CN2285679Y - Two-stage combined selective cracking lift pipe reactor - Google Patents
Two-stage combined selective cracking lift pipe reactor Download PDFInfo
- Publication number
- CN2285679Y CN2285679Y CN 96216070 CN96216070U CN2285679Y CN 2285679 Y CN2285679 Y CN 2285679Y CN 96216070 CN96216070 CN 96216070 CN 96216070 U CN96216070 U CN 96216070U CN 2285679 Y CN2285679 Y CN 2285679Y
- Authority
- CN
- China
- Prior art keywords
- lighter hydrocarbons
- reaction tube
- riser reactor
- cracking
- combined selective
- 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 - Lifetime
Links
Images
Abstract
The utility model discloses a two-stage combined selective lifting-pipe reactor used for the catalytic cracking process of petrochemical industry. An outer shell is composed of a rectifying section, a light hydrocarbon cracking section, a mixing section and a heavy hydrocarbon cracking section which are arranged orderly from top to bottom. A light hydrocarbon reacting tube is arranged in the light hydrocarbon cracking section. The utility model can effectively control the catalyst-oil ratio of each section in the lifting-pipe reactor, and the raw materials of the light hydrocarbon and the heavy hydrocarbon can be cracked according to the desired technical conditions. The regulating range of product variety is enlarged, and the petroleum productivity and the gasoline octane number are improved.
Description
The utility model belongs to a kind of nucleus equipment in the petrochemical industry catalytic cracking process process, particularly a kind of selective cracking riser reactor.
At present, the riser reactor of commercial Application has patterns such as single riser, double lifting leg, sectional feeding riser.In fact, the sectional feeding riser also belongs to single riser, and it is to adopt sectional feeding to carry out cracking reaction to satisfy technological requirement.As the feedstock oil injecting lift pipe bottom of Kellogg company with difficult cracking, the feedstock oil injecting lift pipe top of easy cracking is to improve conversion ratio and to increase yield of gasoline.Chevron and BP company then will divide two place's injecting lift pipe reactors up and down with a kind of raw material, in order to reduce hydrogen migration, increase propylene, butylene productive rate, and improve octane number.Aforementioned sectional feeding riser only is to increase by one section feedstock oil charging aperture on traditional single riser reactor, and other structure is all less than changing.The shortcoming of this structure is that catalyst flow is fixed, and can't adjust oil ratio respectively, promptly can not satisfy the requirement of the needed oil ratio of cracking respectively of heavy hydrocarbon (residual oil, fraction oil) and lighter hydrocarbons (direct steaming gasoline, coker gasoline), and the cracking effect is bad.
But the purpose of this utility model is to provide a kind of flexible modulation oil ratio, is applicable to that heavy hydrocarbon and light hydrocarbon feedstocks carry out the two segments combined selective cracking riser reactor of catalytic cracking respectively by required separately process conditions, to satisfy the heavy hydrocarbon cracking is that gasoline and diesel oil, lighter hydrocarbons cracking are liquefied petroleum gas, and lighter hydrocarbons upgrading, octane number are improved.
For achieving the above object, the technical solution adopted in the utility model is that riser reactor adopts the sectional feeding riser, and the lighter hydrocarbons reaction tube is set in it, carries out cracking selectively to realize light hydrocarbon feedstocks oil.For more effective controlling agent oil ratio, improve the distribution of catalyst, reduce catalyst landing coefficient, lighter hydrocarbons reaction tube gateway is respectively arranged with the gateway structure.Concrete technical scheme is, riser reactor is made up of rectification section, lighter hydrocarbons cracking zone, mixer, heavy hydrocarbon cracking zone from bottom to up successively, and its underpart is provided with catalyst inlet and regenerator sloped tube joins, and top connects cyclone separator.The lighter hydrocarbons reaction tube is set in the lighter hydrocarbons cracking zone, and this reaction tube lower end is provided with entrance structure, with the circulation area of control regenerated catalyst; Its upper end is provided with export structure, makes by the lighter hydrocarbons reaction tube regenerated catalyst premixed of a small amount of carbon deposited catalyst with being risen by annular space between riser and the lighter hydrocarbons reaction tube that comes.Be provided with the lighter hydrocarbons charging aperture in the rectification section bottom, light hydrocarbon feedstocks oil charging aperture thus enters in the lighter hydrocarbons reaction tube, under a part of regenerated catalyst (oil ratio can reach 15～30) effect that comes by rectification section, part cracking is an oil liquefied gas, the uncracked raw material of another part has obtained upgrading, catalyst with a small amount of carbon deposit reaches lighter hydrocarbons reaction tube top, enters mixer after export structure and regenerated catalyst premixed.The rectification section bottom is provided with the fluidization steam vapor distributor, plays the effect of stream with uniform distribution steam and the stabilization fluid next regenerated catalyst by regenerator sloped tube, and regenerated catalyst is assigned in lighter hydrocarbons reaction tube and the lighter hydrocarbons cracking zone.On lighter hydrocarbons reaction tube entrance structure, lighter hydrocarbons reaction tube outer lower portion is provided with the lifting steam distributor, promote and the control rectification section in another part regenerated catalyst directly enter mixer.Because the mixer linear speed reaches 3～8m/s, has reduced the landing coefficient of catalyst.Oil ratio generally can be controlled to be 5～8 in the heavy hydrocarbon cracking zone, and this section bottom is provided with the heavy hydrocarbon feedstocks mouth, and heavy hydrocarbon feeds cracking under the effect of the catalyst that is come by mixer is gasoline, diesel oil.All oil gas and catalyst enter cyclone separator together and carry out gas solid separation.
The utility model compared with prior art, have the following advantages: be provided with the lighter hydrocarbons reaction tube in the riser reactor, make riser inner catalyst density radial distribution more even, catalyst landing coefficient reduces, lighter hydrocarbons and heavy hydrocarbon feeds can carry out cracking by required process conditions separately, strengthen the adjustable range of product category, improved oil product productive rate and octane number.
Below in conjunction with accompanying drawing, further specify the utility model by specific embodiment, wherein:
Fig. 1 is a kind of typical structure schematic diagram of the utility model.
Fig. 2～6 are the other several structural representations of the utility model, and wherein the form and the arrangement of lighter hydrocarbons reaction tube and gateway structure thereof are different.
Fig. 1 is a kind of version of the present utility model, the housing 3 of riser reactor is made up of rectification section 7, lighter hydrocarbons cracking zone 6, mixer 5, heavy hydrocarbon cracking zone 4 from bottom to up successively, its underpart regenerated catalyst import 2 connects regenerator sloped tube, top connects cyclone separator 1, in order to satisfy technological requirement better, this cyclone separator 1 preferably divides soon.Be provided with lighter hydrocarbons reaction tube 8 in the lighter hydrocarbons cracking zone 6, the top and bottom of this reaction tube 8 can set out mouth structure 9, entrance structure 11 respectively, with the superiority of further performance present technique.Wherein, entrance structure 11 is an oviduct, and export structure 9 is a conical plate.Lighter hydrocarbons reaction tube 8 outer lower portion are provided with and promote steam distributor 10, and rectification section 7 bottoms are provided with lighter hydrocarbons charging aperture 14 and fluidization steam vapor distributor 12, and heavy hydrocarbon cracking zone 4 bottoms are provided with heavy hydrocarbon feedstocks mouth 13.
The working condition of present embodiment is such: regenerated catalyst under the vapor action of being come by fluidization steam vapor distributor 12, carries out stabilization fluid in regenerated catalyst import 2 enters rectification section 7, and radially evenly distributes.Wherein, part regenerated catalyst enters lighter hydrocarbons reaction tube 8 through lighter hydrocarbons reaction tube entrance structure 11, carry out cracking reaction with light hydrocarbon feedstocks through lighter hydrocarbons charging aperture 14, another part not with the effect of the contacted regenerated catalyst of lighter hydrocarbons through promoting steam distributor 10 steam under, rise to the lower end of mixer 5, the cracking oil gas, uncracked upgrading feedstock oil, a small amount of carbon deposited catalyst that come with reaction tube carry out premixed under the guide effect of export structure 9, after mixer fully mixes, enter heavy hydrocarbon cracking zone 4.In this section, the heavy hydrocarbon that comes by heavy hydrocarbon feedstocks mouth 13 and under the effect of a part of lighter hydrocarbons at mixed catalyst of lighter hydrocarbons cracking zone upgrading, carry out cracking reaction, all reaction oil gas and catalyst enter cyclone separator 1 together and carry out gas solid separation, isolate oil gas and reclaimable catalyst.
Fig. 2 is an another kind of structural shape of the present utility model, and its structure and working condition and first embodiment are basic identical, and different is that entrance structure 11 is directly to offer the bar shaped slotted hole on the lower case of lighter hydrocarbons reaction tube 8.Certainly, also can offer the hole of circular hole, elliptical aperture or other shape, also can be the combining form in these holes.
Fig. 3 is another structural shape of the present utility model, and its structure and working condition and first embodiment are basic identical, and different is that entrance structure 11 is directly to offer serrate slot in the lower end of lighter hydrocarbons reaction tube 8 to form.
Fig. 4 is another structural shape of the present utility model, its structure and working condition and first embodiment are basic identical, and different is that entrance structure 11 is that a conical plate is formed, its upper end joins with the lower end of lighter hydrocarbons reaction tube 8, and the lower end links to each other with the upper end of rectification section 7.And entrance structure 11 is positioned at the top of regenerated catalyst import 2 and rectification section 7 intersections, offers the hole of definite shape on it, as annular, circle, ellipse etc., or their combining form.
Fig. 5 is another structural shape of the present utility model, and its structure and working condition and first embodiment are basic identical, and different is that export structure 9 is a back taper plate.
Fig. 6 is another structural shape of the present utility model, its structure and working condition and embodiment illustrated in fig. 4 basic identical, different is, do not offer the hole on entrance structure 11 conical plates, and respectively being provided with regenerated catalyst import 2 at rectification section 7 and lighter hydrocarbons cracking zone 6 bottoms, above-mentioned entrance structure 11 is between two regenerated catalyst imports 2.In the present embodiment, entrance structure 11 is other versions such as back taper plate or ring plate also.In the present embodiment,, can regulate the catalyst inlet respectively, change to satisfy oil ratio owing to have two regenerated catalyst imports 2.
In the foregoing description, export structure 9 also can be varied to other form, as conical plate or back taper board diameter internal diameter less than riser reactor housing 3, and be positioned at the top of lighter hydrocarbons reaction tube 8, directly the regenerated catalyst by rectification section 7 enters mixer through the radial clearance between export structure 9 and riser reactor housing; Also can make conical plate or back taper board diameter equal to promote the internal diameter of reactor shell 3, offer the hole of definite shape on conical plate between lighter hydrocarbons reaction tube 8 and the riser reactor housing 3 or back taper plate, directly the regenerated catalyst by rectification section 7 enters mixer through this hole.
Certainly, as required, also the export structure in the foregoing description 9 and entrance structure 11 can be made up and form the utility model.
Claims (13)
1, two segments combined selective cracking riser reactor in a kind of petrochemical industry catalytic cracking process, it is characterized in that, its housing (3) is from bottom to up successively by rectification section (7), lighter hydrocarbons cracking zone (6), mixer (5), heavy hydrocarbon cracking zone (4) is formed, described riser reactor bottom is provided with a regenerated catalyst import (2), top connects cyclone separator (1), in lighter hydrocarbons cracking zone (6), be provided with lighter hydrocarbons reaction tube (8), its top and bottom are respectively arranged with export structure (9) and entrance structure (11), outer lower portion is provided with and promotes steam distributor (10), rectification section (7) bottom is provided with lighter hydrocarbons charging aperture (14) and fluidization steam vapor distributor (12), and heavy hydrocarbon cracking zone (4) bottom is provided with heavy hydrocarbon feedstocks mouth (13).
2, two segments combined selective cracking riser reactor according to claim 1 is characterized in that, export structure (9) is a conical plate, and entrance structure (11) is a horn-like pipe.
3, two segments combined selective cracking riser reactor according to claim 1 is characterized in that, export structure (9) is a conical plate, entrance structure (11) be directly on the lower case of lighter hydrocarbons reaction tube (8), offer porose.
4, two segments combined selective cracking riser reactor according to claim 1 is characterized in that, export structure (9) is a conical plate, and entrance structure (11) is directly to offer the profile of tooth notch in the lower end of lighter hydrocarbons reaction tube (8).
5, two segments combined selective cracking riser reactor according to claim 1, it is characterized in that, export structure (9) is a conical plate, entrance structure (11) constitutes for the conical plate of perforate, its upper end joins with the lower end of lighter hydrocarbons reaction tube (8), the lower end links to each other with the upper end of rectification section (7), opens the top that is positioned at regenerated catalyst import (2) and rectification section (7) intersection.
6, two segments combined selective cracking riser reactor according to claim 1, it is characterized in that, export structure (9) is the back taper plate, its diameter equals the internal diameter of housing (3), be positioned at and offer porosely on the back taper plate between lighter hydrocarbons reaction tube (8) and the housing (3), entrance structure (11) is horn-like pipe.
7, two segments combined selective cracking riser reactor in a kind of petrochemical industry catalytic cracking process, it is characterized in that, its housing (3) is from bottom to up successively by rectification section (7), lighter hydrocarbons cracking zone (6), mixer (5), heavy hydrocarbon cracking zone (4) is formed, described rectification section (7), the bottom of lighter hydrocarbons cracking zone (6) respectively is provided with regenerated catalyst import (2), in lighter hydrocarbons cracking zone (6), be provided with lighter hydrocarbons reaction tube (8), its top and bottom are respectively arranged with export structure (9) and entrance structure (11), outer lower portion is provided with and promotes steam distributor (10), rectification section (7) bottom is provided with lighter hydrocarbons charging aperture (14) and fluidization steam vapor distributor (12), and heavy hydrocarbon cracking zone (4) bottom is provided with heavy hydrocarbon feedstocks mouth (13).
8, two segments combined selective cracking riser reactor according to claim 7, it is characterized in that, described entrance structure (11) is a conical plate, its upper end joins with the lower end of lighter hydrocarbons reaction tube (8), the lower end links to each other with the upper end of rectification section (7) and is positioned between two regenerated catalyst imports (2), and described export structure (9) is a conical plate.
9, two segments combined selective cracking riser reactor according to claim 7, it is characterized in that, described entrance structure (11) is a conical plate, its upper end joins with the lower end of lighter hydrocarbons reaction tube (8), the lower end links to each other with the upper end of rectification section (7) and is positioned between two regenerated catalyst imports (2), and described export structure (9) is a back taper plate.
10, two segments combined selective cracking riser reactor according to claim 7, it is characterized in that, described entrance structure (11) is a back taper plate, the lower end of its lower end and lighter hydrocarbons reaction tube (8) joins, the upper end links to each other with riser housing (3) and is positioned between two regenerated catalyst imports (2), and described export structure (9) is a conical plate.
11, two segments combined selective cracking riser reactor according to claim 7, it is characterized in that, described entrance structure (11) is a back taper plate, the lower end of its lower end and lighter hydrocarbons reaction tube (8) joins, the upper end links to each other with riser housing (3) and is positioned between two regenerated catalyst imports (2), and described export structure (9) is a back taper plate.
12, two segments combined selective cracking riser reactor according to claim 7, it is characterized in that, described entrance structure (11) is a ring plate, join with lower end in it with lighter hydrocarbons reaction tube (8), outer garden links to each other with the upper end of rectification section (7) and is positioned at two regeneration catalyzings and stops between the import (2), and described export structure (9) is a conical plate.
13, two segments combined selective cracking riser reactor according to claim 7, it is characterized in that, described entrance structure (11) is a ring plate, lower end of garden and lighter hydrocarbons reaction tube (8) joins in it, outer garden links to each other with the upper end of rectification section (7) and is positioned between two regenerated catalyst imports (2), and described export structure (9) is a back taper plate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 96216070 CN2285679Y (en) | 1996-06-11 | 1996-08-06 | Two-stage combined selective cracking lift pipe reactor |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96212360.9 | 1996-06-11 | ||
| CN 96216070 CN2285679Y (en) | 1996-06-11 | 1996-08-06 | Two-stage combined selective cracking lift pipe reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN2285679Y true CN2285679Y (en) | 1998-07-08 |
Family
ID=33897686
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 96216070 Expired - Lifetime CN2285679Y (en) | 1996-06-11 | 1996-08-06 | Two-stage combined selective cracking lift pipe reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN2285679Y (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1320096C (en) * | 2004-10-13 | 2007-06-06 | 姜国文 | Brewing equipment for preparing lightweight alkane from heavy hydrocarbon and process thereof |
-
1996
- 1996-08-06 CN CN 96216070 patent/CN2285679Y/en not_active Expired - Lifetime
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1320096C (en) * | 2004-10-13 | 2007-06-06 | 姜国文 | Brewing equipment for preparing lightweight alkane from heavy hydrocarbon and process thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| KR100939503B1 (en) | Downflow catalytic cracking reactor and use thereof | |
| CN110240932B (en) | Petroleum hydrocarbon multistage fluidized catalytic reaction method and reactor | |
| CN102039107A (en) | Parallel cyclic reaction-regeneration device with embedded riser | |
| US4753721A (en) | Process for resid hydrotreating employing feed distributor | |
| CN109833834A (en) | A kind of petroleum hydrocarbon catalytic pyrolysis reaction method and reactor | |
| CN110240925A (en) | A kind of fluid catalytic cracking reaction regeneration method | |
| CN100567460C (en) | Utilize catalyzing and cracking light-hydrocarbon material to prepare the method and the device of low-carbon alkene | |
| CN201020348Y (en) | Fluidization mixer for thin powder solid media | |
| CN1058046C (en) | Catalyst cracking method for producing in high-yield olefin and lift-leg reaction system thereof | |
| CN2285679Y (en) | Two-stage combined selective cracking lift pipe reactor | |
| CN103788993B (en) | A kind of catalytic cracking unit | |
| CN110499181A (en) | A kind of catalyst cracking method and device of the reaction of at the uniform velocity bed | |
| CN114262624B (en) | Method and device for catalytic cracking of double-component granular catalyst coupling fluidized bed | |
| CN215353341U (en) | Petroleum hydrocarbon fluidized catalytic conversion reactor | |
| CN216946880U (en) | Catalytic cracking reactor and catalytic cracking system | |
| CN1091393C (en) | Catalytic cracking riser reactor | |
| CN117186937A (en) | Catalytic cracking reaction-regeneration system and method | |
| CN114717021A (en) | Method and reaction device for preparing olefin and aromatic hydrocarbon through catalytic cracking | |
| CN2791050Y (en) | Fluidized catalytic-cracking lift pipe reactor | |
| CN208839567U (en) | A kind of petroleum hydrocarbon catalytic pyrolysis reactor | |
| CN111100664B (en) | Method for preparing aromatic hydrocarbon by catalytic conversion of methanol | |
| CN102268291A (en) | Catalytic cracking technology and device for reducing olefins in gasoline | |
| CN2506644Y (en) | Double-pathway feeding sleeve type catalyzing-cracking reactor | |
| CN102212382B (en) | Catalytic cracking process and device | |
| CN216864088U (en) | Clean fuel production riser reactor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CX01 | Expiry of patent term |