CN1309465C - Riser reactor for hydrocarbon fluidized catalytic conversion - Google Patents

Abstract

The invention discloses a hydrocarbon fluidized catalytic conversion riser reactor used in the field of petroleum processing to solve the problem of uneven radial density distribution of catalyst particles existing in conventional riser reactors. In the riser reactor (1) of the present invention, the main reaction section above the nozzle reaction zone and the pre-lift section below the nozzle reaction zone are respectively provided with internal components along the axial direction, and each group of internal components is arranged on the pipe wall of the riser reactor An annular baffle (8) on the inner surface and a cone (7) arranged axially below the annular baffle (8) constitute. The middle part of each annular baffle (8) has a vertical cylindrical inner surface around its axis; the cone (7) in each group of internal members consists of a cylinder and an inverted cone at the bottom of the cylinder, located at the Composition of cones on top of cylinders. The invention is mainly used in various hydrocarbon fluidized catalytic conversion devices.

Description

A Hydrocarbon Fluidized Catalytic Conversion Riser Reactor

technical field

The invention relates to a hydrocarbon fluidized catalytic conversion riser reactor used in the petroleum processing field.

Background technique

Fluid Catalytic Cracking (FCC) is the most important secondary processing method in the oil refining industry. Today's FCC units generally use riser reactors. In recent years, on the basis of the FCC process, DCC, MGG and other catalytic cracking processes and the HCC process for producing light olefins by direct contact cracking of atmospheric residue have been developed. The above-mentioned fluidized catalytic conversion process including the FCC process adopts the existing FCC fluidized technology and a similar riser reactor form. The conventional riser reactor can be divided into three working areas: the pre-lifting section, the main reaction section and the outlet rapid separation section, and the lower part of the main reaction section is the nozzle reaction area. The high-temperature regenerated catalyst from the regenerator enters the pre-lift section at the bottom of the riser reactor through the regeneration inclined tube, and flows upward along the riser reactor into the main reaction section under the action of the pre-lift gas. After the contact, the pyrolysis reaction is carried out, and after the reaction, it enters the rapid separator in the rapid separation section at the outlet for separation. The separated oil and gas are sent to the fractionation tower, and the catalyst is stripped and then enters the regenerator for regeneration to burn off the carbon deposits on the surface of the catalyst, and then enters the riser reactor to participate in the reaction, thus completing the cycle process.

At present, most conventional riser reactors are straight pipes or variable diameter pipes with a height of 20-50 meters. The flow of catalyst in the riser reactor is a typical movement form close to plug flow. Due to the influence of the boundary layer effect, a large amount of catalyst is concentrated near the side wall of the riser reactor, while there is relatively little catalyst in the central area of the riser reactor, and the radial density distribution of the catalyst particles is extremely uneven. The research results confirm that: in the current industrial installations, the catalyst density at the side wall of the riser reactor is more than three times higher than the catalyst density at the center of the riser reactor (the unit of catalyst density is kg/m3). This results in poor mixing between the oil gas and the catalyst in the riser reactor and a reduction in contact efficiency. The contact of raw oil with these unevenly distributed catalysts will lead to uneven reaction levels in different regions; the cracking depth in some regions is not enough, while overcracking and coking will occur in other regions, which directly affects the yield of the target product . In this regard, some researchers at home and abroad try to change the radial distribution of the gas-solid phase in the riser reactor by setting internal components. For example, in the riser reactor proposed by U.S. Patent No. 5,851,380, the main reaction section above the feed injection section (equivalent to the nozzle reaction zone) of the riser reactor is provided with multiple sets of internal components (the internal components are formed in the riser reaction zone). The annular baffle installed along the axial direction on the inner surface of the pipe wall of the riser), by changing the flow area in the riser reactor, the original flow pattern of the fluid is forcibly changed, and the turbulence between the gas-solid two phases is increased. Improve the radial density distribution of catalyst particles in the riser reactor to increase the oil agent contact efficiency, reaction efficiency and target product yield. However, this patent still has certain limitations, which are mainly reflected in: (1) The patent does not set internal components in the pre-lift section, so the radial density distribution of the catalyst in the nozzle reaction zone has not been effectively improved, and the oil contact efficiency lower. Because after the regenerated catalyst enters the pre-lift section from the regenerated inclined tube, if the flow of the catalyst is not improved, the catalyst in the pre-lift section will flow in an S-shaped trajectory, and the radial density distribution is very uneven. After contacting with raw material oil, the reaction depth of the riser reactor is different due to uneven contact, which is easy to cause coking and reduce the yield of the target product; (2) Improve the radial distribution of catalyst particles in the riser reactor To a limited extent. Because the upper and lower surfaces of the inner member of the annular baffle type intersect at a circular terminal edge, the cross section of the annular baffle is triangular; the circumference formed by the terminal edge is in the axial direction of the riser reactor The height of the riser reactor is zero, and the diameter reduction at this place has very limited changes to the fluid flow pattern of the riser reactor. At the same time, too many internal components cannot be installed, otherwise the pressure drop of the riser reactor will be greatly increased.

Contents of the invention

The technical problem to be solved by the present invention is: the problem of uneven radial density distribution of catalyst particles in the existing conventional riser reactor, and at the same time solve the problem of the existing riser reactor with internals. The above-mentioned problems are not sufficiently solved.

In order to solve the above problems, the technical solution adopted in the present invention is: a hydrocarbon fluidized catalytic conversion riser reactor, which is provided with a nozzle reaction zone, the nozzle reaction zone is provided with a nozzle, and the nozzle reaction zone is located in the main reaction section The lower part of the nozzle reaction zone is the pre-lift section, and the inner surface of the riser reactor wall of the main reaction section above the nozzle reaction zone is provided with several annular baffles along the axial direction, which is characterized in that: each ring The middle part of the baffle has a vertical cylindrical inner surface around its axis, and a cone is arranged under each annular baffle along the axial direction of the riser reactor. The cone consists of a cylinder and a It is composed of an inverted cone and a cone at the top of the cylinder. The above-mentioned annular baffle and a cone below it constitute a set of internal components. The pre-lift section below the nozzle reaction zone of the riser reactor is also provided with the described internal components.

Adopting the present invention has the following beneficial effects: Compared with the existing conventional riser reactor without internal components, the present invention compulsorily The catalyst in the sidewall area of the riser reactor flows to the central area of the riser reactor, effectively improving the phenomenon that the radial distribution of the catalyst particles in the riser reactor is seriously uneven. By changing the flow area of the riser reactor, the degree of turbulence of the fluid inside the riser reactor is enhanced. When the catalyst particles flow through the cone, the original flow pattern is changed, and the fluid (including catalyst, oil gas and pre-lift gas) is accelerated and shunted to the side wall, generating strong turbulence in the side wall area, which promotes the Mass transfer between the wall region and the fluid in the central region. When the fluid flows through the cone, a strong vortex will be generated, causing the catalyst in the side wall area of the riser reactor to fall back to the central area of the riser reactor, reducing the side wall effect and making the radial density distribution of the catalyst particles uniform . When the catalyst particles run for a certain distance and leave the action area of the cone, their radial distribution will gradually return to normal. At this time, by setting an annular baffle above the cone to change the flow area of the riser reactor, the fully rectified catalyst flows to the center of the riser reactor, which can further improve the radial direction of the catalyst in this area. distributed. As a preferred embodiment of the present invention, a set of internal components is arranged in the pre-lift section below the nozzle reaction zone to improve the catalyst distribution in the nozzle reaction zone; the catalyst and the raw oil can be evenly contacted to maximize the reaction efficiency. In the main reaction section above the nozzle reaction zone, there are 1 to 3 sets of internal components, which can repeatedly strengthen the mass transfer between oil agents and facilitate the uniform reaction. By adopting the riser reactor of the present invention, the ratio of the catalyst density in the inner side wall region of the conventional riser reactor to the catalyst density in the center region can be reduced from 3:1 to within 1.5:1, and there may even be a rise in the local region. The phenomenon that the catalyst density in the central region of a tube reactor is greater than that in the sidewall regions. In this way, the contact efficiency between oil agents can be significantly improved, the distribution of products can be improved, the conversion rate of raw oil and the yield of light oil can be increased, and the yield of dry gas and coke can be reduced.

Compared with USP 5851380, each group of internal members of the present invention is made up of annular baffle plate and cone two parts (it is as mentioned above to the rectification effect of catalyzer). As far as the structure of the annular baffle is concerned, since the cylindrical inner surface of the annular baffle in the internal member of the present invention has a relatively long length, the length of the rectification area that changes the flow of the catalyst in the riser reactor is much longer than The internal components in USP 5851380 can more effectively improve the phenomenon that the radial distribution of catalyst particles in the riser reactor is seriously uneven, and improve the reaction efficiency of the catalyst and oil and gas in the main reaction section of the riser reactor. The present invention also has internal components in the pre-lift section; the improvement of the catalyst flow in the pre-lift section makes the initial contact between the catalyst and the oil gas in the nozzle reaction zone of the riser reactor uniform, and improves the reaction between the catalyst and the oil gas in the nozzle reaction zone efficiency. In addition, due to the reasonable structure of the internal member of the present invention, only a small number of internal members (recommended to install 1 to 3 groups in the main reaction section and 1 group in the pre-lifting section) can achieve the radial direction of the catalyst particles. The purpose of uniform density distribution, so that the pressure drop of the riser reactor will not be increased too much.

The present invention will be further described in detail below in conjunction with the accompanying drawings, specific embodiments and examples. The drawings, specific implementations and examples do not limit the scope of protection claimed by the present invention.

Description of drawings

Figure 1 is a schematic structural view of the riser reactor of the present invention.

Fig. 2 is an enlarged schematic view of part I in Fig. 1, showing a cross-sectional shape of an annular baffle.

Figure 3 is an enlarged schematic view of the cone.

Fig. 4 is an enlarged schematic view of another annular baffle cross-sectional shape.

Fig. 5 is a schematic diagram of the flow mechanism when gas-solid flows through a set of internal components in the riser reactor of the present invention.

The reference numerals among Fig. 1 to Fig. 5 represent:

1——riser reactor; 101——the metal pipe wall of the riser reactor pipe wall;

102——The thermal insulation and wear-resistant layer of the tube wall of the riser reactor;

103——inner surface of riser reactor pipe wall; 2—regeneration inclined pipe; 3—regeneration slide valve;

4——Pre-lifting gas; 5——Gas distributor; 6——Stand-by inclined pipe; 7——Cone;

8—annular baffle; 801—the lower surface of the annular baffle; 802—the upper surface of the annular baffle;

803—cylindrical inner surface of the annular baffle; 9—nozzle; 10—raw oil;

11—regenerated catalyst; 12—quick separator; 13—settler;

14—the oil and gas separated by the settler; 15—the stripping section of the settler; 16—the unborn catalyst.

Detailed ways

Referring to Fig. 1, the hydrocarbon fluidized catalytic conversion riser reactor 1 of the present invention (hereinafter referred to as the riser reactor) is divided into three working areas of a pre-lift section, a main reaction section and an outlet rapid separation section from bottom to top, Wherein the lower part within the main reaction section is a nozzle reaction zone, and the nozzle reaction zone is provided with a nozzle 9 . The outlet of the quick separation section above the main reaction section extends into the settler 13 and is provided with a quick separator 12 . The lower part of the settler 13 is provided with a settler stripping section 15 , and the lower part of the settler stripping section 15 is provided with an inclined pipe 6 to be produced. The pre-lift section at the bottom of the riser reactor 1 is provided with a regeneration inclined pipe 2 (the regeneration inclined pipe 2 is provided with a regeneration slide valve 3 ) and a gas distributor 5 . The above structure and arrangement are the same as the existing conventional riser reactor.

Referring to Fig. 1, in the riser reactor 1 of the present invention, the main reaction section above the nozzle reaction zone and the pre-lift section below the nozzle reaction zone are respectively provided with internals along the axial direction, and each group of internals consists of an annular baffle 8 and The cone 7 located below it constitutes (the cone 7 in FIG. 1 is not sectioned). Referring to Fig. 1 and Fig. 2, a kind of annular baffle plate 8 shown is arranged on the inner surface 103 of the tube wall of the riser reactor 1, and this annular baffle plate 8 has the inner surface 103 upwards from the inner surface 103 of the tube wall of the riser reactor reactor. Inclined lower surface 801 and downwardly inclined upper surface 802; the middle part of each annular baffle plate 8 also has a vertical cylindrical inner surface 803 around its axis, and the lower surface 801 and upper surface 802 of the annular baffle plate 8 are respectively connected to The bottom and top of the cylindrical inner surface 803 meet. Wherein, the lower surface 801 of the annular baffle 8 faces the flow direction of the fluid, and the upper surface 802 faces away from the flow direction of the fluid. The cross-sectional shape of the annular baffle 8 shown in Figure 2 is trapezoidal; the angle β between its lower surface 801 and the inner surface 103 of the riser reactor pipe wall is generally 20 to 70 degrees, and the optimal angle is 35 to 60 degrees. The angle γ between the upper surface 802 and the inner surface 103 of the riser reactor wall is generally 5-45 degrees, and the optimal angle is 15-30 degrees. As shown in Figure 1, each set of internal members is provided with a cone 7 along the axial direction of the riser reactor 1 below the annular baffle 8; referring to Figure 3, the cone 7 consists of a cylinder and a cone at the bottom of the cylinder An inverted cone, consisting of a cone on top of the cylinder.

Refer to FIG. 4 for the cross-sectional shape of the annular baffle 8 of another structure of the present invention. The middle part of this annular baffle 8 also has a vertical cylindrical inner surface 803 around its axis, and also has an upper surface 802 inclined downwards from the inner surface 103 of the riser reactor tube wall; The tops of the cylindrical inner surfaces 803 intersect. Different from the annular baffle 8 shown in FIG. 2 , the bottom of the annular baffle 8 shown in FIG. 4 is an open structure without a lower surface 801 inclined upward from the inner surface 103 of the riser reactor tube wall. The annular baffle plate 8 shown in Figure 2 is a solid body, while the annular baffle plate 8 shown in Figure 4 is made up of a section of inverted conical plate and a section of cylindrical plate (thus forming its cylindrical inner surface 803 and upper surface 802), a space is formed between the inverted conical and cylindrical plates and the inner surface 103 of the riser reactor tube wall. The angle γ between the upper surface 802 of the annular baffle 8 shown in FIG. 4 and the inner surface 103 of the riser reactor pipe wall is also generally 5-45 degrees, and the optimal angle is 15-30 degrees. The remaining structures of the annular baffle 8 shown in FIG. 4 and FIG. 2 and the manner in which the annular baffle 8 and the cone 7 are configured to form a set of internal members are exactly the same. Compared with the annular baffle 8 shown in FIG. 2 , the advantages of the annular baffle 8 shown in FIG. 4 are: (1) convenient construction and installation; (2) easy to absorb thermal expansion during operation.

2 and 4, the distance a (also referred to as the width of the annular baffle 8) between the cylindrical inner surface 803 of the annular baffle 8 of the two structures and the inner surface 103 of the riser reactor tube wall is generally 5-15% of the diameter of the riser reactor 1, the length b of the cylindrical inner surface 803 of the annular baffle 8 (also referred to as the length of the annular baffle 8) is generally 10-50% of the diameter of the riser reactor 1 . The diameter of the riser reactor mentioned in the present invention all refers to the inner diameter (commonly known as the lining inner diameter) of the heat-insulating and wear-resistant layer of the main reaction section. Referring to Fig. 3, the cone angle α of the inverted cone at the bottom of the cylinder of the cone 7 and the cone angle δ of the cone at the top of the cylinder are generally 45-150 degrees, and the optimal angle is 90-130 degrees. The length L of the cone 7 and the cylinder is generally 0.2-1 times the diameter of the riser reactor 1 , and the optimal length is 0.3-0.6 times the diameter of the riser reactor 1 . The diameter d of the cylinder is generally 0.2 to 0.6 times the diameter of the riser reactor 1 , and the optimal diameter is 0.3 to 0.5 times the diameter of the riser reactor 1 . In each group of internal components, the distance between the annular baffle 8 and the cone 7 is generally 0.3-3 times the diameter of the riser reactor 1, and the optimal distance is 0.8-1.5 times the diameter of the riser reactor 1. The distance between the above-mentioned annular baffle 8 and the cone 7 refers to the vertical distance between the midpoint of the length b of the cylindrical inner surface 803 of the annular baffle 8 and the midpoint of the cylindrical length L of the cone 7 .

In the riser reactor 1 of the present invention, 1 to 3 sets of the above-mentioned internal components are usually arranged in the main reaction section above the nozzle reaction zone; as shown in FIG. 1 , 3 sets are arranged. Among them, the distance from a group of internal components adjacent to the nozzle 9 to the nozzle 9 is generally 1 to 2 times the diameter of the riser reactor 1, and this distance refers to the distance between the midpoint of the length L of the cone 7 and the cylinder of the internal component. 9 Vertical distance between entrance centers. When 2 or 3 sets of internal components are arranged in the main reaction section above the nozzle reaction zone of riser reactor 1, the distance between two adjacent sets of internal components is generally 2 to 10 times the diameter of riser reactor 1, and the distance is Refers to the vertical distance between the midpoint of the length L of the cone 7 cylinder in the upper set of internal components and the midpoint of the length b of the cylindrical inner surface 803 of the annular baffle plate 8 in the lower set of internal components. Usually, one set of internals is set in the pre-lift section below the nozzle reaction zone (as shown in Figure 1, one set is set), and the distance from this set of internals to the nozzle 9 is generally 0.2 to 1 mm of the diameter of the riser reactor 1. The distance refers to the vertical distance between the midpoint of the length b of the cylindrical inner surface 803 of the annular baffle 8 in the inner member and the center of the inlet of the nozzle 9 .

As shown in Fig. 2 and Fig. 4, the pipe wall of the riser reactor 1 of the present invention is composed of a metal pipe wall 101 and a heat-insulating and wear-resistant layer 102, which is the same as the existing conventional riser reactor. The inner surface 103 of the pipe wall of the riser reactor described in the description of the present invention is actually the inner surface of the heat-insulating and wear-resistant layer 102, and the inner diameter of the heat-insulating and wear-resistant layer in the main reaction section of the riser reactor 1 is also determined by The inner surface of the heat-insulating and wear-resistant layer 102 of the main reaction section is determined. The internal components (annular baffle and cone) of the present invention can be installed in the riser reactor by various common methods and components. Among them, the connection between the annular baffle 8 of the two structures and the inner surface of the riser reactor wall can adopt the same or similar installation method as USP 5851380, make a connection on the annular baffle, and insert it into the riser to react In the heat-insulating and wear-resistant layer of the tube wall. The inner member (annular baffle plate and cone) of the present invention can be made of commonly used metal materials (such as 20R, 16MnR, 15CrMoR, 0Cr18Ni9Ti, etc.).

The operation process of the riser reactor of the present invention will be described below by taking the device shown in FIG. 1 as an example applied to a conventional fluid catalytic cracking process. The high-temperature regenerated catalyst 11 from the regenerator enters the pre-lift section at the lower part of the riser reactor 1 through the regeneration inclined pipe 2 under the regulation of the regeneration slide valve 3 , and the pre-lift gas 4 enters the pre-lift section through the gas distributor 5 . The regenerated catalyst 11 and the pre-lift gas 4 flow upward and pass through a set of internal components arranged in the pre-lift section. After passing through the inner member, the regenerated catalyst particles are redistributed, and a large number of catalyst particles are concentrated in the axial center of the pre-lift section. In the nozzle reaction zone, the regenerated catalyst is in contact with the atomized and preheated feedstock oil 10 from the nozzle 9, mixed and gasified, and catalytic cracking reaction of hydrocarbons occurs. Then the catalyst and oil-gas mixture enters the main reaction section above the nozzle reaction zone, continues to flow upward, and then passes through three sets of internal components located in the main reaction section, so that the mass transfer and reaction process between the oil agents are continuously strengthened; the oil agent can be further fully Mixing is more conducive to the uniform progress of the reaction to improve the reaction efficiency. Fig. 5 shows the mechanism of gas-solid flow when the gas-solid mixture in the riser reactor passes through a group of internal components of the present invention. The reacted oil gas and catalyst enter the outlet quick separation section above the main reaction section, and enter the settler 13 after being separated by the quick separator 12 at the outlet. The oil and gas 14 separated by the settler 13 enters the fractionation system for fractionation. The separated coke-deposited spent catalyst 16 is stripped by the settler stripping section 15, and then enters the regenerator through the spent inclined pipe 6 for burnt regeneration. The regenerated high-temperature regenerated catalyst is returned to the riser reactor for recycling. Among the internal components shown in Fig. 1 and Fig. 5, the annular baffle 8 has the structure shown in Fig. 2 . When the annular baffle 8 shown in Figure 4 is used, the flow mode of the gas-solid mixture when passing through a set of internal components is the same as that of the annular baffle 8 shown in Figure 2 (see Figure 5); only here The space between the inverted conical plate and the cylindrical plate of the annular baffle and the inner surface of the riser reactor tube wall forms a stagnation zone.

The total height of the riser reactor of the present invention is generally 20-50 meters, and the diameter is generally 300-3000 mm; the height of the pre-lifting section is generally 1-15 meters. The diameter of the pre-lift section of the riser reactor shown in Figure 1 (referring to the inner diameter of the heat-insulating and wear-resistant layer of the pre-lift section) and the diameter of the main reaction section of the riser reactor (referring to the inner diameter of the heat-insulating and wear-resistant layer of the main reaction section ) is the same, but like a conventional riser reactor, the diameter of the pre-lift section can also be greater than or smaller than the diameter of the main reaction section of the riser reactor (that is, the riser reactor is a variable-diameter tube structure). The gas distributor 5 in Fig. 1 is a distribution ring, and a distribution pipe can also be used.

Riser reactor of the present invention can not only be used for fluidized catalytic cracking process, but also can be used for other hydrocarbons fluidized catalytic conversion process, as HCC process, DCC process etc., its operating process and above-mentioned fluidized catalytic cracking operating process basically the same. For various fluidized catalytic conversion operations including fluidized catalytic cracking, the residence time of oil and gas in the riser reactor of the present invention is generally 1 to 3 seconds, and the outlet temperature at the top of the riser reactor is generally 350 to 700°C , the agent-oil ratio in the riser reactor is generally 4-25 (the agent-oil ratio refers to the weight ratio of the catalyst circulation flow rate to the feedstock oil flow rate), and the operating line speed of the pre-lift section is generally 0.5-4 m/s, The linear velocity at the top outlet of the riser reactor is generally 12-25 m/s. The pre-lift gas can be water vapor, dry gas, naphtha, etc. The raw material oil and catalyst can be selected from those commonly used in the existing fluidized catalytic conversion process to produce various target products.

The riser reactor of the invention has a simple structure and is easy to implement, and can be widely used in the modification of various hydrocarbon fluidized catalytic conversion devices and the design of new devices in the field of petroleum refining and petrochemical industry.

Comparative Examples and Examples

comparative example

An 800,000-ton/year atmospheric residue fluidized catalytic cracking unit uses a conventional riser reactor (without internals). The main structural parameters and process operating conditions of the riser reactor are as follows: the total height of the riser reactor is 45 meters, and the diameter is 1300 mm; the height of the pre-lift section is 6 meters, and the diameter of the pre-lift section is the same as that of the main reaction section. same diameter. The processed raw oil is Daqing atmospheric residue fraction, with a density of 893.3 kg/m3 and a carbon residue of 4.4% by weight. The catalyst is a LCS-7B catalytic cracking molecular sieve catalyst produced and sold in China. During operation, the residence time of oil and gas in the riser reactor is 2.7 seconds, the outlet temperature at the top of the riser reactor is 505°C, and the ratio of agent to oil in the riser reactor is 6.8. The temperature of the regenerated catalyst was 680°C and the carbon content was 0.05% by weight. The pre-lift gas is water vapor, the operating linear velocity of the pre-lift section is 2.5 m/s, and the linear velocity of the outlet at the top of the riser reactor is 17 m/s. The operation mode is one-way passage of raw material oil. The product distribution is shown in Table 1.

Example

Adopt the scheme of the present invention to transform the device described in the comparative example. One set of internal components is set in the pre-lift section below the nozzle reaction zone of the riser reactor, and three sets of internal components are set in the main reaction section above the nozzle reaction zone. Among the internal components The annular baffle adopts the structure shown in Figure 2. The specific structural parameters of the internal components are shown in Table 2. Other structures, structural parameters and related process operation parameters of the device are the same as those of the comparative example.

Table 3 gives the specific data of product distribution and yield after the modification of the unit, and gives the data of the change of product distribution compared with the unit before modification. As can be seen from the data in table 3, after adopting the present invention, the yield of liquefied gas, gasoline and diesel oil in the process cracking product improves to some extent compared with the conventional riser technology of comparative ratio, and the total liquid product (gasoline, diesel oil and liquefied gas) ) yield increased by 0.7 weight percent, while dry gas and coke yields decreased.

In the text descriptions of the comparative examples and examples and Tables 1 to 3, weight percentages are expressed in weight %.

Table 1 Product distribution before plant renovation project Output, 10,000 tons Yield, % by weight gasoline 35.2 44 diesel fuel 25.28 31.6 liquefied gas 6.8 8.5 dry gas 5.28 6.6 oil slurry 2.8 3.5 coke 4.32 5.4 loss 0.32 0.4 Light oil (gasoline and diesel) yield 75.6 Total Liquid Product Yield 84.1

Table 2 Concrete structural parameters of the riser reactor internals of the present invention project Structural parameters Cone angle α of an inverted cone at the base of a cone-cylinder 135 degrees cone angle δ of a cone on top of a cone cylinder 135 degrees The length L of the cone and cylinder 500mm The diameter d of the cone and cylinder 450 mm Angle β between the lower surface of the annular baffle and the inner surface of the riser reactor wall 45 degree Angle between the upper surface of the annular baffle and the inner surface of the riser reactor wall γ 25 degree The distance between the cylindrical inner surface of the annular baffle and the inner surface of the riser reactor wall a 100mm The length b of the cylindrical inner surface of the annular baffle 400mm The distance between the annular baffle and the cone in each set of internal members 800mm Distance from a set of internal components of the pre-lift section to the nozzle 300 mm The distance from a set of internals adjacent to the nozzle in the main reaction section to the nozzle 1500mm The distance between two adjacent groups of internal members in the main reaction section 3000mm

Table 3 Product distribution after plant modification project Output, 10,000 tons Yield, % by weight Yield change compared with comparative example, weight % gasoline 35.36 44.2 +0.2 diesel fuel 25.6 32.0 +0.4 liquefied gas 6.88 8.6 +0.1 dry gas 5.12 6.4 -0.2 oil slurry 2.72 3.4 -0.1 Coke 4.0 5.0 -0.4 loss 0.32 0.4 0 Light oil (gasoline and diesel) yield 76.2 +0.6 Total Liquid Product Yield 84.8 +0.7

Claims (8)

1, a kind of hydro carbons fluidized catalytic conversion riser reactor, which is provided with the nozzle reaction zone, the nozzle reaction zone is provided with nozzle (9), the nozzle reaction zone is positioned at the bottom within the main reaction section, the below of nozzle reaction zone is a pre lift zone, inner surface (103) upper edge of riser reactor (1) tube wall of the main reaction section above the nozzle reaction zone is axially arranged with several ring baffles (8), it is characterized in that: there is a vertical drum type inner surface (803) at the middle part of each ring baffle (8) around its axis, be axially arranged with cone (7) in the below of each ring baffle (8) along riser reactor (1), cone (7) is by a cylinder and the inverted cone that is positioned at this cylinder bottom, the cone that is positioned at this cylinder top is formed, a cone (7) of an above-mentioned ring baffle (8) and its below constitutes one group of inner member, and the pre lift zone in riser reactor (1) nozzle reaction zone below also is provided with described inner member.

2, riser reactor according to claim 1, it is characterized in that: ring baffle (8) has from the acclivitous lower surface of inner surface (103) (801) of riser reactor tube wall and downward-sloping upper surface (802), lower surface (801) and upper surface (802) respectively with the bottom and the roof intersection of drum type inner surface (803).

3, riser reactor according to claim 2, it is characterized in that: the angle β between the lower surface (801) of described ring baffle (8) and the inner surface (103) of riser reactor tube wall is 20～70 degree, and the angle γ between the upper surface (802) of ring baffle (8) and the inner surface (103) of riser reactor tube wall is 5～45 degree.

4, riser reactor according to claim 1, it is characterized in that: ring baffle (8) has from the downward-sloping upper surface (802) of the inner surface (103) of riser reactor tube wall, the roof intersection of upper surface (802) and drum type inner surface (803), the bottom of ring baffle (8) is uncovered structure.

5, riser reactor according to claim 4 is characterized in that: the angle γ between the upper surface (802) of described ring baffle (8) and the inner surface (103) of riser reactor tube wall is 5～45 degree.

6, according to any one described riser reactor in the claim 2 to 5, it is characterized in that: between the drum type inner surface (803) of ring baffle (8) and the riser reactor inner surface of tube wall (103) is 5～15% of riser reactor (1) main reaction section heat insulation and wear resistance layer (102) interior diameter apart from a, the length b of drum type inner surface (803) is 10～50% of riser reactor (1) main reaction section heat insulation and wear resistance layer (a 102) interior diameter, the cone angle δ of the cone angle of the inverted cone of described cone (7) cylinder bottom and the cone at cylinder top is 45～150 degree, the cylindrical length L of cone (7) is 0.2～1 times of riser reactor (1) main reaction section heat insulation and wear resistance layer (102) interior diameter, cylindrical diameter d is 0.2～0.6 times of riser reactor (1) main reaction section heat insulation and wear resistance layer (102) interior diameter, and each vertical range of organizing between the mid point of the mid point of ring baffle in the inner member (8) drum type inner surface (803) length b and cone (7) cylinder length L is 0.3～3 times of riser reactor (1) main reaction section heat insulation and wear resistance layer (102) interior diameter.

7, according to any one described riser reactor in the claim 2 to 5, it is characterized in that: the main reaction section of riser reactor (1) nozzle reaction zone top is provided with 1～3 group of inner member, and the pre lift zone of nozzle reaction zone below is provided with 1 group of inner member.

8, riser reactor according to claim 6 is characterized in that: the main reaction section of riser reactor (1) nozzle reaction zone top is provided with 1～3 group of inner member, and the pre lift zone of nozzle reaction zone below is provided with 1 group of inner member.

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