CN105505456A - Catalytic cracking apparatus and method for catalytically cracking petroleum hydrocarbon - Google Patents
Catalytic cracking apparatus and method for catalytically cracking petroleum hydrocarbon Download PDFInfo
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- CN105505456A CN105505456A CN201410559249.6A CN201410559249A CN105505456A CN 105505456 A CN105505456 A CN 105505456A CN 201410559249 A CN201410559249 A CN 201410559249A CN 105505456 A CN105505456 A CN 105505456A
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Abstract
The invention discloses a catalytic cracking apparatus. The catalytic cracking apparatus comprises a riser reactor, a settler and a stripping device; the stripping device is disposed below the settler, and the stripping device and the settler are integrally formed and are coaxial; the riser reactor penetrates the bottom of the stripping device and stretches into the settler; the settler is inside provided with a cyclone separator for oiling-agent separation; the lower-part chamber of the settler is inside provided with a sleeve with an upper opening and a lower opening, and the sleeve is coaxial with the settler; the outlet of the riser reactor is disposed in the sleeve in order to form a fluidized-bed reaction zone in the sleeve; and a catalyst outlet of the cyclone separator is disposed in a space formed by the outer wall of the sleeve and the inner wall of the settler. The invention also provides a method for catalytically cracking petroleum hydrocarbon. Through the above technical scheme, the catalysis efficiency of the fluidized-bed reactor in the catalytic cracking apparatus is substantially improved, and therefore the low-carbon olefin yield of catalytic cracking is improved.
Description
Technical field
The present invention relates to petrochemical industry, particularly, relate to a kind of a kind of method of catalytic cracking unit and catalytic cracking gasoline hydrocarbon.
Background technology
Carbon olefin is important industrial chemicals, and at present, the dominant technology of producing ethene and propylene in world wide is steam cracking, about has the ethene of more than 95% and the propylene of more than 60% to be obtained by this technology.From world wide, with petroleum naphtha be cracking stock account for 48%, ethane accounts for 33%, and propane accounts for 8%, and butane accounts for about 5%, and oil gas accounts for 4%, and other account for 2%.In steam-cracking process, owing to there is no catalyzer, the cracking of hydro carbons needs comparatively harsh operational condition, make produce and plant construction cost higher, and crude oil day by day heaviness, light hydrocarbon feedstocks lacks day by day serious, develop with heavy oil be raw material production low-carbon alkene technological line thus become the only selection of producing low-carbon alkene.
Catalytic cracking is another important sources of low-carbon alkene, can improve the level of crude oil processing, produces stop bracket gasoline, diesel oil and liquefied gas in refinery.In Conventional catalytic cracking, along with the production of gasoline and diesel oil, also by-product low-carbon alkene simultaneously, but its productive rate is lower, can not meet the needs in market.
The structure of conventional catalytic cracking unit comprises riser tube, gas-solid separator and revivifier, such as CN103725321A discloses a kind of catalytic cracking unit, this device comprises riser tube, gas-solid separator and revivifier, the discharge end of described riser tube is communicated with the opening for feed of gas-solid separator, the gaseous stream outlet of described gas-solid separator is used for being communicated with follow-up oil and gas separating system, the spent agent outlet of described gas-solid separator is connected with the spent agent inclined tube of revivifier and is communicated with, to provide spent agent to revivifier, the regenerator discharge port of revivifier is communicated with the catalyst feeds of riser tube, for providing regenerator to riser tube.
In the catalytic cracking unit of routine, the utilization ratio of fluidized-bed reactor is lower, thus causes existing catalytic cracking unit and there is the lower defect of productivity of low carbon olefin hydrocarbon.
Summary of the invention
Object of the present invention overcomes the defect that existing for existing catalytic cracking unit and method, productivity of low carbon olefin hydrocarbon is lower, provides a kind of and has catalytic cracking unit compared with high-low carbon olefins yield and catalyst cracking method.
The present inventor finds, the reason of existing catalytic cracking unit and the lower defect of the productivity of low carbon olefin hydrocarbon existing for method is that the fluidized bed layer height in catalytic cracking unit is lower, and fluidized-bed bed is subject to the interference of the reclaimable catalyst of the carbon distribution that the cyclonic separator in catalytic cracking unit separates and unstable, thus, the present inventor is provided with sleeve to increase fluidized bed layer height and to hinder the interference of the reclaimable catalyst of carbon distribution, considerably improve productivity of low carbon olefin hydrocarbon, resulting in the present invention.
To achieve these goals, the invention provides a kind of catalytic cracking unit, this catalytic cracking unit comprises riser reactor, settling vessel and stripper; Described stripper is positioned at the below of described settling vessel and is integrally formed with described settling vessel and coaxial; Described riser reactor passes the bottom of described stripper and stretches in described settling vessel; The cyclonic separator for carrying out finish separation is provided with in described settling vessel; Wherein, in the lower cavity of described settling vessel, be provided with the sleeve of the upper and lower opening coaxial with this settling vessel; The material outlet of described riser reactor is positioned at described sleeve to form fluidized bed reaction zone at described sleeve; The dipleg mouth of described cyclonic separator is arranged in the space formed by the inwall of the outer wall of described sleeve and described settling vessel; Described fluidized bed reaction zone, described space and described stripper be all fluid connections each other.
On the other hand, present invention also offers a kind of method of catalytic cracking gasoline hydrocarbon, the method comprises the steps: (a) by the bottom of the stock oil after preheating, cracking catalyst and pre-lift gas injecting lift pipe reactor to form the first reaction oil gas logistics risen along riser reactor; (b) by described first reaction oil gas logistics by fluidized bed reaction zone to form the second reaction oil gas logistics; Wherein, described fluidized bed reaction zone is formed in the sleeve of upper and lower opening, and the lower cavity that described sleeve is arranged at settling vessel is interior and coaxial with described settling vessel, and the outlet of described riser reactor is positioned at described sleeve; C described second reaction oil gas logistics is separated into the reclaimable catalyst of gaseous product and carbon distribution by () through cyclonic separator; The reclaimable catalyst outlet of the carbon distribution of described cyclonic separator is arranged in the space formed by the inwall of the outer wall of described sleeve and described settling vessel; D () makes described reclaimable catalyst carry out stripping from the bottom importing stripper of described settling vessel; Described stripper is positioned at the below of described settling vessel and is integrally formed with described settling vessel and coaxial; Described riser reactor passes the bottom of described stripper and stretches in described settling vessel.
By technique scheme, invention significantly increases the catalytic efficiency of the fluidized-bed reactor in catalytic cracking unit, thus improve the productivity of low carbon olefin hydrocarbon of catalytic cracking.
Other features and advantages of the present invention are described in detail in embodiment part subsequently.
Accompanying drawing explanation
Accompanying drawing is used to provide a further understanding of the present invention, and forms a part for specification sheets, is used from explanation the present invention, but is not construed as limiting the invention with embodiment one below.In the accompanying drawings:
Fig. 1 is the structural representation of the particularly preferred a kind of embodiment of the present invention catalytic cracking unit used.
Description of reference numerals
1 riser reactor 11 stock oil feed nozzle
12 regenerated catalyst 13 spargers
14 cyclonic separators
2 fluidized bed reaction zone 21 sleeves
3 settling vessels
4 stripper 41 baffle plates
42 reclaimable catalyst transfer limes
5 space 6 catalyst regenerators
Embodiment
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described in detail.Should be understood that, embodiment described herein, only for instruction and explanation of the present invention, is not limited to the present invention.
In the present invention, when not doing contrary explanation, the situation that the noun of locality used normally normally uses in catalytic cracking unit provided by the invention as " upper and lower, the end, top " is undefined, particularly can with reference to the page shown in figure 1, " inside and outside " refers to the interior and outer of respective profile.It should be noted that, these nouns of locality, only for illustration of the present invention, are not limited to the present invention.
With reference to figure 1, the invention provides a kind of catalytic cracking unit, this catalytic cracking unit comprises riser reactor 1, settling vessel 3 and stripper 4; Described stripper 4 is positioned at the below of described settling vessel 3 and is integrally formed with described settling vessel 3 and coaxial; Described riser reactor 1 passes the bottom of described stripper 4 and stretches in described settling vessel 3; The cyclonic separator 14 for carrying out finish separation is provided with in described settling vessel 3; Wherein, in the lower cavity of described settling vessel 3, be provided with the sleeve 21 of the upper and lower opening coaxial with this settling vessel 3; The material outlet of described riser reactor 1 be positioned at described sleeve 21 with at described sleeve 21 to form fluidized bed reaction zone 2; The dipleg mouth of described cyclonic separator 14 is arranged in the space 5 formed by the outer wall of described sleeve 21 and the inwall of described settling vessel 3; Described fluidized bed reaction zone 2, described space 5 and described stripper 4 be all fluid connections each other.
According to catalytic cracking unit of the present invention, wherein, the aspect ratio of described sleeve 21 can change in a big way, and preferably, the aspect ratio of described sleeve 21 is 0.2-5, and more preferably, the aspect ratio of described sleeve 21 is 0.5-3.
According to catalytic cracking unit of the present invention, wherein, preferably, the lower end of described riser reactor 1 is provided with stock oil feed nozzle 11 and regenerated catalyst 12.Wherein, described stock oil feed nozzle 11 is for importing described riser reactor 1 by stock oil; Described regenerated catalyst 12 is for importing described riser reactor 1 by regenerated catalyst.Described riser reactor 14 can be 1 or be symmetrically arranged 2-3.
According to catalytic cracking unit of the present invention, wherein, preferably, the described material outlet of described riser reactor 1 is provided with sparger 13.Wherein, described sparger 13 can be the various spargers that this area routine uses, such as screen hole type sparger.
According to catalytic cracking unit of the present invention, wherein, preferably, described cyclonic separator 14 is 1 or is symmetrically arranged 2-3.More preferably, described cyclonic separator comprises primary cyclone and secondary cyclone.Described primary cyclone and described secondary cyclone can be arranged in series.
According to catalytic cracking unit of the present invention, wherein, described catalytic cracking unit can also comprise catalyst regenerator 6; Described stripper 4 can be provided with the reclaimable catalyst transfer lime 42 be communicated with the catalyst inlet of described catalyst regenerator 6; The regenerated catalyst 12 of described riser reactor 1 can be communicated with the catalyst outlet of described catalyst regenerator 6.Wherein, the decaying catalyst of deriving in described stripper 4 can be passed through coke burning regeneration under oxygen-containing gas exists by described catalyst regenerator 6.
According to catalytic cracking unit of the present invention, wherein, described catalyst regenerator 6 can coaxially be arranged with described settling vessel 3, also can be set up in parallel, and preferably, described catalyst regenerator 6 is set up in parallel with described settling vessel 3.
According to catalytic cracking unit of the present invention, wherein, preferably, described riser reactor 1 stretches in described settling vessel 3 through described stripper 4.
According to catalytic cracking unit of the present invention, wherein, preferably, the internal diameter on described settling vessel 3 top is greater than the internal diameter of described settling vessel 3 bottom.
In catalytic cracking unit of the present invention, each component can adopt airtight connection, and the reaction can born in catalytic cracking process or regeneration pressure, such as 1-10 normal atmosphere; But also the impact of expanding with heat and contract with cold on component and pipeline that the factors such as the change of shutting down, seasonal variation, reactant flow temperature cause will be considered.
As shown in Figure 1, although this schematic diagram is simple flow, this does not affect those of ordinary skill in the art's the understanding of the present invention to a kind of carrying out practically mode of catalytic cracking unit provided by the invention.After fuel oil preheating, riser reactor 1 is sprayed into by stock oil feed nozzle 11 together with water vapour, with the hot regenerated catalyst contact reacts from regenerated catalyst 12, reaction oil gas enters fluidized bed reaction zone 2 from riser reactor outlet, in fluidized bed reaction zone 2 after reaction, upper outlet through sleeve 21 enters settling vessel 4, be separated with gaseous product through the reclaimable catalyst of cyclonic separator 14 by carbon distribution, the reclaimable catalyst of isolated carbon distribution enters stripper 4 through space 5; Gaseous product and the stripping air-fuel mixture from stripper 4, enter fractionation plant from the top of settling vessel 3, is separated further and obtains gas (comprising dry gas, liquefied gas), petroleum naphtha, is rich in light aromatic hydrocarbons heavy petrol, diesel oil and slurry oil.Gas products, by isolation technique well known to those skilled in the art, obtains the low-carbon alkenes such as propylene.Reclaimable catalyst stripping in stripper 4 of carbon distribution goes out the hydrocarbon product of absorption, and the reclaimable catalyst obtained is delivered to catalyst regenerator 6 through reclaimable catalyst transfer lime 42 and carried out coke burning regeneration, and regenerated catalyst returns riser reactor 1 and reuses.
Present invention also offers a kind of method of catalytic cracking gasoline hydrocarbon, wherein, the method comprises the steps: (a) by the bottom of the stock oil after preheating, cracking catalyst and pre-lift gas injecting lift pipe reactor 1 to form the first reaction oil gas logistics risen along riser reactor 1; (b) by described first reaction oil gas logistics by fluidized bed reaction zone 2 to form the second reaction oil gas logistics; Wherein, described fluidized bed reaction zone 2 is formed in the sleeve 21 of upper and lower opening, and the lower cavity that described sleeve 21 is arranged at settling vessel 3 is interior and coaxial with described settling vessel 3, and the material outlet of described riser reactor 1 is positioned at described sleeve 21; C described second reaction oil gas logistics is separated into the reclaimable catalyst of gaseous product and carbon distribution by () through cyclonic separator 14; The dipleg outlet of described cyclonic separator 14 is arranged in the space 5 formed by the outer wall of described sleeve 21 and the inwall of described settling vessel 3; D () makes described reclaimable catalyst carry out stripping from the bottom importing stripper 4 of described settling vessel 3; Described stripper 4 is positioned at the below of described settling vessel 3 and is integrally formed with described settling vessel 3 and coaxial; Described riser reactor 1 passes the bottom of described stripper 4 and stretches in described settling vessel 3.
Wherein, the first reaction oil gas logistics refers to the mixture of reaction oil gas in described riser reactor 1 and catalyzer, and the second reaction oil gas logistics refers to the mixture of reaction oil gas in described settling vessel 3 and catalyzer.
Wherein, described sleeve 21 defines the segment boundary of described fluidized bed reaction zone 2, the dipleg outlet of described cyclonic separator 14 is arranged in the space 5 formed by the outer wall of described sleeve 21 and the inwall of described settling vessel 3, the reclaimable catalyst of carbon distribution is directly imported in described space 5 through the dipleg outlet of described cyclonic separator 14, and does not enter described fluidized bed reaction zone 2; Described sleeve 21 can be increased fluidized bed layer height and the reclaimable catalyst of carbon distribution can be hindered the interference of fluidized-bed bed.
According to the method for catalytic cracking gasoline hydrocarbon of the present invention, wherein, reaction conditions in described riser reactor 1 can be the condition used conventional in catalytic cracking field, such as, the temperature out of described riser reactor 1 can be 450-600 DEG C, is preferably 480-530 DEG C, top hole pressure can be 0.15-0.3MPa, be preferably 0.18-0.28MPa, agent-oil ratio can be (4-15): 1, is preferably (6-12): 1; Reaction times can be 1-5 second, is preferably 2-4 second.
According to the method for catalytic cracking gasoline hydrocarbon of the present invention, wherein, the weight ratio of described stock oil and described pre-lift gas can change in a big way, the weight ratio of such as described stock oil and described pre-lift gas can be (0.01-2): 1, is preferably (0.05-0.2): 1; Described pre-lift gas can comprise at least one in the alkane of water vapour, nitrogen and C1-C4; The temperature of described pre-lift gas can be 180-280 DEG C, is preferably 220-250 DEG C.
According to the method for catalytic cracking gasoline hydrocarbon of the present invention, wherein, reaction conditions in described fluidized bed reaction zone (2) can for selection conventional in catalytic cracking field, such as, bed temperature in described fluidized bed reaction zone (2) can be 480-620 DEG C, be preferably 500-600 DEG C, weight hourly space velocity can be 0.2-30h
-1, be preferably 0.5-20h
-1, bed layer pressure can be 0.15-0.3MPa, is preferably 0.2-0.25MPa.
According to the method for catalytic cracking gasoline hydrocarbon of the present invention, wherein, the aspect ratio of described sleeve 21 can change in a big way, such as, be 0.1-10; Preferably, the aspect ratio of described sleeve 21 is 0.2-5, is more preferably 0.5-3.Be 0.2-5 at the aspect ratio of preferred described sleeve 21, when being more preferably 0.5-3, catalytic efficiency can be improved further.
Wherein, at least one in fixed fluidized-bed reactor, particulate fluidization bed bioreactor, bubbling bed reactor, turbulent bed reactor, fast bed reactor, transport bed reactor and dense fluidized bed bioreactor can be formed in described fluidized bed reaction zone 2 as required.
According to the method for catalytic cracking gasoline hydrocarbon of the present invention, wherein, the preheating temperature of described stock oil can be 180-400 DEG C, is preferably 200-380 DEG C; The range of choice of described stock oil is wider, such as, can comprise at least one in diesel oil, hydrogenation tail oil, vacuum gas oil, crude oil, long residuum, pressurization residual oil, liquefied coal coil, tar sand oil and shale oil.
Wherein, the reclaimable catalyst of described carbon distribution is imported in stripper 4 from described space 5 and carries out stripping, can use through regeneration Posterior circle.Described stripping can carry out by gas stripping process conveniently, and stripping fluid used can be water vapour; The weight ratio of the reclaimable catalyst of stripping water vapour used and carbon distribution can be (0.005-0.1): 1, is preferably (0.005-0.01): 1; The temperature of the water vapour that stripping passes into can be 200-300 DEG C.
According to the method for catalytic cracking gasoline hydrocarbon of the present invention, wherein, described gaseous product and stripping oil gas can be derived from the top of described settling vessel 3; The gaseous product of deriving and stripping oil gas can enter fractionation plant and carry out fractionation, and to obtain the cut of different boiling ranges, such as pyrolysis gasoline, Pyrolysis gas oil PGO, liquefied gas, oil refinery dry gas and slurry oil, wherein oil refinery dry gas contains a large amount of low-carbon alkenes.
According to the method for catalytic cracking gasoline hydrocarbon of the present invention, wherein, the method can also comprise: the reclaimable catalyst obtained by stripping imports in catalyst regenerator and carries out coke burning regeneration.Wherein, the coke burning regeneration of reclaimable catalyst can carry out according to method conventional in catalytic cracking field, and the technician in catalytic cracking field knows this, and the present invention does not repeat them here.
According to the method for catalytic cracking gasoline hydrocarbon of the present invention, wherein, the various catalyzer that described cracking catalyst can use for catalytic cracking field routine, such as, with the gross weight of described cracking catalyst for benchmark, described cracking catalyst can contain the clay of the mixed zeolite of 1-60 % by weight, the carrier of 5-98 % by weight and 0.1-70 % by weight.Wherein, with the gross weight of described mixed zeolite for benchmark, in described mixed zeolite can containing 40-99.5 % by weight containing rare earth and the five-ring supersiliceous zeolite of phosphorus and the type-Y high silicon zeolite of 0.5-60 % by weight.Wherein, described carrier can be selected from aluminum oxide and/or pure aluminium silicate.Wherein, the described five-ring supersiliceous zeolite containing rare earth and phosphorus comprises one or more in MFI zeolite, ZSM-5 zeolite and ZRP zeolite.Described cracking catalyst used in the present invention is prepared by technology known in the art or is commercially available.
The following examples will be further described present method, but therefore not limit present method.
In following examples, take total catalyst weight as benchmark, used catalyst contains the ZRP-1 zeolite of 30 % by weight, the DASY zeolite of 10 % by weight, the kaolin of 40 % by weight and the alumina binder of 20 % by weight; Wherein ZRP-1 zeolite, DASY zeolite are catalyzer asphalt in Shenli Refinery of China Petrochemical Industry product.In following examples, stock oil used is long residuum, and the numerical value after its character detects according to national standard is as shown in table 1.
Table 1
Embodiment 1
With reference to figure 1, by the heavy oil feedstock (its character is as shown in table 1) after preheating, water vapor and cracking catalyst injecting lift pipe reactor 1 bottom from revivifier 6, form the first reaction oil gas logistics risen along riser reactor 1, first reaction oil gas logistics is left riser reactor 1 and is exported, enter bottom, fluidized bed reaction zone 2, reaction is continued in the bed that catalyzer is formed, described fluidized bed reaction zone 2 is formed in the sleeve 21 of upper and lower opening, the lower cavity that described sleeve 21 is arranged at settling vessel 3 is interior and coaxial with described settling vessel 3, and the outlet of described riser reactor 1 is positioned at described sleeve 21, the aspect ratio of described sleeve 21 is 0.25, described first reaction oil gas logistics by fluidized bed reaction zone 2 to form the second reaction oil gas logistics.Described second reaction oil gas logistics is separated into the reclaimable catalyst of gaseous product and carbon distribution through cyclonic separator 14; The dipleg outlet of described cyclonic separator 14 is arranged in the space 5 formed by the outer wall of described sleeve 21 and the inwall of described settling vessel 3; The reclaimable catalyst of described carbon distribution is imported in stripper 4 from described space 5 and carries out stripping; Described stripper 4 is arranged on the below of described fluidized bed reaction zone 2 and coaxial with described settling vessel 3; The reclaimable catalyst obtained after stripping is transported to revivifier by regenerator sloped tube and regenerates.Gaseous product and stripping oil gas are derived from the top of described settling vessel 3; The gaseous product of deriving and stripping oil gas enter fractionation plant and carry out fractionation, to obtain the cut of different boiling ranges.The reaction conditions of the present embodiment comprises: stock oil inlet amount is 6.0kg/h; The temperature out of riser reactor 1 is 540 DEG C; Agent-oil ratio is 10; The reaction times of riser reactor 1 is 2.8s, and top hole pressure is 0.2MPa, and the importing water vapour of riser reactor 1 and the ratio of stock oil are 0.15:1; The temperature of fluidized bed reaction zone 2 is 565 DEG C; Weight hourly space velocity is 6h
-1; Bed layer pressure is 0.2MPa.
Embodiment 2
Adopt the method for embodiment 1 to carry out catalytic cracking, difference is, the aspect ratio of described sleeve 21 is 0.75.
Embodiment 3
Adopt the method for embodiment 1 to carry out catalytic cracking, difference is, the aspect ratio of described sleeve 21 is 1.86.
Embodiment 4
Adopt the method for embodiment 1 to carry out catalytic cracking, difference is, the aspect ratio of described sleeve 21 is 2.86
Embodiment 5
Adopt the method for embodiment 1 to carry out catalytic cracking, difference is, the aspect ratio of described sleeve 21 is 4.78.
Comparative example 1
Adopt the method for embodiment 1 to carry out catalytic cracking, difference is, does not arrange described sleeve 21.
Testing example 1
Product slates in the catalytic cracking production (comprising pyrolysis gasoline, Pyrolysis gas oil PGO, liquefied gas, oil refinery dry gas and coke) that mensuration embodiment 1-5 and comparative example 1 obtain and productivity of propylene; Result is as shown in table 2.
Table 2
Visible according to the data of table 1, apparatus and method of the present invention can significantly improve the catalytic efficiency of fluidized-bed reactor, thus significantly improve the productivity of low carbon olefin hydrocarbon of catalytic cracking; Further, when the aspect ratio of preferred described sleeve (21) is 0.5-3, the productivity of low carbon olefin hydrocarbon of catalytic cracking can be improved further.
Below the preferred embodiment of the present invention is described in detail by reference to the accompanying drawings; but; the present invention is not limited to the detail in above-mentioned embodiment; within the scope of technical conceive of the present invention; can carry out multiple simple variant to technical scheme of the present invention, these simple variant all belong to protection scope of the present invention.
It should be noted that in addition, each concrete technical characteristic described in above-mentioned embodiment, in reconcilable situation, can be combined by any suitable mode, in order to avoid unnecessary repetition, the present invention illustrates no longer separately to various possible array mode.
In addition, also can carry out arbitrary combination between various different embodiment of the present invention, as long as it is without prejudice to thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (14)
1. a catalytic cracking unit, is characterized in that: this catalytic cracking unit comprises riser reactor (1), settling vessel (3) and stripper (4); Described stripper (4) is positioned at the below of described settling vessel (3) and is integrally formed with described settling vessel (3) and coaxial; Described riser reactor (1) through described stripper (4) bottom and stretch in described settling vessel (3); The cyclonic separator (14) for carrying out finish separation is provided with in described settling vessel (3); Wherein, in the lower cavity of described settling vessel (3), be provided with the sleeve (21) of the upper and lower opening coaxial with this settling vessel (3); The material outlet of described riser reactor (1) is positioned at described sleeve (21) to form fluidized bed reaction zone (2) at described sleeve (21); The dipleg mouth of described cyclonic separator (14) is arranged in the space (5) formed by the inwall of the outer wall of described sleeve (21) and described settling vessel (3); Described fluidized bed reaction zone (2), described space (5) and described stripper (4) be all fluid connections each other.
2. catalytic cracking unit according to claim 1, is characterized in that: the aspect ratio of described sleeve (21) is 0.2-5.
3. catalytic cracking unit according to claim 1, is characterized in that: the lower end of described riser reactor (1) is provided with stock oil feed nozzle (11) and regenerated catalyst (12).
4. catalytic cracking unit according to claim 1, is characterized in that: the described material outlet of described riser reactor (1) is provided with sparger (13).
5. catalytic cracking unit according to claim 1, is characterized in that: described cyclonic separator (14) is 1 or is symmetrically arranged 2-3.
6. catalytic cracking unit according to claim 3, is characterized in that: described catalytic cracking unit also comprises catalyst regenerator (6); Described stripper (4) is provided with the reclaimable catalyst transfer lime (42) be communicated with the catalyst inlet of described catalyst regenerator (6); The regenerated catalyst (12) of described riser reactor (1) is communicated with the catalyst outlet of described catalyst regenerator (6).
7. catalytic cracking unit according to claim 6, is characterized in that: described catalyst regenerator (6) and described settling vessel (3) are set up in parallel.
8. a method for catalytic cracking gasoline hydrocarbon, is characterized in that: the method comprises the steps:
A rise along riser reactor (1) with formation in the bottom of the stock oil after preheating, cracking catalyst and pre-lift gas injecting lift pipe reactor (1) by () the first reaction oil gas logistics;
B described first reaction oil gas logistics is passed through fluidized bed reaction zone (2) to form the second reaction oil gas logistics by (); Wherein, described fluidized bed reaction zone (2) is formed in the sleeve (21) of upper and lower opening, the lower cavity that described sleeve (21) is arranged at settling vessel (3) is interior and coaxial with described settling vessel (3), and the material outlet of described riser reactor (1) is positioned at described sleeve (21);
C described second reaction oil gas logistics is separated into the reclaimable catalyst of gaseous product and carbon distribution by () through cyclonic separator (14); The dipleg outlet of described cyclonic separator (14) is arranged in the space (5) formed by the inwall of the outer wall of described sleeve (21) and described settling vessel (3);
D () makes described reclaimable catalyst carry out stripping from bottom importing stripper (4) of described settling vessel (3); Described stripper (4) is positioned at the below of described settling vessel (3) and is integrally formed with described settling vessel (3) and coaxial; Described riser reactor (1) through described stripper (4) bottom and stretch in described settling vessel (3).
9. method according to claim 8, is characterized in that: the temperature out of described riser reactor (1) is 450-600 DEG C, and top hole pressure is 0.15-0.3MPa, and agent-oil ratio is (4-15): 1, and the reaction times is 1-5 second.
10. method according to claim 8 or claim 9, is characterized in that: the weight ratio of described stock oil and described pre-lift gas is (0.01-2): 1; Described pre-lift gas bag draws together at least one in the alkane of water vapour, nitrogen and C1-C4; The temperature of described pre-lift gas is 180-280 DEG C.
11. methods according to claim 8, is characterized in that: the bed temperature in described fluidized bed reaction zone (2) is 480-620 DEG C, and weight hourly space velocity is 0.2-30h
-1, pressure is 0.15-0.3MPa.
Method described in 12. according to Claim 8 or 11, is characterized in that: the aspect ratio of described sleeve (21) is 0.2-5.
13. methods according to claim 8, is characterized in that: the preheating temperature of described stock oil is 180-400 DEG C; Described stock oil comprises at least one in diesel oil, hydrogenation tail oil, vacuum gas oil, crude oil, long residuum, pressurization residual oil, liquefied coal coil, tar sand oil and shale oil.
14. methods according to claim 8, is characterized in that: the method also comprises: the reclaimable catalyst obtained by stripping imports in catalyst regenerator and carries out coke burning regeneration.
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| CN110628456A (en) * | 2018-06-22 | 2019-12-31 | 中国石油化工股份有限公司 | Catalytic cracking oil separating equipment, reaction regeneration system and application |
| CN111484386A (en) * | 2019-01-28 | 2020-08-04 | 中国科学院大连化学物理研究所 | Raw material conversion device containing naphtha |
| CN111484387A (en) * | 2019-01-28 | 2020-08-04 | 中国科学院大连化学物理研究所 | Method for converting raw material containing naphtha into low-carbon olefin and/or aromatic hydrocarbon |
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| CN109107615A (en) * | 2017-06-23 | 2019-01-01 | 中国石油大学(华东) | A kind of alkane dehydrogenating catalyst regeneration method and regenerating unit |
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| CN109701460B (en) * | 2017-10-26 | 2021-11-16 | 中国石油化工股份有限公司 | Method and system for on-line cyclic regeneration of hydrocracking catalyst |
| CN108636303A (en) * | 2018-05-23 | 2018-10-12 | 安徽国星生物化学有限公司 | A kind of recirculating fluidized bed prepares the consersion unit of pyridine base |
| CN110628456A (en) * | 2018-06-22 | 2019-12-31 | 中国石油化工股份有限公司 | Catalytic cracking oil separating equipment, reaction regeneration system and application |
| CN110628456B (en) * | 2018-06-22 | 2021-10-08 | 中国石油化工股份有限公司 | Catalytic cracking oil separating equipment, reaction regeneration system and application |
| CN111484386A (en) * | 2019-01-28 | 2020-08-04 | 中国科学院大连化学物理研究所 | Raw material conversion device containing naphtha |
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| CN111484387B (en) * | 2019-01-28 | 2021-08-20 | 中国科学院大连化学物理研究所 | Method for converting raw material containing naphtha into low-carbon olefin and/or aromatic hydrocarbon |
| CN111484386B (en) * | 2019-01-28 | 2021-09-21 | 中国科学院大连化学物理研究所 | Raw material conversion device containing naphtha |
| CN111603884A (en) * | 2020-06-22 | 2020-09-01 | 中国石油化工股份有限公司 | System and method for effectively removing impurities carried in catalytic dry gas in ethylbenzene preparation process |
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