A flexibly adjustable catalytic cracking reactor

Abstract

The invention discloses a flexibly adjustable catalytic cracking reactor, in which fluidizing steam sprayed from a storage tank through a fluidizing steam inlet pipe causes the entering catalyst to be in dense phase fluidization, and the material discharged from the regeneration inclined tube can be adjusted by the storage capacity of the storage tank so that the catalyst can be evenly lifted to the riser reaction section, and the storage tank serves to improve the catalyst lifting capacity, i.e., to adjust and improve the catalyst-oil ratio of the catalytic cracking reaction, and the atomized oil and gas sprayed from the nozzle is consistent with the distribution area of ​​the catalyst density, and the nozzle extension length, nozzle spray angle, and arc fan angle are all consistent with the distribution of the catalyst density, thus changing the concept of the traditional riser reactor, and through the gas-solid two-phase flow theory and the distribution law of the catalyst, the oil and gas and the catalyst are in the reaction section, the dense phase area of ​​the catalyst and the oil and gas spray area are consistent, so that the oil and gas and the catalyst are fully contacted and reacted, the over-cracking and incomplete reaction phenomena are reduced, and the product yield is improved.

Description

Technical Field

[0001] The invention relates to the technical field of catalytic cracking devices, in particular to a flexibly adjustable catalytic cracking reactor. Background Art

[0002] The catalytic cracking unit is one of the important units in petrochemical industry. It re-reacts low-quality residual oil slurry into diesel and gasoline that we need. The operation of the fluidized catalytic cracking unit is mainly on the fluidization of the catalyst. For example, catalyst running, vibration of the unit or pipeline, bridging, catalyst-oil ratio cannot be increased, etc. are all catalyst fluidization problems. Whether the catalytic cracking can produce qualified products depends on process conditions such as catalyst activity and reaction temperature. Summary of the invention

[0003] In order to overcome the deficiencies in the background technology, the present invention discloses a flexibly adjustable catalytic cracking reactor, which reduces over-cracking and incomplete reaction phenomena and improves product yield.

[0004] In order to achieve the above-mentioned object of the invention, the present invention adopts the following technical scheme:

[0005] A flexibly adjustable catalytic cracking reactor comprises a tank body, wherein a partition is arranged inside the tank body, the inside of the tank body above the partition is arranged as a catalyst reaction tank, the inside of the tank body below the partition is arranged as a storage tank, the storage tank and the catalyst reaction tank are connected via a pre-lift pipe, a regeneration inclined pipe is arranged on the side of the storage tank, a feeder inlet is arranged on the side of the catalyst reaction tank, the inside of the catalyst reaction tank above the pre-lift pipe is arranged as a lift pipe, and at least one nozzle is distributed on the side of the lift pipe;

[0006] A venturi body is installed inside the nozzle, an oil and gas cavity is opened inside the nozzle on the left side of the venturi body, an opening connected to the outside is opened on the nozzle on the left side of the oil and gas cavity, a secondary atomizing steam inlet nozzle is installed inside the rightmost side of the nozzle, the top end of the secondary atomizing steam inlet nozzle penetrates and extends into the interior of the nozzle, a primary atomizing oil and gas annular nozzle disk is installed inside the nozzle on the right side of the top end of the secondary atomizing steam inlet nozzle, an oil storage body is opened between the primary atomizing oil and gas annular nozzle disk and the rightmost side of the nozzle, a primary atomizing steam inlet nozzle and an oil and gas inlet nozzle are installed at the position of the outside of the nozzle corresponding to the inside of the oil storage body, a tertiary atomizing steam channel is opened between the venturi body and the outer wall of the nozzle, a tertiary atomizing steam inlet nozzle is installed at the position of the outer wall of the nozzle corresponding to the tertiary atomizing steam channel, and a tertiary atomizing steam nozzle is installed inside the nozzle between the oil and gas cavity and the venturi body.

[0007] A pre-lift steam inlet pipe and a mounting pipe are provided at the bottom end of the storage tank, and a passivation gas inlet pipe, a dry gas nozzle and a fluidizing steam inlet pipe are provided inside the mounting pipe. A heat collector is provided inside the storage tank, and the top ends of the pre-lift steam pipe, the passivation gas pipe, the fuel gas nozzle and the fluidizing steam pipe penetrate and extend into the interior of the storage tank.

[0008] A trumpet-shaped opening structure is arranged at the bottom end of the pre-lifting pipe at a position corresponding to the storage tank.

[0009] The center lines of the primary atomizing steam inlet nozzle and the oil and gas inlet nozzle are arranged to intersect in the same plane, and the intersection point of the center lines of the primary atomizing steam inlet nozzle and the oil and gas inlet nozzle is arranged on the central axis of the nozzle.

[0010] The opening is set to be a symmetrical circular arc-shaped fan-shaped offset opening, the angle between the symmetry center line of the opening and the central axis of the nozzle is set to α, and α is 5~40°, the radius of the circular arc-shaped fan-shaped offset opening of the opening is R, and R is 60~95% of the radius of the riser.

[0011] The left side of the venturi body is set as a venturi tube expansion atomization cavity, and the right side of the venturi body is set as a venturi body contraction atomization cavity. The venturi body contraction atomization cavity is set apart from the top end of the secondary atomization steam inlet nozzle.

[0012] The tertiary atomization steam nozzles are evenly distributed in a ring shape inside the nozzle on the left side of the venturi tube expansion atomization cavity.

[0013] Due to the adoption of the above technical solution, the present invention has the following beneficial effects:

[0014] In the flexibly adjustable catalytic cracking reactor described in the present invention, the fluidizing steam ejected from the storage tank through the fluidizing steam inlet pipe makes the catalyst entering into the dense phase fluidized, and the catalyst can be evenly lifted to the riser reaction section by adjusting the storage capacity of the storage tank regardless of whether the material is discharged uniformly from the regeneration inclined tube. The storage tank serves to improve the catalyst lifting capacity, that is, to adjust and improve the catalyst-oil ratio of the catalytic cracking reaction.

[0015] The atomized oil and gas sprayed from the nozzle is consistent with the distribution area of ​​catalyst density. The nozzle extension length, nozzle spray angle, and arc fan angle must be consistent with the distribution of catalyst density, which has changed the concept of traditional riser reactors. It uses gas-solid two-phase flow theory and the distribution law of catalysts to make the oil and gas and catalyst in the reaction section, the dense phase area of ​​the catalyst and the oil and gas injection area consistent, so that the oil and gas and catalyst can fully contact and react, reduce over-cracking and incomplete reaction, and improve product yield.

[0016] Adjust the catalytic cracking reactant-oil ratio, lower the catalyst temperature, achieve low temperature-large reactant-oil ratio operation, reduce thermal cracking, increase hydrogen transfer, reduce olefin yield, further reduce coke production and dry gas, improve the catalytic cracking heavy oil cracking capacity, and enable catalytic cracking to process high carbon residue and high-density raw materials. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] Figure 1 It is the overall layout structure diagram of the present invention;

[0018] Figure 2 It is a schematic diagram of the longitudinal layout of the nozzle of the present invention;

[0019] Figure 3 It is a schematic diagram of the nozzle opening of the nozzle of the present invention;

[0020] Figure 4 This is the density distribution diagram of the improved riser;

[0021] Figure 5 This is the density distribution diagram of the original riser;

[0022] Figure 6 It is a schematic diagram of the horizontal layout of the nozzle of the present invention;

[0023] Figure 7 It is a schematic diagram of the internal structure of the nozzle of the present invention;

[0024] Figure 8 A is a cross-sectional view of the nozzle of the present invention;

[0025] Fig. 9 It is a cross-sectional view of the nozzle of the present invention taken along the direction B;

[0026] A1 pre-lifting steam inlet pipe, A2 passivation gas inlet pipe, A3 dry gas nozzle, A4 fluidizing steam inlet pipe, A5 storage tank, A6 partition, A7 regeneration inclined pipe, A8 pre-lifting pipe, A9 feeder inlet, A10 lifting pipe, A11 catalyst reaction tank, A12 nozzle, A13 heat collector, A14 tank body, 2 oil and gas cavity 3, tertiary atomization steam nozzle, 4 Venturi tube expansion atomization cavity, 5 tertiary atomization steam channel, 6 Venturi body, 7 Venturi body contraction atomization cavity, 8 nozzle outer wall, 9 tertiary atomization steam inlet nozzle, 10 primary atomization rear oil and gas annular nozzle disk, 11 oil storage body, 12 secondary atomization steam inlet nozzle, 13 primary atomization steam inlet nozzle, 14 oil and gas inlet nozzle. DETAILED DESCRIPTION

[0027] The present invention can be explained in detail by the following examples, and the purpose of disclosing the present invention is to protect all technical improvements within the scope of the present invention.

[0028] Combined with Figures 1 to 9A flexibly adjustable catalytic cracking reactor comprises a tank body A14, a partition A6 is arranged inside the tank body A14, a catalyst reaction tank A11 is arranged inside the tank body A14 above the partition A6, a storage tank A5 is arranged inside the tank body A14 below the partition A6, the storage tank A5 and the catalyst reaction tank A11 are connected through a pre-lift pipe A8, a regeneration inclined pipe A7 is arranged on the side of the storage tank A5, a feeder inlet A9 is arranged on the side of the catalyst reaction tank A11, and the catalyst reaction tank A11 above the pre-lift pipe A8 is connected to the storage tank A5 through a pre-lift pipe A8. 11 is provided with a lifting pipe A10 inside, and at least one nozzle A12 is distributed on the side of the lifting pipe A10; the storage tank A5 is provided so that no matter whether the material is discharged uniformly from the regeneration inclined pipe A7, the catalyst can be uniformly lifted to the reaction section of the catalytic cracking reactor by adjusting the storage capacity of the storage tank A5, and the storage tank A5 plays a role in improving the lifting capacity of the catalyst, that is, regulating and improving the catalyst-oil ratio of the catalytic cracking reaction. The passivation gas pipe A2 is provided mainly to reduce the activity of the catalyst so that it can reach the activity required for catalytic cracking, which is beneficial to protecting the catalyst.

[0029] A venturi body 6 is installed inside the nozzle A12, an oil and gas cavity 2 is opened inside the nozzle 1 on the left side of the venturi body 6, an opening communicating with the outside is opened on the nozzle 1 on the left side of the oil and gas cavity 2, a secondary atomizing steam inlet nozzle 12 is installed inside the rightmost side of the nozzle A12, the top end of the secondary atomizing steam inlet nozzle 12 penetrates and extends into the interior of the nozzle 1, a primary atomizing oil and gas annular nozzle plate 10 is installed inside the nozzle 1 on the right side of the top end of the secondary atomizing steam inlet nozzle 12, an oil storage body 11 is opened between the primary atomizing oil and gas annular nozzle plate 10 and the rightmost side of the nozzle 1, a primary atomizing steam inlet nozzle 13 and an oil and gas inlet nozzle 14 are installed on the outside of the nozzle A12 at a position corresponding to the inside of the oil storage body 11, a tertiary atomizing steam channel 5 is opened between the venturi body 6 and the nozzle outer wall 8, and the nozzle outer wall 8 corresponds to the tertiary atomizing steam channel 5 A tertiary atomizing steam inlet nozzle 9 is installed at the position, and a tertiary atomizing steam nozzle 3 is installed inside the nozzle 1 between the oil and gas cavity 2 and the venturi body 6. The oil and steam entering through the primary atomizing steam inlet nozzle 13 and the oil and gas inlet nozzle 14 have uneven pressure fluctuations, which can be adjusted through the oil storage body 11. The steam ejected from the tertiary atomizing steam nozzle 3 plays an emulsifying and viscosity-reducing role, which impacts and breaks the oil and gas, and forms uniform oil and gas particles through the impact of the gas-liquid two-phase flow in the atomizing section, film pulling, steam-bag oil and oil-bag water explosion, etc., which ensures that the catalyst and oil and gas particles are fully contacted and mixed. The atomized oil and gas ejected from the nozzle A12 is consistent with the distribution area of ​​the catalyst density. The extension length of the nozzle A12, the injection angle of the nozzle A12, and the arc fan angle must be consistent with the distribution of the catalyst density.

[0030] The bottom of the storage tank A5 is provided with a pre-lift steam inlet pipe A1 and a mounting pipe, and the interior of the mounting pipe is provided with a passivation gas inlet pipe A2, a dry gas nozzle A3, and a fluidizing steam inlet pipe A4. A heat collector A13 is provided inside the storage tank A5, and the tops of the pre-lift steam pipe A1, the passivation gas pipe A2, the fuel gas nozzle A3, and the fluidizing steam pipe A4 penetrate and extend into the interior of the storage tank A5. When the catalyst temperature is too high, the heat collector A13 is used to lower the catalyst temperature, so that the catalytic cracking reaction reacts at a suitable temperature, reduces the breakage of the catalyst, and improves the yield of the target product. Compared with the external heat extraction of the regenerator, it has flexible adjustment, small heat extraction, and large temperature drop.

[0031] A trumpet-shaped opening structure is provided at the bottom end of the pre-lift pipe 8 at a position corresponding to the storage tank A5.

[0032] pass Figure 4 The catalyst and oil and gas injection area diagram is a static diagram. The actual situation inside is much more complicated. First, a large amount of oil and gas is injected to increase the speed. Secondly, the oil and gas gasification further increases the gas speed and the back mixing is intense. These phenomena occur in the dense phase, which makes the catalyst and oil and gas contact and react violently. If the catalyst is injected in the dilute phase, the situation is completely different, which will increase the amount of coke and dry gas.

[0033] The center lines of the primary atomizing steam inlet nozzle 13 and the oil and gas inlet nozzle 14 are arranged to intersect in the same plane, and the intersection of the center lines of the primary atomizing steam inlet nozzle 13 and the oil and gas inlet nozzle 14 is arranged on the central axis of the nozzle 1, thereby ensuring that the oil and gas entering from the primary atomizing steam inlet nozzle 13 and the oil and gas inlet nozzle 14 can quickly contact with the steam, thereby improving the formation speed of oil-in-water or water-in-oil.

[0034] The opening is set to a symmetrical circular arc-shaped fan-shaped deflection, and the angle between the symmetrical center line of the opening and the central axis of the nozzle 1 is set to α, and α is 5~40°. The radius of the circular arc-shaped fan-shaped deflection of the opening is R, and R is 60~95% of the radius of the lifting pipe. This structural setting is based on the density distribution of the gas-solid two-phase flow catalyst in the lifting pipe, and is inclined to spray upward and in an arc-shaped fan shape, which is conducive to the dense phase injection of oil and gas particles into the catalyst, so as to achieve full contact, gasification and reaction between the oil and gas particles and the catalyst, reduce the amount of coke and dry gas production, and improve the product yield. The nozzle has low pressure drop and low speed. The oil and gas pressure drop is less than 0.4MPa, the injection speed is about 60m / s, the gas consumption is about 5%, the oil and gas particles are directly less than 60ηm, wear resistance, and large operational flexibility.

[0035] The left side of the Venturi body 6 is set as a Venturi tube expansion atomization cavity 4, and the right side of the Venturi body 6 is set as a Venturi body contraction atomization cavity 7. The Venturi body contraction atomization cavity 7 is set apart from the top of the secondary atomization steam inlet nozzle 12. After the pressure fluctuation and air pressure influence are eliminated in the oil storage body 11, the oil and gas smoothly enter the atomization cavity through the oil and gas annular nozzle disk 10 after the primary atomization, and then impact and break with the secondary atomization steam and pass through the Venturi body contraction atomization cavity 7 at high speed. Pull, tear, and explode, and then repeatedly impact, collide, tear and explode through the Venturi tube expansion atomization cavity 4, so as to form a uniform oil and gas airflow.

[0036] The tertiary atomizing steam nozzles 3 are evenly distributed in a ring shape inside the nozzle 1 on the left side of the venturi tube expansion atomizing cavity 4, so that the steam sprayed from the tertiary atomizing steam nozzles 3 can fully and quickly contact the oil and gas inside the venturi tube expansion atomizing cavity 4.

[0037] Embodiment 1, a flexibly adjustable catalytic cracking reactor, when in use, firstly regenerates the catalyst from the regeneration inclined tube A7 into the storage tank A5, passes through the fluidizing steam A4, fluidizes the catalyst in the storage tank A5 through the heat collector A13 to reduce the catalyst temperature, and the catalyst enters the pre-lifting pipe A8, and is lifted to the lifting pipe A10 inside the catalyst reaction tank A11 through the pre-lifting steam pipe A1 and the passivation gas pipe A2, and finally reaches the position of the nozzle A12. It can be seen from the original lifting pipe catalyst density distribution diagram and the current lifting pipe catalyst density distribution diagram that The catalyst distribution in the reaction section moves obviously toward the center. The oil and gas particles sprayed from the feed nozzle react with the catalyst here. The density of the oil and gas particles is conical and fan-shaped. The oil and gas are concentrated through the dense phase area of ​​the catalyst, so that the oil and gas and the catalyst can fully contact and react. This has changed the concept of the traditional riser reactor. It uses the gas-solid two-phase flow theory and the distribution law of the catalyst to make the oil and gas and the catalyst in the reaction section, the dense phase area of ​​the catalyst and the oil and gas injection area consistent, so that the oil and gas and the catalyst can fully contact and react, reduce over-cracking and incomplete reaction, and improve product yield.

[0038] When nozzle A12 is in use, steam and oil and gas are simultaneously sprayed into the interior of the oil storage body 11 through the primary atomizing steam inlet nozzle 13 and the oil and gas inlet nozzle 14 for preliminary mixing, and then after the first atomization, the oil and gas are sprayed out from the nozzle in the oil and gas annular nozzle disk 10 to be mixed again with the whole sprayed from the secondary atomizing steam inlet nozzle 12, and then, under the action of the airflow, they pass through the secondary atomizing steam inlet nozzle 12 and the interior of the Venturi tube expansion atomizing cavity 4 in turn, at which time they are repeatedly pulled, torn, and exploded at high speed, and then they come into contact with the steam sprayed from the tertiary atomizing steam nozzle 3 again, which plays a role of re-atomization, forming a steam curtain to prevent the catalyst from coking and breaking, and finally pass through the oil and gas cavity 2 and be sprayed out from the opening on its side.

[0039] The parts of the present invention that are not described in detail are prior art. Although the present invention is specifically demonstrated and introduced in conjunction with the preferred implementation scheme, there are many methods and approaches to specifically implement the technical solution. The above is only a preferred implementation scheme of the present invention, but technical personnel in the relevant field should understand that various changes can be made to the present invention in form and details without departing from the spirit and scope of the present invention as defined in the attached claims, and all of them are within the scope of protection of the present invention.

Claims

1. A flexibly adjustable catalytic cracking reactor, comprising a tank body (A14), characterized in that: The tank body (A14) is provided with a partition (A6) inside, the tank body (A14) above the partition (A6) is provided with a catalyst reaction tank (A11), the tank body (A14) below the partition (A6) is provided with a storage tank (A5), the storage tank (A5) and the catalyst reaction tank (A11) are connected via a pre-lifting pipe (A8), a regeneration inclined pipe (A7) is provided on the side of the storage tank (A5), a feeder inlet (A9) is provided on the side of the catalyst reaction tank (A11), the catalyst reaction tank (A11) above the pre-lifting pipe (A8) is provided with a lifting pipe (A10), and at least one nozzle (A12) is distributed on the side of the lifting pipe (A10); A venturi body (6) is installed inside the nozzle (A12), an oil-gas chamber (2) is provided inside the nozzle (A12) on the left side of the venturi body (6), an opening communicating with the outside is provided on the nozzle head on the left side of the oil-gas chamber (2), a secondary atomizing steam inlet nozzle (12) is installed inside the rightmost side of the nozzle (A12), the top end of the secondary atomizing steam inlet nozzle (12) penetrates and extends into the nozzle (A12), a primary atomizing post-oil-gas annular nozzle disc (10) is installed inside the nozzle (A12) on the right side of the top end of the secondary atomizing steam inlet nozzle (12), and the primary atomizing post-oil-gas annular nozzle disc (10) is installed inside the nozzle (A12) An oil storage body (11) is provided between the shaped nozzle plate (10) and the rightmost side of the nozzle (A12); a primary atomizing steam inlet nozzle (13) and an oil and gas inlet nozzle (14) are installed at a position on the outside of the nozzle (A12) corresponding to the inside of the oil storage body (11); a tertiary atomizing steam channel (5) is provided between the venturi body (6) and the outer wall (8) of the nozzle; a tertiary atomizing steam inlet nozzle (9) is installed at a position on the outer wall (8) of the nozzle corresponding to the tertiary atomizing steam channel (5); and a tertiary atomizing steam nozzle (3) is installed inside the nozzle (A12) between the oil and gas cavity (2) and the venturi body (6); The opening is set to be a symmetrical circular arc-shaped fan-shaped deflection opening, the angle between the symmetry center line of the opening and the central axis of the nozzle is set to α, and α is 5-40°, the radius of the circular arc-shaped fan-shaped deflection opening of the opening is R, and R is 60-95% of the radius of the riser; A trumpet-shaped open structure is provided at the bottom end of the pre-lift pipe (A8) at a position corresponding to the storage tank (A5).

2. A flexibly adjustable catalytic cracking reactor according to claim 1, characterized in that: The bottom end of the storage tank (A5) is provided with a pre-lifting steam inlet pipe (A1) and a mounting pipe, and the interior of the mounting pipe is provided with a passivation gas inlet pipe (A2), a dry gas nozzle (A3), and a fluidizing steam inlet pipe (A4); the interior of the storage tank (A5) is provided with a heat collector (A13); the top ends of the pre-lifting steam inlet pipe (A1), the passivation gas inlet pipe (A2), the dry gas nozzle (A3), and the fluidizing steam inlet pipe (A4) penetrate and extend into the interior of the storage tank (A5).

3. The flexibly adjustable catalytic cracking reactor according to claim 1, characterized in that: The center lines of the primary atomizing steam inlet nozzle (13) and the oil and gas inlet nozzle (14) are arranged to intersect in the same plane, and the intersection point of the center lines of the primary atomizing steam inlet nozzle (13) and the oil and gas inlet nozzle (14) is arranged on the central axis of the nozzle (A12).

4. The flexibly adjustable catalytic cracking reactor according to claim 1, characterized in that: The left side of the Venturi body (6) is provided as a Venturi tube expansion atomization chamber (4), and the right side of the Venturi body (6) is provided as a Venturi body contraction atomization chamber (7), and the Venturi body contraction atomization chamber (7) is arranged to be spaced apart from the top end of the secondary atomization steam inlet nozzle (12).

5. A flexibly adjustable catalytic cracking reactor according to claim 1 or 4, characterized in that: The tertiary atomization steam nozzles (3) are evenly distributed in a ring shape inside the nozzle (A12) on the left side of the venturi tube expansion atomization cavity (4).

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