CN110961043A - Riser catalytic cracking unit - Google Patents
Riser catalytic cracking unit Download PDFInfo
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- CN110961043A CN110961043A CN201811156818.7A CN201811156818A CN110961043A CN 110961043 A CN110961043 A CN 110961043A CN 201811156818 A CN201811156818 A CN 201811156818A CN 110961043 A CN110961043 A CN 110961043A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/38—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
- B01J8/384—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only
- B01J8/388—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only externally, i.e. the particles leaving the vessel and subsequently re-entering it
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/245—Spouted-bed technique
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
- C10G11/04—Oxides
- C10G11/05—Crystalline alumino-silicates, e.g. molecular sieves
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
- C10G11/182—Regeneration
Abstract
A riser catalytic cracking unit comprising: the inlet end of the riser reactor is communicated with the atomizing nozzle, and the outlet end of the riser reactor is communicated with the stripper; a catalyst regenerator comprising a catalyst inlet in communication with the stripper and a catalyst outlet in communication with the riser reactor; the riser reactor sequentially comprises a first reaction zone and a second reaction zone from an inlet end to an outlet end, the inlet end of the first reaction zone is communicated with the atomizing nozzle, the outlet end of the first reaction zone is communicated with the second reaction zone, the inlet end to the outlet end of the first reaction zone sequentially comprises a non-diameter-variable structure and a diameter-variable structure, and the diameter-variable structure sequentially comprises a diameter-expanding structure, an equal-diameter structure and a diameter-reducing structure from the inlet end of the first reaction zone to the outlet end of the first reaction zone.
Description
Technical Field
The invention belongs to the field of catalytic cracking, and relates to a riser catalytic cracking device.
Background
Catalytic cracking is one of the most important heavy oil upgrading processes. The catalytic cracking process has the advantages of low investment, low operation cost, strong raw material adaptability, high yield of light products and mature technology, and is the main source of profits of the current oil refineries (Zulihua. the current development situation and the prospect of the catalytic cracking technology in China [ J ]. petrochemical engineering technology economy, 2000, 16 (1): 16-21.). At present, the annual processing capacity of catalytic cracking in China exceeds 1 hundred million t, and in the composition of commercial gasoline, the catalytic cracking gasoline accounts for about 80 percent, the diesel oil accounts for about 30 percent, and more than 30 percent of propylene comes from the catalytic cracking process. The status and the role spread of catalytic cracking in oil refineries [ J ] in petroleum institute (petroleum processing), 2003,19(1):1-11.) were stated as the important roles of catalytic cracking as the main heavy oil lightening process, and still continue to play the backbone role, respectively, by the hou fusheng academy (hou.s.: 1-5.) and chen warrio academy (chen, well-safeguarded.: the role of catalytic cracking in oil refineries [ J ]. petroleum institute (petroleum processing), 2003,19(1): 1-11.).
Propylene is an important basic organic synthetic feedstock and market demand has grown year by year. At present, the main source (about 70 percent) of propylene is still a process for preparing ethylene by steam cracking by using naphtha, light diesel oil, liquefied petroleum gas and other light petroleum hydrocarbons as raw materials, and due to the restriction of the reaction mechanism of the process, the yield of the propylene serving as a main byproduct is difficult to greatly improve; due to the intervention of the catalyst, the fluidized catalytic cracking process has the advantages of wide raw materials, low reaction temperature, low energy consumption, mild operation conditions and the like, and the reaction is carried out according to the carbonium ion mechanism in the process, so that the content of propylene and butylene in gas products is high, and the process plays an important role in the aspect of producing propylene.
At present, the technology for producing propylene by catalytic cracking of heavy oil developed at home and abroad is based on the conventional catalytic cracking process, adopts catalysts or auxiliaries containing shape-selective molecular sieves in different proportions, and selects the operating conditions of high temperature and large catalyst-oil ratio. The specific process form comprises the following steps: the method realizes the high yield of propylene on a conventional catalytic cracking unit by selecting a proper catalyst and adjusting the operating conditions; recycling naphtha (comprising light hydrocarbons such as C4-C8) at a certain part of a riser reactor of a conventional catalytic cracking unit; reforming a single riser reactor and feeding naphtha at the bottom of a riser for recycling; in the conventional catalytic cracking unit, a riser or other fluidized bed reactor is additionally added to recover naphtha.
According to the literature reports, patents CN1279270, CA2186744, CN1237477, CN1031834, US4980053, US3928172, CN1069054, US6569316 and cn200610080831.x respectively describe various production technologies capable of increasing the yield of low-carbon olefins, improving the quality of gasoline, and improving the reaction conditions and product distribution of heavy oil raw materials, but the process technologies for producing propylene in an increased way by using heavy oil as a raw material mainly can be divided into three major categories:
(1) based on the conventional catalytic cracking process, the form of a single riser reactor is modified, and the catalytic cracking naphtha or other light hydrocarbons are recycled in a certain mode. Propylene yields of these techniques are typically below 10%, and too high a propylene yield results in a significant increase in dry gas and coke yields.
(2) On the basis of the conventional catalytic cracking process, a riser or other fluidized bed reactor is additionally arranged to recycle naphtha or other light hydrocarbons under the harsher operating conditions. The yield of propylene relative to heavy oil feedstock of this type of technology is also difficult to exceed 15%, otherwise the same is faced with a significant increase in dry gas and coke yields.
(3) On the basis of the conventional catalytic cracking process, a riser or other fluidized bed reactor is additionally arranged to recycle naphtha and other hydrocarbons under milder operating conditions. CN200610080831.X discloses a method for producing propylene and high-quality gasoline and diesel oil by two-stage catalytic cracking, which mainly utilizes two-stage riser catalytic process, adopts catalyst rich in shape-selective molecular sieve, takes heavy petroleum hydrocarbon or various animal and vegetable oils rich in hydrocarbon as raw materials, carries out optimized combination of feeding modes aiming at reaction materials with different properties, controls the reaction conditions suitable for different materials, and can achieve the purposes of improving the propylene yield, giving consideration to the light oil yield and quality and inhibiting the generation of dry gas and coke. However, the first-stage feeding and the second-stage feeding of the process both react with the regenerated catalyst, the surface of the regenerated catalyst is also provided with uneven strong acid centers, the probability of generating coke during the contact reaction with materials is greatly increased, the yield of the coke is increased, and the energy consumption is increased.
At present, the main systems for the development of riser reactors in process engineering are as follows: the improvement of a raw material atomizing nozzle, the sectional feeding of raw materials along a riser, a rapid oil separation technology at the outlet of the riser and the like, but reports on the structural improvement of combined feeding and an initial oil contact section at the lower part of the riser are still less.
The patent USP4820493, USP5318691, CN1056543C, CN1058046C, CN2415832Y, CN1191325C, CN1078094C and the like disclose riser reactor structures mainly based on the improvement of the riser structure and the diameter change of the middle upper part of the riser. CN2010100343910 and CN 201010169726 disclose reducing at the lower part of a lifting section, but the feeding mode of the lifting section is dense phase section feeding, and the activity of a regenerated catalyst in a dense phase section is higher, so that coke is easily generated; the latter is to divide the catalytic cracking mixed raw material into vacuum wax oil and vacuum residue oil feed to improve the yield of light oil, but the vacuum residue oil is used as the catalytic cracking raw material, so the device is difficult to operate for a long period.
Disclosure of Invention
The invention mainly aims to provide a riser catalytic cracking device to overcome the defect of high yield of dry gas and coke in the catalytic cracking process in the prior art.
In order to achieve the above object, the present invention provides a riser catalytic cracking apparatus comprising:
the inlet end of the riser reactor is communicated with the atomizing nozzle, and the outlet end of the riser reactor is communicated with the stripper;
a catalyst regenerator comprising a catalyst inlet in communication with the stripper and a catalyst outlet in communication with the riser reactor;
the riser reactor sequentially comprises a first reaction zone and a second reaction zone from an inlet end to an outlet end, the inlet end of the first reaction zone is communicated with the atomizing nozzle, the outlet end of the first reaction zone is communicated with the second reaction zone, the inlet end to the outlet end of the first reaction zone sequentially comprises a non-diameter-variable structure and a diameter-variable structure, and the diameter-variable structure sequentially comprises a diameter-expanding structure, an equal-diameter structure and a diameter-reducing structure from the inlet end of the first reaction zone to the outlet end of the first reaction zone.
The riser catalytic cracking apparatus of the present invention, wherein the atomizing nozzle comprises:
the nozzle comprises a nozzle main body, a nozzle body and a nozzle body, wherein the nozzle main body is a three-layer sleeve composed of an inner pipe, an intermediate pipe and an outer pipe, the two ends of the three-layer sleeve are respectively an inlet end and an outlet end, the inlet end of the inner pipe is provided with a raw oil inlet, the inlet end of the intermediate pipe is provided with a dispersion medium inlet, and the inlet end of the outer pipe is provided with a light raw material inlet;
a first nozzle tip connected to the outlet end of the inner tube, the first nozzle tip having a cross-sectional area that gradually decreases in a direction away from the inner tube;
a second nozzle tip connected to the outlet end of the intermediate pipe, the second nozzle tip having a cross-sectional area that gradually decreases in a direction away from the intermediate pipe;
the third nozzle head is arranged at the outlet end of an annular channel formed by the outer wall of the intermediate pipe and the inner wall of the outer pipe;
wherein, one end of the second nozzle head far away from the intermediate pipe protrudes a first distance than one end of the first nozzle head far away from the inner pipe, and one end of the first nozzle head far away from the inner pipe protrudes a second distance than one end of the third nozzle head far away from the outer pipe; at least one bulge is arranged on the inner wall of the intermediate pipe.
The outlet end of the intermediate pipe protrudes a distance from the outlet end of the inner pipe, the outlet end of the inner pipe protrudes a distance from the outlet end of the outer pipe, the second nozzle head wraps the first nozzle head, the vertical distance from one end of the first nozzle head far away from the inner pipe to one end of the second nozzle head far away from the intermediate pipe is 0.006-0.1 m, and the vertical distance from one end of the third nozzle head far away from the outer pipe to one end of the first nozzle head far away from the inner pipe is 0.005-1.00 m.
The riser catalytic cracking device is characterized in that the three layers of sleeves are cylindrical sleeves, the first nozzle head and the second nozzle head are both hollow conical trapezoids, the third nozzle head is annular, and the inner pipe, the intermediate pipe, the outer pipe, the first nozzle head, the second nozzle head and the third nozzle head have the same longitudinal center line.
The riser catalytic cracking device is characterized in that one end of the first nozzle head, which is far away from the inner pipe, is of a first plane structure, one end of the second nozzle head, which is far away from the intermediate pipe, is of a second plane structure, one end of the third nozzle head, which is far away from the outer pipe, is of a third plane structure, and a plurality of holes are formed in the first plane structure, the second plane structure and the third plane structure.
The riser catalytic cracking device is characterized in that the included angle between the trapezoidal surface of the first nozzle head and the inner pipe is β -60 degrees, the included angle between the trapezoidal surface of the second nozzle head and the intermediate pipe is α -70 degrees, the sum of α and β is 90 degrees, the space from one end of the first nozzle head far away from the inner pipe to one end of the second nozzle head far away from the intermediate pipe is a mixing chamber, and the mixing chamber is used for mixing raw oil and a dispersion medium.
The longitudinal section of the bulge is one or more of square, semi-circle and ellipse, the bulge is positioned on the inner wall of the intermediate pipe, and the distance between the bulge and the outlet end of the side wall of the intermediate pipe accounts for 5-90% of the distance between the inlet end and the outlet end of the side wall of the intermediate pipe.
The invention relates to a riser tube catalytic cracking device, wherein the tail end of the inlet end of an inner tube, the tail end of the inlet end of an intermediate tube and the tail end of the inlet end of an outer tube are respectively provided with a cover, a raw oil inlet is arranged on the side wall of the inlet end of the inner tube, a dispersion medium inlet is arranged on the side wall of the inlet end of the intermediate tube, a light raw material inlet is arranged on the side wall of the inlet end of the outer tube, a raw oil channel is arranged in the inner tube, a dispersion medium channel is formed between the inner tube and the intermediate tube, and a light raw material channel is formed between the intermediate tube and the outer tube.
The riser catalytic cracking device comprises a catalyst regenerator, a first catalyst outlet and a second catalyst outlet, wherein the first catalyst outlet is communicated with the diameter-variable structure of the first reaction zone of the riser reactor, and the second catalyst outlet is communicated with the diameter-variable structure of the first reaction zone of the riser reactor.
The riser catalytic cracking apparatus of the present invention, wherein the third nozzle tip of the atomizing nozzle extends into the first reaction zone of the riser reactor, and the first nozzle tip and the second nozzle tip of the atomizing nozzle extend into the second reaction zone of the riser reactor.
The riser catalytic cracking device comprises a catalyst regenerator, a catalyst inlet, a catalyst outlet and a riser catalytic cracking unit, wherein the catalyst regenerator comprises a first regenerator and a second regenerator, the catalyst inlet is arranged on the first regenerator, and the first catalyst outlet and the second catalyst outlet are arranged on the second regenerator.
The riser catalytic cracking device is characterized in that the structure without diameter change is cylindrical; the diameter expanding structure is an inverted conical trapezoid, the longitudinal section of the diameter expanding structure is an inverted isosceles trapezoid, and the vertex angle b of the inverted isosceles trapezoid is more than 90 degrees and less than or equal to 150 degrees; the equal diameter structure is cylindrical; the reducing structure is a conical trapezoid, the longitudinal section of the reducing structure is an isosceles trapezoid, and the vertex angle a of the isosceles trapezoid is more than 90 degrees and less than or equal to 150 degrees.
The riser catalytic cracking device of the invention is characterized in that the length of the first reaction zone accounts for 3% -30% of the total length of the riser reactor, and the reducing structure of the first reaction zone is connected with the second reaction zone.
The invention has the beneficial effects that:
(1) the invention adopts the riser reactor with the reducing structure, strengthens the secondary reaction at the lower part of the riser reactor so as to inhibit alkylation and hydrogen transfer reactions and improve the yield of liquefied gas rich in gas olefin and gasoline rich in aromatic hydrocarbon.
(2) The invention adopts the upper part fast bed riser reactor, shortens the material retention time on the upper part of the riser and realizes the effective control on the target reaction of the material.
(3) The atomizing nozzle improves the shearing and tearing capacity of the dispersion medium by the diameter changing technology of the dispersion medium channel, and simultaneously combines with the diameter changing of the first nozzle head and the second nozzle head to realize twice pressure changing, ensure that oil and gas are fully mixed and improve the oil and gas atomizing effect.
Drawings
FIG. 1 is a schematic of a riser catalytic cracking unit of the present invention.
FIG. 2 is a schematic cross-sectional view of an atomizing nozzle in a riser catalytic cracking unit of the present invention.
FIG. 3 is a perspective view of an atomizing nozzle in the riser catalytic cracking unit of the present invention.
FIG. 4 is a schematic illustration of a riser catalytic cracking unit of comparative example 1.
Wherein, the reference numbers:
701-atomizing nozzle
10-raw oil passage
11-first nozzle head
110-first plane structure
111-hole
12-feedstock oil inlet
20-channels for dispersion medium
21-second nozzle head
210-second plane Structure
211-hole
22-Dispersion Medium inlet
23-convex
30-light feedstock channel
31-third nozzle head
32-light raw material inlet
310-third planar Structure
311-hole
3-thermocouple sleeve
702-riser reactor
703-stripper
704 oil and gas
705 flue gas
706-catalyst regenerator
7061 first regenerator
7062 second regenerator
707-pipeline one
708-line two
709-pipeline three
Detailed Description
The following examples illustrate the invention in detail: the present example is carried out on the premise of the technical scheme of the present invention, and detailed embodiments and processes are given, but the scope of the present invention is not limited to the following examples, and the experimental methods without specific conditions noted in the following examples are generally performed according to conventional conditions.
The present invention provides a riser catalytic cracking apparatus, as shown in fig. 1, comprising:
the inlet end of the riser reactor 702 is communicated with the atomizing nozzle 701, and the outlet end of the riser reactor 702 is communicated with the stripper 703;
a catalyst regenerator 706, the catalyst regenerator 706 comprising a catalyst inlet and a catalyst outlet, the catalyst inlet being in communication with the stripper 703 and the catalyst outlet being in communication with the riser reactor 702;
the riser reactor 702 comprises a first reaction zone I and a second reaction zone II in sequence from an inlet end to an outlet end, the inlet end of the first reaction zone I is communicated with the atomizing nozzle 701, the outlet end of the first reaction zone I is communicated with the second reaction zone II, the inlet end to the outlet end of the first reaction zone I comprises a non-reducing structure and a reducing structure in sequence, and the reducing structure comprises an expanding structure, an equal-diameter structure and a reducing structure in sequence from the inlet end of the first reaction zone to the outlet end of the first reaction zone.
Wherein, the cross-sectional view of the atomizing nozzle 701 is shown in fig. 2, the atomizing nozzle 701 includes:
the nozzle comprises a nozzle main body, a nozzle main body and a nozzle cover, wherein the nozzle main body is a three-layer sleeve composed of an inner pipe, an intermediate pipe and an outer pipe, the two ends of the three-layer sleeve are respectively an inlet end and an outlet end, the inlet end of the inner pipe is provided with a raw oil inlet 12, the inlet end of the intermediate pipe is provided with a dispersion medium inlet 22, and the inlet end of the outer pipe is provided with a light raw material inlet 32;
a first nozzle head 11, the first nozzle head 11 being connected to the outlet end of the inner tube, the first nozzle head 11 having a cross-sectional area that gradually decreases in a direction away from the inner tube;
a second nozzle head 21, the second nozzle head 21 being connected to an outlet end of the intermediate pipe, the second nozzle head 21 being gradually reduced in cross-sectional area in a direction away from the intermediate pipe;
a third nozzle head 31, the third nozzle head 31 is arranged at the outlet end of an annular channel formed by the outer wall of the intermediate pipe and the inner wall of the outer pipe;
wherein, the end of the second nozzle head 21 far away from the intermediate pipe is protruded a first distance than the end of the first nozzle head 11 far away from the inner pipe, and the end of the first nozzle head 11 far away from the inner pipe is protruded a second distance than the end of the third nozzle head 31 far away from the outer pipe; at least one protrusion 23 is arranged on the inner wall of the intermediate pipe.
Specifically, the inner tube, the intermediate tube and the outer tube are all hollow structures, and the three tubes can be connected through the positioning column and have the same longitudinal center line, but the invention is not limited thereto. The inner tube provides a raw oil passage 10, the annular passage formed between the intermediate tube and the inner tube is a dispersion medium passage 20, and the annular passage formed between the outer tube and the intermediate tube is a light raw material passage 30. The raw oil inlet 12 is provided in the inner tube side wall, the dispersion medium inlet 22 is provided in the intermediate tube side wall, and the light raw material inlet 32 is provided in the outer tube side wall. The top end of the inlet end of the inner pipe is of a closed structure, such as a cover structure, or is integrally formed with the side wall, and the top ends of the inlet ends of the intermediate pipe and the outer pipe are also of a closed structure, such as a cover structure, or is integrally formed with the side wall. As for the relative positions of the stock oil inlet 12, the dispersion medium inlet 22 and the light-weight stock inlet 32, the present invention is not particularly limited, for example, the stock oil inlet 12 is farther from the outlet end of the three-layer casing than the dispersion medium inlet 22, as shown in fig. 2; or the dispersion medium inlet 22 is farther from the outlet end of the two-layer casing than the stock oil inlet 12, as shown in fig. 1.
The outlet end of the inner tube is connected to the first nozzle head 11, the outlet end of the intermediate tube is connected to the second nozzle head 21, and the outlet end of the outer tube is connected to the third nozzle head 31. The first nozzle head 11 and the second nozzle head 21 may be hollow conical trapezoids. Specifically, the side wall of the outlet end of the inner tube is connected with the trapezoidal side wall of the first nozzle head 11, and the side wall of the second end of the intermediate tube is connected with the trapezoidal side wall of the second nozzle head 21, and the connection can be designed as an integral molding, such as welding, or can be a threaded connection. The third nozzle head 31 may be a hollow conical trapezoid, a hollow cylindrical structure, or an annular thin sheet disposed at the outlet end of the light raw material passage, and the present invention is not particularly limited.
The first nozzle head 11, the second nozzle head 21 and the third nozzle head 31 are of a hollow design, and no conical trapezoid lower bottom surface (or cylindrical lower bottom surface) is arranged, so that raw oil in the raw oil channel 10 can smoothly enter the first nozzle head 11, a dispersion medium in the dispersion medium channel 20 smoothly enters the second nozzle head 21, and a light raw material in the light raw material channel 30 smoothly enters the third nozzle head 31, as shown in fig. 3, one end of the first nozzle head 11, which is far away from the inner tube, is of a first planar structure 110, one end of the second nozzle head 21, which is far away from the middle tube, is of a second planar structure 210, one end of the third nozzle head 31, which is far away from the outer tube, is of a third planar structure 310, a plurality of holes 111 are arranged on the first planar structure 110, a plurality of holes 211 are arranged on the second planar structure 210, a plurality of holes 311 are arranged on the third planar structure 310, the number of holes is not limited to a special outer tube, and can be 1, 2 or 3, … …, but in order to improve the oil-gas mixing efficiency, the number of the holes 111 on the first planar structure is preferably greater than or equal to the number of the second nozzle head structure 210, and is 1.10 mm, and the further preferably, if the included angle between the diameter of the inner tube is 1.10 mm, 10, 35, 10.
The end of the second nozzle head 21 remote from the intermediate pipe projects a first distance beyond the end of the first nozzle head 11 remote from the inner pipe. That is, the space from the end of the first nozzle head 11 away from the inner tube to the end of the second nozzle head 21 away from the intermediate tube is a mixing chamber for mixing the stock oil and the dispersion medium. That is, the second nozzle head 21 surrounds the first nozzle head 11, and the portion of the second nozzle head 21 beyond the first nozzle head 11 forms a mixing chamber, the raw oil passage 10 and the dispersion medium passage 20 are not communicated with each other, and only when the raw oil and the dispersion medium enter the nozzle, they are mixed in the mixing chamber. In one embodiment of the present invention, the vertical distance (first distance) between the end of the first nozzle tip 11 away from the inner pipe and the end of the second nozzle tip 21 away from the intermediate pipe is 0.006-0.030 m, which ensures the sufficient mixing and atomization of the oil gas and the dispersion medium, and the oil gas and the dispersion medium are smoothly injected into the riser reactor through the holes 211 of the second planar structure 210 of the second nozzle tip 21.
The light raw material passage 30 is also not communicated with the raw material oil passage 10 and the dispersion medium passage 20. The end of the first nozzle head 11 remote from the inner tube is projected a second distance than the end of the third nozzle head 31 remote from the outer tube. That is, the first nozzle head 11 and the second nozzle head 21 both protrude from the light raw material passage 30, the third nozzle head 31 is closer to the inlet end of the three-layer shroud relative to the first nozzle head 11 and the second nozzle head 21, and the first nozzle head 11 is closer to the inlet end of the three-layer shroud relative to the second nozzle head 21. The vertical distance (second distance) from one end of the third nozzle head 31 far away from the outer tube to one end of the first nozzle head far away from the inner tube is 0.005-1.00 m. The distance can make the light raw material sprayed by the third nozzle head 31 and the heavy raw material oil sprayed by the second nozzle head 21 enter different parts of the riser reactor to react with different catalysts, so that the distribution of catalytic products is more reasonable.
In addition, the inner wall of the intermediate pipe is provided with the bulges 23, the number of the bulges 23 is more than or equal to 1, the longitudinal section of each bulge 23 is in one or more of a square shape, a trapezoid shape, a semicircular shape and an oval shape, the bulges 23 are positioned between the inlet end and the outlet end of the inner wall of the intermediate pipe, and the distance between the bulges 23 and the outlet end of the side wall of the intermediate pipe accounts for 5-90%, preferably 50-90% of the distance between the inlet end and the outlet end of the side wall of the intermediate pipe. In one embodiment of the present invention, the protrusions 23 are irregularly distributed on the inner wall of the intermediate pipe; in another embodiment of the invention, all the protrusions 23 are at the same distance from the outlet end of the side wall of the intermediate tube, i.e. all the protrusions 23 form a circular ring around the side wall of the intermediate tube.
In one embodiment of the present invention, the thermocouple sleeve 3 is provided in the inner tube, and preferably the thermocouple sleeve 3 is provided at the feedstock oil inlet 12, and the feedstock oil entering the feedstock oil inlet 12 can be measured to select an appropriate preheating temperature for the feedstock oil.
In one embodiment of the present invention, the radius of the intermediate pipe is 0.05 to 0.25m, preferably 0.1 to 0.25m, more preferably 0.12 to 0.2m, and the radius of the inner pipe is 0.04 to 0.20 m.
Referring again to FIG. 1, FIG. 1 shows a riser catalytic cracking apparatus of the present invention, wherein an atomizing nozzle 701 is connected to a first reaction zone I, a stripper 703 is connected to a second reaction zone II, and a fresh catalyst inlet (not shown) is further provided at the inlet end of a riser reactor 702. The catalyst regenerator 706 comprises a first regenerator 7061 and a second regenerator 7062, wherein the first regenerator 7061 is provided with a regenerated catalyst inlet which is communicated with the stripper 703 through a first pipeline 707; the second regenerator 7062 is provided with a regenerated catalyst outlet which is in communication with the riser reactor 702.
Specifically, the regenerated catalyst outlet provided on the second regenerator 7062 includes a first catalyst outlet and a second catalyst outlet, the first catalyst outlet is communicated with the reducing structure of the first reaction zone i of the riser reactor 702 through a third pipeline 709, preferably, the distance from the communication position of the third pipeline 709 with the riser reactor 702 to the outlet end of the riser reactor 702 accounts for 10% -80% of the distance from the inlet end to the outlet end of the riser reactor 702, and the second catalyst outlet is communicated with the non-reducing structure of the first reaction zone i of the riser reactor 702 through a second pipeline 708, preferably, the second catalyst outlet is communicated with the bottom of the first reaction zone i.
The non-reducing structure of the first reaction zone I of the riser reactor 702 is cylindrical; the diameter expanding structure is an inverted conical trapezoid, the longitudinal section of the diameter expanding structure is an inverted isosceles trapezoid, and the vertex angle b of the inverted isosceles trapezoid is more than 90 degrees and less than or equal to 150 degrees; the isodiametric structure is cylindrical; the reducing structure is a conical trapezoid, the longitudinal section of the reducing structure is an isosceles trapezoid, and the vertex angle a of the isosceles trapezoid is more than 90 degrees and less than or equal to 150 degrees. The length of the first reaction zone I accounts for 3% -30% of the total length of the riser reactor 702, and the reducing structure of the first reaction zone I is connected with the second reaction zone II.
Wherein the third nozzle tip 31 of the atomizing nozzle 701 extends into the first reaction zone i of the riser reactor 702, preferably into the bottom of the first reaction zone i; the first nozzle 11 and the second nozzle 21 of the atomizing nozzle 701 protrude into the second reaction zone ii of the riser reactor 702, preferably the bottom of the second reaction zone ii. By the arrangement, the light raw material sprayed out of the third nozzle head 31 and the heavy raw material sprayed out of the second nozzle head 21 can respectively react with the regenerated catalysts at different positions, so that reaction products are reasonably distributed, the yield of dry gas and coke is reduced, and excessive reaction is avoided.
In one embodiment of the present invention, the diameter of the constant diameter structure of the variable diameter structure of the first reaction zone I is 0.1 to 5m, and the ratio of the diameter to the diameter of the second reaction zone II is 1.1 to 6.0: 1. the first reaction zone I is connected with the second pipeline 708, and the included angle between the first reaction zone I and the second pipeline 708 is 20-60 degrees. The number of the combined feeding nozzles 701 is 1-8, and the combined feeding nozzles are uniformly distributed around the inlet end of the first reaction zone I.
When the riser catalytic cracking device is used for carrying out the catalytic cracking process, the operation is as follows:
firstly, preheated raw oil enters an inner tube through a raw oil inlet 12, flows from the inlet end of the inner tube to the outlet end of the inner tube through a raw oil channel 10 and enters a first nozzle head 11, wherein when the raw oil flows through the inlet end of the inner tube, a thermocouple sleeve 3 can adjust the preheating temperature of the raw oil through temperature measurement; the dispersion medium (in one embodiment of the present invention, the dispersion medium is water vapor) enters the intermediate pipe through the dispersion medium inlet 22, flows from the inlet end of the intermediate pipe to the outlet end of the intermediate pipe through the dispersion medium passage 20, and enters the second nozzle head 21. The raw oil entering the first nozzle head 11 enters the mixing chamber through the holes 111 arranged on the first plane structure 110, is fully mixed and atomized with the dispersion medium entering the mixing chamber, and then is discharged out of the atomizing nozzle 701 through the holes 211 on the second plane structure to enter the riser reactor 702.
The water vapor discharged from the dispersion medium passage 20 enters the feedstock oil to form a fine two-phase mixture of water vapor bubbles emerging from the hydrocarbon mixture, which is thoroughly mixed in the mixing chamber, and the first nozzle head 11 functions to preliminarily disperse the heavy oil feedstock, and the second nozzle head 21 functions to uniformly atomize the water vapor and the heavy oil feedstock into the catalytic cracking riser reactor. The raw oil and the dispersion medium are subjected to cold-heat conversion at the outlet end, so that the temperature of the raw oil is instantly raised, and the condition that the atomizing nozzle is blocked due to coking of the raw oil is avoided.
Meanwhile, a fresh catalyst is added into the riser reactor 702 through a fresh catalyst inlet arranged at the inlet end of the riser reactor 702, moves upwards under the action of a dispersion medium, and reacts with the raw oil sprayed by the second nozzle head 21 in the second reaction zone II, wherein the reaction temperature is 500-580 ℃, the reaction time is 0.5-2 seconds, and the weight ratio of the catalyst to the hydrocarbon oil raw material is 4-20: 1. the raw oil can be petroleum fractions, residual oil or crude oil with different boiling ranges, and specifically, the raw oil can be: the primary processing distillate oil comprises gasoline, diesel oil, vacuum wax oil, residual oil and the like; a mixture of two or more of the above primary processed distillates in any proportion; primary process distillate or mixture thereof doped with 10-30 wt% of coker gas oil, deasphalted oil or other secondary process distillate; coker gas oil, crude oil.
The oil gas after the reaction in the second reaction zone II continuously flows upwards to the stripper 703, after the oil gas is settled in the stripper 703, the oil gas 704 is discharged from the top of the stripper 703 to a subsequent process, the settled catalyst to be generated enters the first regenerator 7061 through the first pipeline 707, and then enters the second regenerator 7062 to be burned and regenerated in the air, wherein the regeneration temperature is 680-720 ℃.
A part of the regenerated catalyst enters the bottom of a first reaction zone I of a riser reactor 702 through a second catalyst outlet and a second pipeline 708, and is mixed with a light raw material sprayed out of a third nozzle head 31 to react in the first reaction zone I, wherein the reaction temperature is 500-600 ℃, the reaction time is 0.5-2 seconds, and the weight ratio of the catalyst to the hydrocarbon oil raw material is 3-12: 1. the light raw material can be a light raw material produced by the riser catalytic cracking device, and can also be a light raw material produced by other processes, the distillation range of the light raw material is generally lower than 205 ℃, preferably 30-205 ℃, and the light raw material can be light oil and/or liquefied gas, preferably one or more of carbon tetracarbon hydrocarbon, carbon tetraolefin, C1, C2, methanol, light gasoline, heavy gasoline, hydrogenated gasoline and coker gasoline.
The other part of the regenerated catalyst enters the reducing structure of the first reaction zone I of the riser reactor 702 through a first catalyst outlet and a pipeline III 709 and continuously reacts with the raw oil sprayed by the second nozzle head 21 and the oil gas ascending to the first reaction zone I.
The device is characterized in that an atomizing nozzle 701 extends upwards from the bottom or the inlet end of a riser reactor 702, raw oil (such as heavy oil hydrocarbon) is preheated, mixed with a dispersion medium and sent into the riser reactor 702, then the heavy oil hydrocarbon is contacted with a cracking catalyst to generate light hydrocarbon and a spent catalyst wrapped with a coke layer, the light hydrocarbon passes through a stripper 703 and then is discharged from the top end of an oil gas 704, the spent catalyst wrapped with the coke layer is sent into a catalyst regenerator 706, the regenerated spent catalyst returns to the riser reactor 702 again, and flue gas 705 generated during catalyst regeneration is discharged from the top of the catalyst regenerator 706.
When the atomizing nozzles are not vertically mounted, the atomizing nozzles 701 typically extend from the riser reactor wall from a location somewhere between vertical and horizontal. Since the desired spray pattern depends on the orientation of the nozzle, different positioning typically requires different nozzle outlet end designs. The nozzle of the present invention is suitable for all these orientations, but the shape of the second nozzle head 21 may be varied to achieve the desired spray pattern. Typically, for vertically mounted nozzles, the orifice 211 of the second nozzle head 21 is square, circular, oval, slit-shaped or other non-linear shape to form a spray suitable for a pipe.
Wherein, the first reaction area agent-oil ratio of the riser reactor refers to the weight ratio of the catalyst and hydrocarbon oil entering the first reaction area; the second reaction zone catalyst-to-oil ratio is the weight ratio of catalyst to hydrocarbon oil entering the second reaction zone.
The catalyst can be conventional catalytic cracking catalyst in the field, and the active component is one, two or three of Y or HY type zeolite containing or not containing rare earth, ultrastable Y type zeolite containing or not containing rare earth, ZSM-5 series zeolite or high-silicon zeolite with five-membered ring structure prepared by other methods, and amorphous silicon-aluminum catalyst.
The feeding nozzle is suitable for the catalytic cracking process of heavy oil hydrocarbon. In the process, heavy oil hydrocarbon is preheated, mixed with steam, and fed into an elevating catalytic cracking riser reactor, then the heavy oil hydrocarbon is contacted with a cracking catalyst to produce light hydrocarbon and spent catalyst wrapped with a coke layer, the light hydrocarbon is discharged from the reactor, a portion of the catalyst covering the coke is fed into a catalyst regenerator, and at least a portion of the coke on the spent catalyst is burned off, thereby regenerating the catalyst.
The invention utilizes the diameter-changing technology of the lifting pipe, adopts a bottom expanding-reducing structure, sets different structural parameters aiming at different reaction conditions, can achieve large catalyst-oil ratio in a reaction area, shortens the retention time of upper materials, thereby achieving the purposes of improving the yield of target products, reducing the yield of dry gas and coke, increasing the density of a catalytic cracking catalyst in a first reaction area, realizing the effective control of the target reaction of the materials and further achieving the purpose of producing more target products under the milder operation conditions.
The riser catalytic conversion process and the device can be used for preparing different target products, such as isobutane or isoparaffin-rich gasoline; preparing a proper amount of propylene, isobutane and gasoline rich in isoparaffin; preparing gas olefin and gasoline rich in aromatic hydrocarbon with maximum yield; preparing diesel oil with maximum yield; catalytic thermal cracking and catalytic cracking process combination, etc.
The following examples further illustrate the invention but are not intended to limit the invention thereto.
Example 1
The catalyst is used for carrying out catalytic cracking reaction on the riser catalytic cracking device provided by the invention to achieve the purposes of increasing the yield of propylene and considering the yield and quality of light oil, and the specific parameters and the technological process of the device are as follows.
The total height of the first reaction zone I and the second reaction zone II of the reactor is 19.5m, wherein the diameter of the reducing structure of the first reaction zone I is 0.9m, the height of the reducing structure is 2.0m, and the diameter of the second reaction zone II is 0.5 m. The isosceles trapezoid vertex angle a of the longitudinal section of the circular truncated cone at the joint of the first reaction zone I and the second reaction zone II is 135 degrees, and the isosceles trapezoid vertex angle b of the longitudinal section of the expanding structure of the first reaction zone I is also 135 degrees.
The comparative apparatus is the apparatus shown in fig. 4.
The catalyst was LCC-300 catalyst (produced by catalyst works of petrochemical company, Lanzhou). The mass ratio of regenerated catalyst from line three 709 to regenerated catalyst from line two 708 was 45%. The heavy raw material is heavy raw oil, the properties are shown in table 1, the light raw material is a gasoline component with a distillation range of 30-205 ℃, and under the condition that the outlet temperatures of the riser reactors are respectively 590 ℃, the propylene yield reaches 24.77%, the ethylene yield is 6.96%, and the heavy oil yield is 2.82%. The specific reaction conditions and product distribution are shown in Table 2.
TABLE 1
TABLE 2
Example 2
The apparatus used was the same as in example 1, and the catalyst was LDC-200 catalyst (manufactured by catalyst works of petrochemical company, Lanzhou). The mass ratio of regenerated catalyst from line three 709 to regenerated catalyst from line two 708 was 12%. The heavy raw material is heavy raw oil, the properties are shown in table 3, the light raw material is carbon tetralkyl hydrocarbon, the yield of propylene is 24.77 percent and the yield of ethylene is 6.96 percent under the condition that the outlet temperatures of the riser reactors are 590 ℃ respectively. The specific reaction conditions and product distribution are shown in Table 4.
TABLE 3
TABLE 4
Example 3
The apparatus used was the same as in example 1, and the catalyst was LCC-2 catalyst (manufactured by catalyst works of petrochemical company, Lanzhou). The mass ratio of regenerated catalyst from line three 709 to regenerated catalyst from line two 708 was 30%. The heavy raw material is heavy raw oil, the properties are shown in Table 5, the light raw material is carbon tetraolefin, the propylene yield reaches 15.69% and the heavy oil yield is 6.53% under the condition that the outlet temperatures of the riser reactors are respectively 500 ℃. The specific reaction conditions and product distribution are shown in Table 6.
TABLE 5
TABLE 6
Compared with the comparative example, the process has the advantages that the yield of the propylene is greatly improved from 6.94% to 15.69%, and the process has obvious advantages in the aspect of increasing the yield of the low-carbon olefin.
The present invention is capable of other embodiments, and various changes and modifications may be made by one skilled in the art without departing from the spirit and scope of the invention as defined in the appended claims.
Claims (13)
1. A riser catalytic cracking unit, comprising:
the inlet end of the riser reactor is communicated with the atomizing nozzle, and the outlet end of the riser reactor is communicated with the stripper;
a catalyst regenerator comprising a catalyst inlet in communication with the stripper and a catalyst outlet in communication with the riser reactor;
the riser reactor sequentially comprises a first reaction zone and a second reaction zone from an inlet end to an outlet end, the inlet end of the first reaction zone is communicated with the atomizing nozzle, the outlet end of the first reaction zone is communicated with the second reaction zone, the inlet end to the outlet end of the first reaction zone sequentially comprises a non-diameter-variable structure and a diameter-variable structure, and the diameter-variable structure sequentially comprises a diameter-expanding structure, an equal-diameter structure and a diameter-reducing structure from the inlet end of the first reaction zone to the outlet end of the first reaction zone.
2. The riser catalytic cracking unit of claim 1, wherein the atomizing nozzle comprises:
the nozzle comprises a nozzle main body, a nozzle body and a nozzle body, wherein the nozzle main body is a three-layer sleeve composed of an inner pipe, an intermediate pipe and an outer pipe, the two ends of the three-layer sleeve are respectively an inlet end and an outlet end, the inlet end of the inner pipe is provided with a raw oil inlet, the inlet end of the intermediate pipe is provided with a dispersion medium inlet, and the inlet end of the outer pipe is provided with a light raw material inlet;
a first nozzle tip connected to the outlet end of the inner tube, the first nozzle tip having a cross-sectional area that gradually decreases in a direction away from the inner tube;
a second nozzle tip connected to the outlet end of the intermediate pipe, the second nozzle tip having a cross-sectional area that gradually decreases in a direction away from the intermediate pipe;
the third nozzle head is arranged at the outlet end of an annular channel formed by the outer wall of the intermediate pipe and the inner wall of the outer pipe;
wherein, one end of the second nozzle head far away from the intermediate pipe protrudes a first distance than one end of the first nozzle head far away from the inner pipe, and one end of the first nozzle head far away from the inner pipe protrudes a second distance than one end of the third nozzle head far away from the outer pipe; at least one bulge is arranged on the inner wall of the intermediate pipe.
3. The riser catalytic cracking apparatus as claimed in claim 2, wherein the outlet end of the intermediate pipe protrudes a distance beyond the outlet end of the inner pipe, the outlet end of the inner pipe protrudes a distance beyond the outlet end of the outer pipe, the second nozzle head wraps the first nozzle head, a vertical distance from an end of the first nozzle head away from the inner pipe to an end of the second nozzle head away from the intermediate pipe is 0.006-0.1 m, and a vertical distance from an end of the third nozzle head away from the outer pipe to an end of the first nozzle head away from the inner pipe is 0.005-1.00 m.
4. The riser catalytic cracking apparatus of claim 2, wherein the three-layer sleeve is a cylindrical sleeve, the first nozzle tip and the second nozzle tip are both hollow conical trapezoids, the third nozzle tip is annular, and the inner tube, the intermediate tube, the outer tube, the first nozzle tip, the second nozzle tip and the third nozzle tip have the same longitudinal centerline.
5. The riser catalytic cracking apparatus of claim 2 wherein an end of the first nozzle tip remote from the inner tube is of a first planar configuration, an end of the second nozzle tip remote from the intermediate tube is of a second planar configuration, an end of the third nozzle tip remote from the outer tube is of a third planar configuration, and the first, second and third planar configurations have a plurality of apertures disposed therein.
6. The riser catalytic cracking apparatus as claimed in claim 4, wherein the angle between the trapezoidal surface of the first nozzle head and the inner tube is β -60 °, the angle between the trapezoidal surface of the second nozzle head and the intermediate tube is α -70 °, and the sum of α and β is 90 °, the space from the end of the first nozzle head away from the inner tube to the end of the second nozzle head away from the intermediate tube is a mixing chamber for mixing the raw oil and the dispersion medium.
7. The riser catalytic cracking apparatus of claim 2, wherein the protrusion has one or more of a square shape, a semi-circular shape and an oval shape in longitudinal section, the protrusion is located on the inner wall of the header, and the distance from the outlet end of the sidewall of the header is 5% to 90% of the distance between the inlet end and the outlet end of the sidewall of the header.
8. The riser catalytic cracking apparatus as claimed in claim 2, wherein a cap is provided at the end of the inlet end of the inner tube, the end of the inlet end of the intermediate tube and the end of the inlet end of the outer tube, the feedstock oil inlet is provided on the sidewall of the inlet end of the inner tube, the dispersion medium inlet is provided on the sidewall of the inlet end of the intermediate tube, the light feedstock inlet is provided on the sidewall of the inlet end of the outer tube, the feedstock oil passage is provided in the inner tube, a dispersion medium passage is formed between the inner tube and the intermediate tube, and a light feedstock passage is formed between the intermediate tube and the outer tube.
9. The riser catalytic cracking apparatus of any one of claims 1 to 8, wherein the catalyst regenerator comprises a first catalyst outlet and a second catalyst outlet, the first catalyst outlet is in communication with the reducing structure of the first reaction zone of the riser reactor, and the second catalyst outlet is in communication with the non-reducing structure of the first reaction zone of the riser reactor.
10. The riser catalytic cracking apparatus of claim 9 wherein the third nozzle tip of the atomizing nozzle extends into the first reaction zone of the riser reactor and the first nozzle tip and the second nozzle tip of the atomizing nozzle extend into the second reaction zone of the riser reactor.
11. The riser catalytic cracking unit of claim 9, wherein the catalyst regenerator comprises a first regenerator and a second regenerator, the catalyst inlet being disposed on the first regenerator, and the first catalyst outlet and the second catalyst outlet being disposed on the second regenerator.
12. The riser catalytic cracking unit of claim 9, wherein the non-reducing structure is cylindrical; the diameter expanding structure is an inverted conical trapezoid, the longitudinal section of the diameter expanding structure is an inverted isosceles trapezoid, and the vertex angle b of the inverted isosceles trapezoid is more than 90 degrees and less than or equal to 150 degrees; the equal diameter structure is cylindrical; the reducing structure is a conical trapezoid, the longitudinal section of the reducing structure is an isosceles trapezoid, and the vertex angle a of the isosceles trapezoid is more than 90 degrees and less than or equal to 150 degrees.
13. The riser catalytic cracking apparatus of claim 9, wherein the length of the first reaction zone is 3% to 30% of the total length of the riser reactor, and the diameter reduction structure of the first reaction zone is connected to the second reaction zone.
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