the regeneration returns riser reactor and recycles; Flue gas enters atmosphere after treatment.
Along with the change day by day of crude oil is heavy, the yield of light oil of petroleum refining industry's time processing process descends, and catalytic cracking unit is faced with the insufficient problem of stock oil.For this reason, catalytic cracking unit just needs processing more residual oil, wax tailings and diasphaltene wet goods heavy feed stock.And the content of the carbon residue of these raw materials, heavy metal and sulphur and nitrogen is all very high, will inevitably bring a series of influence to the normal running of catalytic cracking unit, for example, environmental issue, corrosion of equipment problem, the serious inactivation of catalyzer, product distribution variation, quality product descend or the like.And the Srteam Stripping effect of improving reclaimable catalyst is an effective way alleviating the problems referred to above.But good stripping will increase strip, hydrocarbons the rate of recovery, remove the hydrogenous petroleum hydrocarbon of more richness from reclaimable catalyst, thereby can reduce regeneration temperature, alleviate the hydrothermal deactivation of catalyzer in revivifier; Good stripping can also be removed sulphur, the nitrogen compound that adsorbs on the reclaimable catalyst, thereby reduces the discharging of sulfur oxide, nitrogen oxide in the regenerated flue gas.
USP5,128,109 have disclosed a kind of two sections steam stripped methods.This method is that two sections strippers are set between reactor and revivifier, and regenerated catalyst that one is hot is introduced in first section of stripper, mixes with spent agent, to improve the temperature of spent agent in this section; Adopt steam as the stripping medium, make itself and catalyzer counter current contact; The indirect heat exchanger of a bundled tube is set in second section of stripper, is used to remove a part of heat; Suitably the spent agent after the cooling is delivered to the revivifier coke burning regeneration.
USP5,538,623 disclose a kind of gas stripping process with steam cycle.This method utilizes airtight cyclonic separator that reaction oil gas and stripping medium are separated, and reaction oil gas is directly introduced subsequent separation system, and stripping media such as hydrogen or steam recycle after cooling, condensation.Because stripping medium and reaction oil gas are isolated fully, thus allow in stripping process, to use a large amount of stripping media, thus optimize the operation of stripper, improve Srteam Stripping effect.
USP5,601,787 disclose a kind of hot stripper of multistage that is used for the coaxial fluid catalytic cracking device.Compare with conventional stripper, this stripper also is provided with second stripper below conventional stripper, and by this stripper being immersed revivifier dense-phase bed or by carrying out heat exchange with the dilute phase transport riser tube or by directly adding the methods such as regenerated catalyst of heat, to improve the temperature of the reclaimable catalyst in the stripper, improve Srteam Stripping effect.
In sum, although all obtained bigger progress,, it technical scheme that possesses stripping and hydrocarbon oil conversion dual-use function is not appeared in the newspapers by transforming stripper at the gas stripping process of catalyzer and the configuration aspects of stripper.
Summary of the invention
The object of the present invention is to provide a kind of improved FCC stripper with stripping and hydrocarbon oil conversion dual-use function.
FCC stripper from top to down provided by the invention is made of reaction zone and stripping zone two portions; The inner from top to down of reaction zone is provided with co-axial lighter hydrocarbons feed distributor and concave shape steam distributor.
Compared with prior art, FCC stripper provided by the present invention mainly has the characteristics of the following aspects:
1. the stripper that has the hydrocarbon oil conversion function concurrently provided by the present invention is easy to implement on catalytic cracking unit.No matter be to build new device, still original catalytic cracking unit is transformed, only need less construction investment or plant modification expense, can be so that original stripper have reaction and steam stripped dual-use function, for the upgrading of light petroleum hydrocarbon creates favorable conditions.
2. stripper provided by the present invention can make full use of the remaining activity on the reclaimable catalyst.As everyone knows, in catalytic cracking process,, but still remain with a considerable amount of active centre though the activity of reclaimable catalyst is lower.Stripper provided by the invention makes light petroleum hydrocarbon contact with reclaimable catalyst by light petroleum hydrocarbon being injected the reaction zone of stripper, carries out secondary reactions such as hydrogen transference, isomerization, thereby improves the quality of petroleum products.
3. stripper provided by the invention can obtain the better Srteam Stripping effect of more conventional stripper.Because the design of stripping zone is identical with conventional catalytic cracking stripping zone among the present invention, therefore, can pass through to adjust the flow of stripped vapor, the mass rate of catalyzer fully, and prolong measures such as the residence time acquisition good Srteam Stripping effect of catalyzer at stripping zone.
Description of drawings
Fig. 1 is the structural representation that the invention provides stripper.
Fig. 2 is the structural representation of lighter hydrocarbons feed distributor and concave shape steam distributor.
Embodiment
Stripper provided by the present invention is divided into two portions, and top is reaction zone, and the bottom is a stripping zone, and reaction zone and stripping zone are coaxial.The height of reaction zone generally accounts for 1/5～4/5 of stripper total height, and the height of stripping zone generally accounts for 1/5～4/5 of stripper total height.The diameter of reaction zone and stripping zone can determine that respectively the diameter of the two can equate, also can not wait according to the mass flow of device.
In stripper provided by the present invention, the inner from top to down of reaction zone is provided with co-axial lighter hydrocarbons feed distributor and concave shape steam distributor.If as starting point, the height of reaction zone is defined as 100% with the upper end of reaction zone, then lighter hydrocarbons feed distributor and concave shape steam distributor should be positioned at 20～80% places of reaction zone height, preferably are positioned at 30～70% places.
The concrete structure of described lighter hydrocarbons feed distributor is as follows: the blind pipe that in one plane intersects mutually and connect more than two or two constitutes the main body of this sparger; One is positioned at lighter hydrocarbons ingress pipe on the reaction zone central axis perpendicular to the plane at above-mentioned blind pipe place, and welds together with each blind pipe with being interconnected; The best symmetric arrangement of each blind pipe, the length of blind pipe are 10%～80%, preferred 20%～70% of stripper reaction zone internal diameter; Downside at every blind pipe is provided with the lighter hydrocarbons nozzle; The lighter hydrocarbons nozzle is tilted to down, with the angle of horizontal direction be 20～60 °; The diameter of lighter hydrocarbons nozzle is 0.5～4.0cm, preferred 1.0～3.0cm; Its length is 1.0～4.0cm; The lighter hydrocarbons nozzle is connected with blind pipe, and welds together with blind pipe; The lighter hydrocarbons nozzle should be arranged in the downside of blind pipe as far as possible equably, so that lighter hydrocarbons are distributed on the cross section at lighter hydrocarbons feed distributor place as far as possible equably; The number of lighter hydrocarbons nozzle is controlled at 10～50m/s with the linear speed of lighter hydrocarbons by nozzle and is advisable.
The concrete structure of described concave shape steam distributor is as follows: the profile of this sparger is similar to bowl-type, and its maximum diameter is 1: 1.2～5 with the ratio of stripper reaction zone internal diameter, and preferred 1: 1.2～4; The upside of this sparger is slick arc-shaped concave, and downside is the arc convex of even perforate; The aperture of side hole is 0.5～4.0cm under the steam distributor, and preferred 1.0～2.5cm, perforated area are that 20～60m/s determines preferred 20～50m/s according to the linear speed of steam by aperture.The outside of above-mentioned aperture all is welded with the short tube that length is 1.0～5.0cm, and the internal diameter of short tube is the internal diameter of aperture.Form the cavity of a bowl-type between the upside of this sparger and the downside, and the downside central position of this cavity is connected with vapour line.
Stripping zone is positioned at the bottom of above-mentioned reaction zone.In order to strengthen Srteam Stripping effect, be provided with 10～20 layers of chev(e)ron baffle in the stripping zone, its method to set up is same as the prior art.Stripped vapor can be sprayed into by the pipe that inserts under bottom 2～3 layers of herringbone baffle plate, also stripped vapor can be divided into multiply, injects the different position of stripping zone respectively.
Stripper provided by the present invention is operated in the following manner:
Come reaction oil gas and mixture of catalysts sharp separation in settling vessel of autoreactor, reaction oil gas is sent into through gas pipeline and is carried out product separation in the follow-up fractionating system, long-pending have the catalyzer of a certain amount of coke to move downward, and at first enters in the reaction zone of stripper.Light petroleum hydrocarbon, for example, catalytic cracking raw gasline, coker gasoline, straight-run spirit, coker gas oil, viscosity breaking diesel oil, liquefied gas, dry gas etc. inject the reaction zone beds through the lighter hydrocarbons feed distributor, contact with catalyzer and react.The injection rate of light petroleum hydrocarbon is so that the density of reaction zone catalyzer dense-phase bed is controlled at 150～500Kg/m
3Be advisable.Temperature of reaction is 400～550 ℃, preferred 420～530 ℃; Agent-oil ratio is 4～20, preferred 6～18; Weight hourly space velocity is 1～50h
-1, preferred 10～30h
-1
A certain amount of steam enters in the cavity of concave shape steam distributor through pipeline, and by in the perforate injecting catalyst dense-phase bed of this sparger downside, the catalyzer in the reaction zone is carried out preliminary stripping.Reaction oil gas and mixture of steam upwards flow, and send into follow-up fractionating system through settling vessel, cyclonic separator, gas pipeline.The quantity of steam that injects reaction zone is about the 10～60V% that injects the stripping zone quantity of steam, preferred 20～40V%.
Catalyzer in the above-mentioned reaction zone moves downward, and enters the stripping zone of bottom.Water vapor is injected by the bottom of stripping zone, and with reacted catalyzer counter current contact, stripping is clean as much as possible with the residual reaction oil gas between the granules of catalyst and catalyst pores inside.The bottom of this stripping zone links to each other with catalyzer pipeline to be generated, and the catalyzer behind the stripping is sent into coke burning regeneration in the revivifier through pipeline to be generated, recovers active catalyzer after the regeneration again and delivers to the reactor cycles use.
FCC stripper provided by the present invention does not have special requirement to the catalyzer that is adopted, any catalyzer of catalytic cracking unit that is applicable to can use in this stripper, for example, the activity of such catalysts component can be selected from one or more in y-type zeolite, HY type zeolite, USY type zeolite, the ZSM-5 series zeolite that contains or do not contain rare earth or the supersiliceous zeolite with five-membered ring structure, β zeolite, the ferrierite, also can be the amorphous silicon aluminium catalyzer.
Further describe stripper provided by the present invention below in conjunction with accompanying drawing, but therefore do not limit the present invention.
As shown in Figure 1, heavy petroleum hydrocarbon contacts with high-temperature regenerated catalyst from revivifier 11 in feed nozzle 1 injecting lift pipe reactor 2, instant vaporization and reaction.Reaction oil gas and mixture of catalysts be along being advanced on the riser tube in the settling vessel 8, reaction oil gas and catalyzer sharp separation, and reaction oil gas is sent into follow-up system through cyclonic separator 6 and gas pipeline 7.
Reacted catalyzer falls into the top reaction zone 10 of stripper 9, and forms the catalyzer dense-phase bed at reaction zone.Lighter hydrocarbons feed distributor 14 and concave shape steam distributor 15 coaxial being arranged in the reaction zone, light petroleum hydrocarbon enters in the lighter hydrocarbons feed distributor through pipeline, and uniform distribution radially, contacts, reacts with catalyzer in the reaction zone.
Above-mentioned catalyzer flows downward gradually, falls on the upside concave surface of concave shape steam distributor 15, goes out along the concave surface peripheral overflow then.Steam enters the concave shape steam distributor through pipeline, and by side hole ejection under this sparger, the annular space between concave shape steam distributor and stripper upwards flows then, and the catalyzer in the reaction zone is carried out preliminary stripping.The mixture of water vapor and reaction oil gas upwards flows, and enters follow-up system through settling vessel, gas pipeline.Catalyzer in the reaction zone continues to flow downward and enters stripping zone 12, and stripped vapor is introduced through pipeline 18, and catalyzer contacts with steam counter-flow once more at stripping zone, and as much as possible that catalyzer is entrained reaction oil gas stripping is clean.
Catalyzer behind the stripping enters in the revivifier 11 through regeneration standpipe 13, and coke burning regeneration under the effect of oxygen-containing gas is recovered activity of such catalysts.Regenerated flue gas is discharged through cyclonic separator 4 and flue gas pipeline 5, and the catalyzer after the regeneration is delivered to the use of riser reactor bottom cycle.
The following examples will be further specified the present invention, but not thereby limiting the invention.Employed catalyzer is the production of Qilu Petrochemical company catalyst plant among the embodiment, and trade names are MLC-500, and its character is listed in table 1.The raw material oil properties is listed in table 2.
Embodiment
Present embodiment is the application result of stripper provided by the present invention on catalytic cracking unit.
The treatment capacity of testing used catalytic cracking unit is 1,400,000 t/a, and the external diameter of its stripper is 3560mm, is 8200mm highly, and is provided with upper and lower two-layer water stripping steam inlet.In order to implement the present invention, this is installed original stripper transform.After the transformation, the external diameter of stripper still is 3560mm, and total height is 9700mm.Wherein, the height of reaction zone is 2000mm, and the height of stripping zone is 7700mm, and concrete structure is referring to Fig. 1 and Fig. 2.
As depicted in figs. 1 and 2, lighter hydrocarbons feed distributor and concave shape steam distributor are arranged on the reaction zone central axis, and the lighter hydrocarbons feed distributor is positioned at 60% place of reaction zone height, are made of two blind pipes vertical mutually and that connect, the blind pipe diameter is 150mm, and long is 1000mm.The downside of blind pipe is provided with the lighter hydrocarbons nozzle, and its internal diameter is 12mm, and lighter hydrocarbons are 45m/s by the linear speed of nozzle.The concave shape steam distributor is positioned at 80% place of reaction zone height, and its maximum diameter is 1600mm, the even perforate of downside arc convex, the aperture is 20mm, and the perforate outside is welded with the long short tube of 25mm, and the short tube internal diameter is identical with the aperture, and steam is 40m/s by the linear speed of above-mentioned perforate.The quantity of steam that injects in the reaction zone by this concave shape steam distributor is the 30V% that injects the stripping zone quantity of steam.The total quantity of steam that injects stripper is 5.25t/h.
Testing sequence is as follows: the heavy petroleum hydrocarbon injecting lift pipe reactor after the preheating, contact with thermocatalyst and react, reaction product and reclaimable catalyst enter settling vessel and carry out gas solid separation, reaction oil gas is sent into subsequent separation system, further be separated into various products, wherein, the character of gasoline products is listed in table 2.Part gasoline products (its mass rate accounts for 10 heavy % of heavy petroleum hydrocarbon mass rate) injects the reaction zone of stripper through the lighter hydrocarbons feed distributor, contact with the long-pending catalyzer that a certain amount of coke arranged and react, be advanced into settling vessel on the reaction oil gas that is generated, after converging with oil gas, enter subsequent separation system from riser reactor.And reacted catalyzer is descending, behind the preliminary stripping of concave shape steam distributor, enters stripping zone stripping once more.Catalyzer behind the stripping is sent into the revivifier coke burning regeneration, and the catalyzer after the regeneration returns riser reactor and recycles.
Main operational condition, product distribute and the character of gasoline products sees Table 3.
Comparative Examples
This Comparative Examples is to overlap on the catalytic cracking unit with conventional stripper one to test.The stock oil identical with embodiment, catalyzer and essentially identical operational condition have been adopted in this test.
Testing sequence is as follows: in the heavy petroleum hydrocarbon injecting lift pipe reactor after the preheating, contact with thermocatalyst and react, reaction oil gas and mixture of catalysts enter settling vessel and carry out gas solid separation, and reaction oil gas is further isolated products such as dry gas, liquefied gas, gasoline and diesel oil by subsequent separation system; There is the catalyzer of a certain amount of coke in stripper, to carry out the water vapor stripping and amassed after the reaction; Catalyzer behind the stripping enters the revivifier coke burning regeneration, and the catalyzer after the regeneration returns riser reactor and recycles.
Main operational condition, product distribute and the character of the gasoline products that generated sees Table 3.
Product distributed data and the Comparative Examples of embodiment in the table 3 are compared as can be seen, because the reaction zone of part gasoline products injection stripper is carried out the catalytic reforming reaction, the productive rate of gasoline products slightly descends than Comparative Examples among the embodiment; But form data as can be seen by hydrocarbon system, the olefin(e) centent of its gasoline products reduces significantly, and the content of isoparaffin and aromatic hydrocarbons increases, and the quality of gasoline improves.In addition, by hydrogen richness among Jiao as can be seen, hydrogen richness slightly descends than Comparative Examples among Jiao of embodiment, illustrates that the Srteam Stripping effect of embodiment is better than Comparative Examples.
Table 1
| Catalyzer | MLC-500 (compound) |
| Chemical constitution, heavy % | |
| Aluminum oxide | 48.5 |
| Sodium oxide | 0.35 |
| Ferric oxide | / |
| Apparent density, kilogram/rice 3 | 690 |
| Pore volume, milliliter/gram | 0.40 |
| Specific surface area, rice 2/ gram | 298 |
| Abrasion index is when weighing % -1 | 2.3 |
| Size composition, heavy % | |
| 0～40 micron | 17.4 |
| 40～80 microns | 44.1 |
| ＞80 microns | 38.5 |
| The hydrothermal aging condition | 800 ℃, 17 hours, 100% water vapor |
| Micro-activity | 66 |
Table 2
| Stock oil | Heavy petroleum hydrocarbon | Catalytic gasoline |
| Density (20 ℃), g/cm 3 | 0.9198 | 0.7359 |
| Carbon residue, heavy % | 2.98 | / |
| Boiling range, ℃ | ||
| Initial boiling point/10% | / | 50/77 |
| 30％/50％ | / | 103/125 |
| 70％/90％ | / | 146/171 |
| Do | / | 199 |
| Gasoline octane rating | ||
| MON/RON | / | 78.5/90.1 |
Table 3
| Operational condition and product distribute | Embodiment | Comparative Examples |
| Riser reactor operational condition: temperature of reaction, ℃ agent-oil ratio reaction times, second | 500 6.5 3.2 | 500 6.5 3.2 |
| Stripper reaction zone operational condition: temperature of reaction, ℃ agent-oil ratio weight hourly space velocity, h -1 | 480 16 10 | / / / |
| Product distributes, heavy % dry gas liquefied gas gasoline, diesel heavy oil coke | 3.92 15.84 39.77 27.64 6.10 6.73 | 3.88 14.48 41.06 26.48 7.00 7.10 |
| Hydrogen richness in the coke, heavy % | 7.8 | 8.1 |
| The gasoline hydrocarbon group composition, heavy % normal paraffin isoparaffin naphthenic hydrocarbon alkene aromatic hydrocarbons | 5.3 33.8 7.2 26.1 27.6 | 5.8 25.9 8.3 42.1 17.9 |
| Gasoline octane rating RON MON | 90.2 80.1 | 90.1 78.5 |
Claims (5)
1, a kind of improved FCC stripper is characterized in that this stripper is made of top reaction zone and bottom stripping zone, and from top to down is provided with co-axial lighter hydrocarbons feed distributor and concave shape steam distributor in the reaction zone; Described reaction zone and stripping zone are coaxial, and the diameter of the two is identical or inequality; The height of reaction zone accounts for 1/5～4/5 of stripper total height, and the height of stripping zone accounts for 1/5～4/5 of stripper total height; Described lighter hydrocarbons feed distributor and concave shape steam distributor are positioned at 20～80% places of reaction zone height, with the upper end of reaction zone as starting point.
2, according to the stripper of claim 1, it is characterized in that described lighter hydrocarbons feed distributor and concave shape steam distributor are positioned at 30～70% places of reaction zone height, with the upper end of reaction zone as starting point.
3, according to the stripper of claim 1, it is characterized in that described lighter hydrocarbons feed distributor is made of the blind pipe that in one plane intersects mutually and connect more than two or two, one is positioned at lighter hydrocarbons ingress pipe on the reaction zone central axis perpendicular to the plane at above-mentioned blind pipe place, and welds together with each blind pipe with being interconnected; The length of blind pipe is 10%～80% of stripper reaction zone internal diameter; Downside at every blind pipe tilts the lighter hydrocarbons feed nozzle down is set, and the angle of described nozzle and horizontal direction is 20～60 °, and diameter is 0.5～4.0cm, and length is 1.0～4.0cm; Described nozzle is connected with blind pipe, and welds together with blind pipe.
4, according to the stripper of claim 1, the maximum diameter that it is characterized in that described concave shape steam distributor is 1: 1.2～5 with the ratio of stripper reaction zone internal diameter; The upside of this sparger is an arc-shaped concave, and downside is the arc convex of even perforate; The aperture of side hole is 0.5～4.0cm under the steam distributor, and the outside of perforate is welded with the short tube that length is 1.0～5.0cm, and the internal diameter of short tube is identical with the aperture of perforate; Form the cavity of a bowl-type between the upside of this sparger and the downside, the downside central position of this cavity is connected with vapour line.
5, according to the stripper of claim 4, the maximum diameter that it is characterized in that described concave shape steam distributor is 1: 1.2～4 with the ratio of stripper reaction zone internal diameter; The aperture of side hole is 1.0～2.5cm under the steam distributor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011154888A CN1191322C (en) | 2001-04-28 | 2001-04-28 | Improved catalytic racking stripper |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011154888A CN1191322C (en) | 2001-04-28 | 2001-04-28 | Improved catalytic racking stripper |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1382764A CN1382764A (en) | 2002-12-04 |
| CN1191322C true CN1191322C (en) | 2005-03-02 |
Family
ID=4662002
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB011154888A Expired - Fee Related CN1191322C (en) | 2001-04-28 | 2001-04-28 | Improved catalytic racking stripper |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1191322C (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8894940B2 (en) | 2012-06-14 | 2014-11-25 | Uop Llc | Process and apparatus for distributing hydrocarbon feed and catalyst |
| US9127212B2 (en) | 2012-06-14 | 2015-09-08 | Uop Llc | Process and apparatus for distributing hydrocarbon feed and catalyst |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101569842B (en) * | 2009-05-29 | 2011-06-29 | 张栋杰 | Suspension cone type stripper capable of effectively improving distribution area of catalyst |
-
2001
- 2001-04-28 CN CNB011154888A patent/CN1191322C/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8894940B2 (en) | 2012-06-14 | 2014-11-25 | Uop Llc | Process and apparatus for distributing hydrocarbon feed and catalyst |
| US9127212B2 (en) | 2012-06-14 | 2015-09-08 | Uop Llc | Process and apparatus for distributing hydrocarbon feed and catalyst |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1382764A (en) | 2002-12-04 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4336160A (en) | Method and apparatus for cracking residual oils | |
| US4786400A (en) | Method and apparatus for catalytically converting fractions of crude oil boiling above gasoline | |
| CN100537721C (en) | A kind of catalysis conversion method of propylene enhancing | |
| US6495028B1 (en) | Catalytic conversion process for producing isobutane and isoparaffin-enriched gasoline | |
| US11332680B2 (en) | Processes for producing petrochemical products that utilize fluid catalytic cracking of lesser and greater boiling point fractions with steam | |
| CN101029248A (en) | Method for increasing light olefin yield | |
| CN102250641B (en) | Method and apparatus for preparing ethylene and propylene with maximized yield | |
| CN1137968C (en) | Two-stage catalytic cracking process for hydrocarbon oil | |
| CN201695001U (en) | Device for preparing ethylene and propylene | |
| CN1191322C (en) | Improved catalytic racking stripper | |
| CN100404644C (en) | Method and apparatus for processing coked waxy oil | |
| CN1181163C (en) | Combination type method for catalyzing and transfering hydrocarbon oil | |
| CN1151232C (en) | Method for regulating heat balance of catalytic conversion technological reaction-regeneration system | |
| CN1179018C (en) | Catalytic conversion process of heavy petroleum hydrocarbon for increasing output of ethylene and propylene | |
| CN1234426A (en) | Process for synchronously preparing low-carbon olefines and high aromatic-hydrocarbon gasoline | |
| CN1191323C (en) | Catalytic cracking stripper with hydrooarbon oil convering function | |
| CN1246516A (en) | Process for catalytic aromatization of gasoline fraction | |
| CN1141361C (en) | Catalytic cracking process for reducing content of olefin in gasoline | |
| CN1233799C (en) | Method and device for adjusting and controlling coupling between cracking heavy oil and transnaturing gasoline | |
| CN1223653C (en) | FCC process for upgrading gasoline heart cut | |
| CN1164717C (en) | Improved catalytic cracking reactor | |
| CN1208435C (en) | Catalytic conversion method for extracting isobutane and gasoline richly containing isoparaffin | |
| CN1142250C (en) | Catalytic cracking process for processing different kinds of petroleum hydrocarbon at same time | |
| CN109554192B (en) | Method for catalytic conversion of kerogen shale oil | |
| CN101987964A (en) | Catalytic conversion method of hydrocarbon oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20050302 Termination date: 20180428 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |