CN100469432C

CN100469432C - A Riser Reactor

Info

Publication number: CN100469432C
Application number: CNB2006100080779A
Authority: CN
Inventors: 侯栓弟; 龙军; 许克家; 张久顺; 张占柱; 许友好; 何峻; 武雪峰
Original assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Current assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Priority date: 2006-02-28
Filing date: 2006-02-28
Publication date: 2009-03-18
Anticipated expiration: 2026-02-28
Also published as: CN101028588A

Abstract

A lift-pipe reactor is composed of such units from bottom to top as pre-lifting segment, the first reaction segment, the second reaction segment, and optional discharging segment. It features that a flow guiding pipe is arranged at lower part of the second reaction segment to decrease the gas flow speed in its wall region for generating a dense phase region of catalyst, so increasing the concentration of catalyst in second reaction segment.

Description

A kind of riser reactor

Technical field

The invention belongs to the equipment of hydrocarbon ils catalyzed conversion under the situation that does not have hydrogen, more particularly, the present invention is a kind of riser reactor that is used for fluidized catalytic conversion.

Background technology

Generally adopt isometrical riser reactor in conventional at present catalytic cracking reaction-regenerative system, the feedstock oil of preheating enters riser reactor through feed nozzle, contact, vaporize and react with high temperature catalyst from regenerator, oil gas is taken the average linear speed of catalyst about with 10 meter per seconds and is upwards flowed along riser, the time about about 3 seconds is experienced in reaction while flowing.Constantly there is coke to generate in the course of reaction and is deposited on catalyst surface and the activated centre, activity of such catalysts and selectivity are sharply descended.For this reason, coked catalyst must in time separate and enter regenerator to carry out recycling use behind the coke burning regeneration with reaction oil gas, forms the closed circuit of catalyst.Reaction oil gas then enters piece-rate system and isolates needed product, reacts for the part of required light-end products (being commonly referred to recycle oil) enters riser reactor once more through primary first-order equation is unconverted in the raw material.The basic process of Here it is catalytic cracking reaction-regenerative system.

By great deal of experiment data and industrial practical operation experience, the means and the measure that reduce sulfur in gasoline and olefin(e) centent are to strengthen favourable secondary response in the course of reaction, as isomerization, hydrogen transfer reaction.And conventional riser reactor, the reactor inlet rate of flow of fluid is the 4-5 meter per second, along with the carrying out of cracking reaction, mean molecule quantity reduces, the fluid issuing flow velocity reaches the 15-18 meter per second, and the reaction time has only 2-3 second, has suppressed some secondary responses useful to product quality.In addition, studies show that the catalyst activity in riser exit only reaches about 1/3rd of initial activity at present, after a second was carried out in reaction, activity of such catalysts descended about 50%.In the second half section of riser reactor, catalyst activity and selectivity sharply descend, the catalytic action variation.For this reason, traditional riser need improve, to adapt to the requirement of new catalytic cracking technology.

CN1078094C discloses a kind of novel riser reactor form, strengthens two stages in the Cherry P process respectively by setting up two reaction zones, at first strengthens the cracking of heavy oil by high temperature, short residence time at first reaction zone; Make gasoline fraction that favourable secondary response take place at second reaction zone by low temperature, long reaction time, be mainly isomerization and hydrogen transfer reaction, improve quality of gasoline.Adopt the industrial experiment of this reactor to show, this equipment can reduce olefin content in gasoline greatly, but finds in industrial reality, and its second reaction zone is difficult to reach the density of catalyst that requires in technology and the design, causes this process advantage to fail to fully play.

Summary of the invention

The present invention is exactly on the basis of this industry actual phenomenon and prior art, proposes a kind of novel riser reactor form, to strengthen the secondary response of hydro carbons.

Riser reactor provided by the invention comprises pre lift zone, first conversion zone, second conversion zone and optional outlet section from bottom to top successively, and wherein the bottom of second conversion zone is provided with mozzle.

In the bottom of described pre lift zone pre-lifting dielectric distribution device being set, fixedlys connected with regenerated catalyst and is communicated with in the bottom that promotes the dielectric distribution device in advance.The length of pre lift zone accounts for the 5-25% of total reactor height.

Feed nozzle is arranged on the bottom of first conversion zone.Fixedlying connected and UNICOM with the upper end of pre lift zone in the lower end of first conversion zone, fixedlys connected and UNICOM by the taper type cylindrical shell that a diameter enlarges from bottom to top gradually in the lower end of its upper end and second conversion zone.

The structure of first conversion zone is similar to conventional equal diameter riser reactor, and its diameter is 0.5-2:1 with the ratio of pre lift zone, and it highly accounts for the 20-60% of total reactor height.When the diameter of the diameter of pre lift zone and first conversion zone not simultaneously, both are fixedly connected and be communicated with by taper type cylindrical shell.First conversion zone and the preferred coaxial arrangement of second conversion zone, the cone-apex angle of taper type changeover portion can be 30-120 ° between the two.

The diameter of second conversion zone is 1.25-5.0 a times of the first conversion zone diameter, and it highly accounts for the 15-50% of total reactor height.Mozzle in second conversion zone is fixedly linked by the taper type changeover portion between gusset and second conversion zone and/or first conversion zone and second conversion zone, and coaxial with second conversion zone, forms toroidal cavity between the two.

The lower port of mozzle is positioned at more than the first conversion zone upper port, and distance between the two can be 0.05-1.25 times of the first conversion zone diameter.The length of mozzle can be 0.1-0.95 times of the second conversion zone length.

Mozzle can be a straight tube, also can be the little down big taper type cylindrical shell of, and can also be the change diameter tube that is combined by straight length and taper type cylindrical shell.When mozzle is straight tube, its external diameter can for the 0.65-0.95 of mozzle arrival end equal height place reactor inside diameter doubly; When mozzle is that taper type cylindrical shell and its cone-apex angle are during greater than 30 °, be preferably in perforate on the sidewall of this taper type cylindrical shell, perforated area can be 0.3-1.5 times of the first conversion zone cross-sectional area, the internal diameter of mozzle end opening can for the 0.05-0.25 of end opening equal height place reactor inside diameter doubly, and its diameter suitable for reading can for the 0.85-0.99 of equal height suitable for reading place reactor inside diameter doubly; When mozzle is that taper type cylindrical shell and its cone-apex angle are during smaller or equal to 30 °, the external diameter of its end opening can for the 0.6-0.9 of end opening equal height place reactor inside diameter doubly, and its external diameter suitable for reading can for the 0.65-0.95 of equal height suitable for reading place reactor inside diameter doubly; When mozzle is that the change diameter tube that combined by straight length and taper type cylindrical shell and its entrance are during into a taper type cylindrical shell, the external diameter of its straight length can be 0.7-0.98 times of the reactor second conversion zone internal diameter, the diameter of entrance taper type cylindrical shell should enlarge from the bottom up gradually, the external diameter of this taper type cylindrical shell end opening can for the 0.6-0.95 of end opening equal height place reactor inside diameter doubly, its cone-apex angle can be selected in 15-120 ° scope; When mozzle is that the change diameter tube that combined by straight length and taper type cylindrical shell and its top are when comprising a taper type cylinder section, the external diameter of its straight length can be 0.75-0.98 times of the reactor second conversion zone internal diameter, the diameter of its outlet section taper type cylindrical shell should be diminishing from the bottom up, this taper type cylindrical shell external diameter suitable for reading can for the 0.5-0.9 of equal height suitable for reading place reactor inside diameter doubly, its cone-apex angle can be selected in 10-120 ° scope.

Above mozzle, be provided with tapered or billiard table shape flow apron, can further improve the catalyst concn of second conversion zone.The summit of the center line of reactor by baffle plate is also vertical with the lower surface of baffle plate.Baffle plate lower surface diameter be with the 0.6-0.9 of this end face equal height place reactor inside diameter doubly, the height of this end face distance mozzle upper surface be mozzle upper port diameter 0.25-2.5 doubly.Can perforate at the top of flow apron, to prevent oil gas long-term delay and cause coking below flow apron.The area sum of all perforates is 0.001-0.01 a times of the riser second conversion zone cross-sectional area.

If between draft tube outlets and the flow apron above it, guide vane is set, oil gas and catalyst in the mozzle are tangentially flowed out, then the catalyst concn in reactor second conversion zone can also be further enhanced.The upper and lower end of guide vane is fixedly connected on respectively on flow apron and the mozzle, and the number of guide vane can be the 3-24 sheet, and circulation area total between the blade can be 0.25-2 times of draft tube outlets sectional area.

This riser reactor can be established outlet section, also can not establish outlet section.If do not establish outlet section, the upper end of second conversion zone is directly fixedly connected with gas-solid separator and be communicated with; If establish outlet section, the structure of outlet section is similar to conventional equal diameter riser reactor top exit portion, the diameter ratio of its diameter and first conversion zone is 0.5-1.5:1, it highly accounts for the 0-30% of total reactor height, the cone-apex angle of the taper type changeover portion between this section and second conversion zone can be 30-120 °, fixedly connected by a diminishing from bottom to top taper type cylindrical shell of diameter and be communicated with in the upper end of the lower end of outlet section and second conversion zone, it is terminal fixedly connected with gas-solid separator and be communicated with.

The feedstock oil of this reactor inlet position, in advance promote position, medium inlet, regenerated catalyst inlet position, feedstock oil atomizing type, all the equal diameter riser reactor with routine is identical with the catalyst mix method for feedstock oil, the mode of operation of this reactor and operating condition also are similar to the equal diameter riser reactor of routine.The material of this reactor requires with conventional equal diameter riser reactor identical.

Compare with prior art, the present invention has following characteristics:

1, by in second conversion zone, mozzle being set, reduce the gas flow rate in the second conversion zone Bian Bi district, make the limit wall of second conversion zone form the catalyst emulsion zone.The catalyst of this emulsion zone can be back to the center of second conversion zone under pressure balanced effect, the intensity of circulation of central area catalyst is increased, thereby improve the catalyst concn of center;

2, pass through the barrier effect of mozzle top flow apron, the gas-solid two-phase is changed in the direction of motion of second conversion zone, eliminate the momentum that the gas-solid two-phase moves upward rapidly, slackened the ability that oil gas is taken catalyst out of second conversion zone, and make the part catalyst flow out the back from mozzle to transfer to by moving upward and moving downward at second conversion zone, increased the second conversion zone Bian Bi district and entered the catalyst flow of center, thereby helped further improving the density of catalyst of second conversion zone by backflow;

3, by guide vane being set at the draft tube outlets place, be subjected to the Bian Bi district that action of centrifugal force and Oil-gas Separation fall into second conversion zone when making catalyst granules tangentially enter annular region between the mozzle and the second conversion zone wall, more effectively the fortifying catalytic agent is in the interior circulation of second conversion zone, thereby further improves the concentration of second reacting section catalyst.

Description of drawings

Fig. 1-6 is 6 kinds of embodiments of riser reactor provided by the invention.

Fig. 7-9 is the curve of the second reacting section catalyst average quality concentration with height change.

The specific embodiment

Below in conjunction with accompanying drawing riser reactor provided by the present invention is given further instruction.Below several embodiments just for the present invention will be described in detail, the mozzle wherein and the form of flow apron can make up respectively, therefore are not restricted.

Fig. 1 to Fig. 6 is the preferred 6 kinds of embodiments of the present invention.Each label is represented respectively among the figure:

1-promotes the dielectric distribution device in advance; The 2-pre lift zone; 3-regenerated catalyst flow control valve; The 4-regenerated catalyst; The 5-feed nozzle; Taper type extension diameter section between 6-first conversion zone and second conversion zone; The 7-mozzle; The connection gusset of 8-fixed diversion pipe; 9-second conversion zone; Taper type undergauge section between 10-second conversion zone and the outlet section; The 11-outlet section; The 12-flow apron; 13-is the connection gusset of flow apron fixedly; The taper type extension diameter section of 14-mozzle bottom; The taper type undergauge section on 15-mozzle top; The 16-guide vane; The perforate at 17-baffle plate top; Perforate on the 18-mozzle; 19-first conversion zone; Communicating pipe between 20-reactor and the gas-solid separator.

Fig. 1 is first kind of embodiment of the present invention.Mozzle 7 is a straight-run of pipe in this embodiment.

Fig. 2 is second kind of embodiment of the present invention.The difference of this embodiment and first kind of embodiment is that the top of mozzle 7 is provided with flow apron 12, and this baffle plate is taper.

Fig. 3 is the third embodiment of the present invention.The difference of this embodiment and the second way is the expansion tube that its mozzle 7 enlarges from bottom to top gradually for diameter, and the flow apron 12 of mozzle top is a billiard table shape plate.

Fig. 4 is the 4th a kind of embodiment of the present invention.The difference of this embodiment and the third embodiment is that the sidewall of mozzle 7 is provided with perforate 18, and is provided with perforate 17 at the top of billiard table shape flow apron 12.

Fig. 5 is the 5th a kind of embodiment of the present invention.The difference of this embodiment and second kind of embodiment is that an extension diameter section 14 and undergauge section 15 are respectively arranged at the bottom and the top of mozzle 7.

Fig. 6 is the 6th a kind of embodiment of the present invention, the difference of this embodiment and the 5th kind of embodiment is that guide vane 16 is set between the flow apron above draft tube outlets and the mozzle 12, makes the mozzle inner fluid by tangentially flowing out after the guide vane guiding.

The feedstock oil that this reactor is suitable for can be petroleum distillate, residual oil or the crude oil of different boiling ranges, and specifically, they are: the time processing distillate comprises gasoline, diesel oil, decompressed wax oil, residual oil etc.; The mixture of the arbitrary proportion of two or more above-mentioned time processing distillate; Be mixed with time processing distillate or its mixture of wax tailings, deasphalted oil or other secondary operations distillate; Crude oil.

Reactor provided by the invention is suitable for the catalyst of all existing types, for example active component is selected from the Y that contains or do not contain rare earth or HY type zeolite, the ultrastable that contains or do not contain rare earth, ZSM-5 series zeolite or the silica-rich zeolite that makes with other method with five-membered ring structure in a kind of, two or three catalyst, and amorphous silicon aluminium catalyst.

Reactor of the present invention can be used to produce different purpose products, for example produces the low-alkene gasoline that is rich in isoparaffin; Produce an amount of propylene and the low-alkene gasoline that is rich in isoparaffin; Produce the gas alkene and the gasoline that is rich in aromatic hydrocarbons of maximum yield; Produce the diesel oil of maximum yield; Catalytic pyrolysis and Deep Catalytic Cracking process combination etc.

Below in conjunction with accompanying drawing riser reactor operating process provided by the present invention is given further instruction.

The pre-medium that promotes enters from pre lift zone 2 through pipeline, and the regenerated catalyst of heat enters pre lift zone 2 through regenerated catalyst 4 and promoted by pre-lifting medium.Feedstock oil after the preheating and atomizing steam enter from nozzle 5 through pipeline, and enter in first conversion zone 19 after thermocatalyst mixes, and carry out cracking reaction under certain conditions.Reactant stream enters second conversion zone 9 by mozzle 7, and changes flow direction under the effect of flow apron 12, and the gas-solid two-phase changes into downwards, flows to the wall direction by upwards flowing.Since turning to suddenly of oil gas and falling sharply of the momentum that makes progress, the entrained catalyst ability drop, and part catalyst and oil gas break away from, and at the annular space regional subsidence of the mozzle 7 and the second conversion zone wall, form the local emulsion zone of catalyst.Because the difference of the interior exterior domain density of catalyst of mozzle 7, the catalyst granules of the outer annular space emulsion zone of mozzle 7 enters mozzle 7 by the interval region of mozzle 7 and first conversion zone, 19 risers, form the interior circulation of catalyst, strengthened the circulation intensity of catalyst, help strengthening the density of catalyst in the second conversion zone zone, increased the contact probability of oil gas and catalyst, helped hydrocarbon ils and carry out secondary response.The reaction logistics flows out through horizontal tube at last, carries out the final of gas-solid two-phase by cyclone separator and settler and separates.

The following examples will give further instruction to the present invention, but not thereby limiting the invention.The character of employed feedstock oil and catalyst is listed in table 1 and table 2 respectively in embodiment, the Comparative Examples.Catalyst in the table 2 is produced by China PetroChemical Corporation's Shandong catalyst plant, and its trade names are MLC-500.

Embodiment 1

Riser reactor shown in Figure 3 provided by the invention, the situation that the catalyst averag density changes vertically in riser second conversion zone that records are by experiment adopted in the present embodiment explanation on the cold mould experimental provision of fluidization.

The total height of testing used riser reactor is 13.5 meters, and its pre lift zone internal diameter is 0.25 meter, highly is 2.5 meters; The first conversion zone internal diameter is 0.2 meter, highly is 4 meters; The second conversion zone internal diameter is 0.5 meter, highly is 5 meters; The internal diameter of outlet section is 0.2 meter, highly is 2 meters; The extension diameter section between first conversion zone and second conversion zone and the cone-apex angle of the undergauge section between second conversion zone and the outlet section are 60 °; The external diameter of mozzle lower end is 0.25 meter, and internal diameter is 0.24 meter, and the external diameter of upper end is 0.35 meter, and internal diameter is 0.34 meter, and the spacing on its lower end and the first conversion zone top is 0.2 meter, and the height of mozzle is 1 meter; The height of billiard table shape baffle plate is 0.16 meter, and the diameter of its lower surface is 0.4 meter, is positioned at above 0.8 meter of draft tube outlets end.The catalyst recycle intensity of second conversion zone is 38.4kg/m during experiment ²S, gas average apparent linear speed is 1.5m/s.Experiment records second conversion zone (be called for short two anti-) catalyst average quality concentration with the curve of height change as shown in Figure 7.

Embodiment 2

Riser reactor shown in Figure 4 provided by the invention, the situation that the catalyst averag density changes vertically in riser second conversion zone that records are by experiment adopted in the present embodiment explanation on the cold mould experimental provision of fluidization.

The total height of testing used riser reactor is 13.5 meters, and its pre lift zone internal diameter is 0.25 meter, highly is 2.5 meters; The first conversion zone internal diameter is 0.2 meter, highly is 4 meters; The second conversion zone internal diameter is 0.5 meter, highly is 5 meters; The internal diameter of outlet section is 0.2 meter, highly is 2 meters; The extension diameter section between first conversion zone and second conversion zone and the cone-apex angle of the undergauge section between second conversion zone and the outlet section are 90 °; The height of taper type mozzle is 0.5 meter.The external diameter of its lower end is 0.03 meter, and internal diameter is 0.02 meter; The external diameter of its upper end is 0.49 meter, and internal diameter is 0.48 meter.On the sidewall of this mozzle, have the circular hole of 80 diameter 20mm equably.The spacing on the mozzle lower end and the first conversion zone top is 0.05 meter.Billiard table shape height of baffle plate is 0.2 meter, and the diameter of its lower surface is 0.45 meter, is positioned at above 1.2 meters of draft tube outlets end.Be provided with the through hole of 10 millimeters of 5 diameters at the top of billiard table shape baffle plate.The catalyst recycle intensity of second conversion zone is 38.5kg/m during experiment ²S, gas average apparent linear speed is 1.5m/s.Experiment records second conversion zone (be called for short two anti-) catalyst average quality concentration with the curve of height change as shown in Figure 8.

Embodiment 3

Riser reactor shown in Figure 6 provided by the invention, the situation that the catalyst averag density changes vertically in riser second conversion zone that records are by experiment adopted in the present embodiment explanation on the cold mould experimental provision of fluidization.

The total height of testing used riser reactor is 13.5 meters, and its pre lift zone internal diameter is 0.25 meter, highly is 2.5 meters; The first conversion zone internal diameter is 0.2 meter, highly is 4 meters; The second conversion zone internal diameter is 0.5 meter, highly is 5 meters; The internal diameter of outlet section is 0.2 meter, highly is 2 meters; The extension diameter section cone-apex angle that connects between first conversion zone and second conversion zone is 60 °, and the cone-apex angle that connects the undergauge section between second conversion zone and the outlet section is 120 °; The total height of combination shape mozzle is 3.56 meters.The bottom of mozzle is the taper type extension diameter section, and its cone-apex angle is 45 °.The external diameter of the lower port of mozzle is 0.25 meter, and internal diameter is 0.24 meter, is positioned at 0.15 meter of upper port of distance first conversion zone.The external diameter of its upper end is 0.45 meter, and internal diameter is 0.44 meter.The external diameter of mozzle straight length is 0.45 meter, and internal diameter is 0.44 meter.The cone-apex angle of the undergauge section of straight length top is 60 °, and the external diameter of its lower end is 0.45 meter, and internal diameter is 0.44 meter, and the upper end external diameter is 0.3 meter, and internal diameter is 0.29 meter.The conical baffled cone-apex angle in mozzle top is 60 °, and the diameter of its lower surface is 0.35 meter, is positioned at the above 250 millimeters places of draft tube outlets end.Between draft tube outlets and flow apron, be provided with 4 guide vanes.The height of guide vane is 250 millimeters, and radius of curvature is 150 millimeters, and radian is 140 °, and the circulation passage that adjacent two guide vanes constitute the spacing at narrow place is 36 millimeters.The catalyst recycle intensity of second conversion zone is 38.2kg/m during experiment ²S, gas average apparent linear speed is 1.5m/s.Experiment records second conversion zone (be called for short two anti-) catalyst average quality concentration with the curve of height change as shown in Figure 9.

Comparative Examples 1

The surface structure of the reactor that Comparative Examples is used and size and embodiment 1-3 are basic identical, just in second conversion zone of Comparative Examples mozzle and flow apron are not set, be provided with perforate distribution grid in the bottom of second conversion zone but resemble the prior art, the perforated area of this perforate distribution grid is 0.8 times of the first conversion zone riser sectional area.Operating condition during experiment is identical with embodiment 1-3.Experiment records catalyst in reactor average quality concentration and sees Fig. 7-9 with the curve that height for reactor changes.By Fig. 7-9 as can be seen, adopt reactor provided by the invention, under the identical operations condition, second conversion zone is that the catalyst average quality concentration of catheter interior or conduit outside all is significantly improved.

Embodiment 4

The present embodiment explanation is adopted riser reactor form shown in Figure 1 provided by the invention on medium-sized tester, use catalyst and decompressed wax oil to carry out the cracking hydrocarbon oil result of experiment.

The pre lift zone of reactor, first conversion zone, second conversion zone, outlet section total height are 6 meters, and the pre lift zone internal diameter is 16 millimeters, highly are 0.5 meter; The first conversion zone internal diameter is 16 millimeters, highly is 2.5 meters; The second conversion zone interior diameter is 35 millimeters, highly is 2 meters; The internal diameter of outlet section is 16 millimeters, highly is 1 meter; Extension diameter section cone-apex angle between first conversion zone and second conversion zone is 60 °, and the extension diameter section cone-apex angle of the undergauge section between second conversion zone and the outlet section is 90 °; The mozzle external diameter is 27 millimeters, and internal diameter is 23 millimeters, highly is 1.5 meters, and the spacing on the mozzle lower end and the first conversion zone top is 15 millimeters.Operating condition and product distribute and list in table 3, and gasoline products character is listed in table 4.

Embodiment 5

The present embodiment explanation is adopted riser reactor form shown in Figure 2 provided by the invention on medium-sized tester, use catalyst and decompressed wax oil to carry out the cracking hydrocarbon oil result of experiment.

The pre lift zone of reactor, first conversion zone, second conversion zone, outlet section total height are 6 meters, and the pre lift zone internal diameter is 16 millimeters, highly are 0.5 meter; The first conversion zone internal diameter is 16 millimeters, highly is 2.5 meters; The second conversion zone interior diameter is 35 millimeters, highly is 2 meters; The internal diameter of outlet section is 16 millimeters, highly is 1 meter; Extension diameter section cone-apex angle between first conversion zone and second conversion zone is 90 °, and the undergauge section cone-apex angle between second conversion zone and the outlet section is 120 °; The mozzle internal diameter is 25 millimeters, and external diameter is 30 millimeters, and length is 1 meter.The spacing on the mozzle lower end and the first conversion zone top is 10 millimeters.The conical baffled cone-apex angle of mozzle top is 60 °, and its lower surface is positioned at above 30 millimeters places, mozzle upper surface, and diameter is 30 millimeters.Operating condition and product distribute and list in table 3, and gasoline products character is listed in table 4.

Embodiment 6

The present embodiment explanation is adopted riser reactor form shown in Figure 5 provided by the invention on medium-sized tester, use catalyst and decompressed wax oil to carry out the cracking hydrocarbon oil result of experiment.

The pre lift zone of reactor, first conversion zone, second conversion zone, outlet section total height are 6 meters, and the pre lift zone internal diameter is 16 millimeters, highly are 0.5 meter; The first conversion zone internal diameter is 16 millimeters, highly is 2.5 meters; The second conversion zone interior diameter is 35 millimeters, highly is 2 meters; The internal diameter of outlet section is 16 millimeters, highly is 1 meter; Extension diameter section cone-apex angle between first conversion zone and second conversion zone is 30 °, and the undergauge section cone-apex angle between second conversion zone and the outlet section is 90 °; The total height of combination shape mozzle is 1.5 meters.The bottom of mozzle is the taper type extension diameter section, and its cone-apex angle is 45 °.The external diameter of this frustum lower end is 20 millimeters, and internal diameter is 17 millimeters.20 millimeters of the mozzle lower port distance first conversion zone ports of export.28 millimeters of the internal diameters of mozzle middle part straight length, 31 millimeters of external diameters.The cone-apex angle of mozzle top undergauge section is 90 °, and its upper end external diameter is 24 millimeters, and internal diameter is 21 millimeters.The conical baffled cone-apex angle of mozzle top is 90 °, and its lower surface diameter is 28 millimeters, is positioned at above 25 millimeters places, mozzle upper surface.Have the through hole of 3 millimeters of diameters at the top of this baffle plate.Operating condition and product distribute and list in table 3, and gasoline products character is listed in table 4.

Comparative Examples 2

Compare with embodiment 4-6, different is that the reactor that this Comparative Examples is used does not have interior mozzle and flow apron, the top and the second conversion zone porch at the changeover portion round platform are provided with the macropore distribution grid, the perforated area of macropore distribution grid is identical with the first conversion zone riser sectional area, and other operating condition is identical with embodiment 4-6.Operating condition and product distribute and list in table 3, and gasoline products character is listed in table 4.From table 3 and table 4 as can be seen, adopt method provided by the invention, hydrocarbon oil conversion is that the productive rate of high value added product (liquefied gas+gasoline+diesel oil) has improved 1.3 percentage points, and the olefin(e) centent of gasoline can be reduced to below 25%, and gasoline MON has increased by 1 more than the unit.

Table 1

Density (20 ℃), kilogram/rice ³	986.0
Density (20 ℃), kilogram/rice ³	986.0	Kinematic viscosity (100 ℃), millimeter ²/ second	84.5
Freezing point, ℃	43.7	Kinematic viscosity (100 ℃), millimeter ²/ second	84.5
Freezing point, ℃	43.7	Carbon residue, heavy %	7.3
Sulfur content, heavy %	0.98	Carbon residue, heavy %	7.3
Sulfur content, heavy %	0.98	Nitrogen content, heavy %	0.21
Carbon content, heavy %	87.1	Nitrogen content, heavy %	0.21
Carbon content, heavy %	87.1	Hydrogen content, heavy %	12.2
Content of beary metal, ppm		Hydrogen content, heavy %	12.2
Content of beary metal, ppm		Nickel	4.3
Iron	2.1	Nickel	4.3
Iron	2.1	Vanadium	0.01
Boiling range, ℃		Vanadium	0.01
Boiling range, ℃		Initial boiling point	386
5％	402	Initial boiling point	386
5％	402	10％	477
30％	498	10％	477
30％	498	500 ℃ distillate v%	35.6
Characterization factor	11.8	500 ℃ distillate v%	35.6

Table 2

Chemical composition, heavy %
Chemical composition, heavy %		Aluminium oxide	56.7
Sodium oxide molybdena	0.07	Aluminium oxide	56.7
Sodium oxide molybdena	0.07	Apparent density, kilogram/rice ³	866
Pore volume, milliliter/gram	0.31	Apparent density, kilogram/rice ³	866
Pore volume, milliliter/gram	0.31	Specific area, rice ²/ gram	308
Abrasion index, %/hour	1.3	Specific area, rice ²/ gram	308
Abrasion index, %/hour	1.3	Nickel contamination, ppm	437
800 ℃ of micro-activities, 4 hours	62.0	Nickel contamination, ppm	437
800 ℃ of micro-activities, 4 hours	62.0	Size consist, heavy %
＜20 microns	3.1	Size consist, heavy %
＜20 microns	3.1	The 20-40 micron	22.4
The 40-80 micron	56.1	The 20-40 micron	22.4
The 40-80 micron	56.1	The 80-110 micron	12.9
110 microns	5.5	The 80-110 micron	12.9

Table 3

	Embodiment 4	Embodiment 5	Embodiment 6	Comparative Examples 2
	Embodiment 4	Embodiment 5	Embodiment 6	Comparative Examples 2	Reaction temperature, ℃
First conversion zone	520	520	520	520	Reaction temperature, ℃
First conversion zone	520	520	520	520	Second conversion zone	501	500	505	498
Reaction time, second					Second conversion zone	501	500	505	498
Reaction time, second					First conversion zone, second	1	1	1	1
Second conversion zone, second	3.5	3.5	3.8	3.5	First conversion zone, second	1	1	1	1
Second conversion zone, second	3.5	3.5	3.8	3.5	Outlet area, second	0.5	0.5	0.5	0.5
Oil ratio	5	5	5	5	Outlet area, second	0.5	0.5	0.5	0.5
Oil ratio	5	5	5	5	Product distributes, heavy %
Dry gas	1.89	1.83	1.92	1.82	Product distributes, heavy %
Dry gas	1.89	1.83	1.92	1.82	Cracked gas	18.62	17.95	19.25	17.41
Gasoline	46.02	45.82	46.32	45.45	Cracked gas	18.62	17.95	19.25	17.41
Gasoline	46.02	45.82	46.32	45.45	Diesel oil	22.87	23.27	22.01	23.32
Heavy oil	5.54	6.30	5.01	7.22	Diesel oil	22.87	23.27	22.01	23.32
Heavy oil	5.54	6.30	5.01	7.22	Coke	4.58	4.33	4.96	4.35
Loss	0.48	0.50	0.53	0.43	Coke	4.58	4.33	4.96	4.35

Table 4

Character	Embodiment	4	Embodiment 5	Embodiment 6	Comparative Examples 2
Character	Embodiment	4	Embodiment 5	Embodiment 6	Comparative Examples 2	Density (20 ℃), kilogram/rice ³	720.8	720.8	720.8	718.8
Octane number						Density (20 ℃), kilogram/rice ³	720.8	720.8	720.8	718.8
Octane number					RON	90.6	90.4	90.8	90.4
MON	81.2	81.1	81.9	80.2	RON	90.6	90.4	90.8	90.4
MON	81.2	81.1	81.9	80.2	Induction period, minute	>1000	>1000	>1000	>1000
Sulfur content, ppm	37	57	30	85	Induction period, minute	>1000	>1000	>1000	>1000
Sulfur content, ppm	37	57	30	85	Nitrogen content, ppm	3	5	2	8
Boiling range, ℃					Nitrogen content, ppm	3	5	2	8
Boiling range, ℃					Initial boiling point	41	40	40	39
10％	58	56	55	57	Initial boiling point	41	40	40	39
10％	58	56	55	57	50％	97	96	98	96
90％	188	186	187	185	50％	97	96	98	96
90％	188	186	187	185	Do	202	201	200	200
Hydrocarbon composition, heavy %					Do	202	201	200	200
Hydrocarbon composition, heavy %					N-alkane	5.07	5.23	4.98	5.3
Isoparaffin	36.31	36.25	37.25	36.55	N-alkane	5.07	5.23	4.98	5.3
Isoparaffin	36.31	36.25	37.25	36.55	Aromatic hydrocarbons	27.56	26.44	30.19	23.05
Cycloalkane	7.70	7.32	7.55	7.25	Aromatic hydrocarbons	27.56	26.44	30.19	23.05
Cycloalkane	7.70	7.32	7.55	7.25	Alkene	23.36	24.15	20.03	27.85

Claims

1. A riser reactor, which comprises a pre-lift section, a first reaction section, a second reaction section and an optional outlet section from bottom to top, and is characterized in that the bottom of the second reaction section is provided with a guide The lower port of the guide tube is located above the upper port of the first reaction section, the distance between the two is 0.05-1.25 times the diameter of the first reaction section, and the length of the guide tube is 0.1-1.25 times the length of the second reaction section. 0.95 times.

2. The reactor according to claim 1, characterized in that a diversion baffle is arranged above said diversion pipe.

3. A reactor according to claim 2, characterized in that guide vanes are provided between the outlet of said draft tube and the guide baffle.

4. The reactor according to claim 1, 2 or 3, characterized in that the guide pipe is a straight pipe, a truncated cone-shaped cylinder or a variable-diameter pipe composed of a straight pipe section and a truncated-conical cylinder.

5. The reactor according to claim 4, wherein the draft pipe is a straight pipe section, and the outer diameter of the straight pipe section is 0.65-0.95 times the inner diameter of the reactor at the same height as the inlet end of the draft pipe.

6. The reactor according to claim 4, characterized in that the guide pipe is a truncated cone-shaped cylinder with an angle greater than 30°, and holes are opened on the side wall of the truncated cone-shaped cylinder, and the area of the holes is the second 0.3-1.5 times the cross-sectional area of a reaction section, while the diameter of the lower opening of the draft tube is 0.05-0.25 times the inner diameter of the reactor at the same height as the lower opening, and the diameter of the upper opening of the draft tube is at the same height as the upper opening 0.85-0.99 times the inner diameter of the reactor.

7. The reactor according to claim 4, characterized in that the draft tube is a truncated cone-shaped cylinder and its cone angle is less than 30°, and the outer diameter of the lower opening of the tube is 0.6-30° of the inner diameter at the same height of the reactor. 0.9 times, the outer diameter of the upper opening of the draft tube is 0.65-0.95 times the inner diameter at the same height of the reactor.

8. The reactor according to claim 4, characterized in that the guide pipe is a straight pipe section in the middle, and the inlet section and/or outlet section of the guide pipe are variable-diameter pipes composed of frustum-shaped cylinders. The outer diameter of the pipe section is 0.7-0.98 times the inner diameter of the second reaction section of the reactor.

9. The reactor according to claim 8, characterized in that the inlet section of the draft pipe is a frustum-shaped cylinder, the diameter of the frustum-shaped cylinder gradually expands from bottom to top, and its apex angle is 15- 120°, the outer diameter of the lower opening of the frustum-shaped cylinder is 0.6-0.95 times the inner diameter of the reactor at the same height as the lower opening.

10. The reactor according to claim 8, characterized in that the outlet section of the draft pipe is a truncated cone-shaped cylinder, the diameter of the truncated cone-shaped cylinder gradually decreases from bottom to top, and its cone angle is 10- 120°, the outer diameter of the upper opening of the frustum-shaped cylinder is 0.5-0.9 times the inner diameter of the reactor at the same height as the upper opening.

11. The reactor according to claim 2, characterized in that said diversion baffle is a cone-shaped or spherical table-shaped diversion baffle, and the apex of said cone-shaped or spherical table-shaped diversion baffle passes through the centerline of the reactor, Its lower end face is perpendicular to the centerline of the reactor, the diameter of the end face is 0.6-0.9 times the inner diameter of the reactor at the same height as the end face, the position of the end face is lower than the upper end face of the second reaction section and the distance from the upper end face of the draft tube The height is 0.25-2.5 times of the port diameter on the draft tube.

12. The reactor according to claim 2 or 11, characterized in that holes are opened at the top of the guide baffle, and the sum of the areas of all the holes is 0.001-0.01 times the cross-sectional area of the second reaction section of the riser.

13. The reactor according to claim 3, characterized in that the upper and lower ends of the guide vanes are respectively fixedly connected to the guide baffle and the guide pipe, the number of the vanes is 3-24, and the total flow area between the vanes is It is 0.25-2 times of the cross-sectional area of the outlet of the draft tube.