COLD REGENERATED CATALYST CIRCULATION METHOD AND DEVICE THEREFOR

Abstract

The present invention provides a method of cooling and cycling a regenerated catalyst. The regenerated catalyst that is from the regenerator is cooled by the catalyst cooler to 200-720 C., and without being mixed with the hot regenerated catalyst directly enters a riser reactor, or mixes with another part of hot regenerated catalyst that has not been cooled to obtain a mixed regenerated catalyst with a temperature below the regenerator temperature, and enters the riser reactor. The hydrocarbon raw material performs the contact reaction with the catalyst in the riser reactor, a reactant stream enters a settler to perform a separation of the catalyst and an oil gas, the separated spent catalyst is steam stripped by a steam stripping section and enters a regenerator to be charring regenerated, and the regenerated catalyst after being cooled returns to the riser reactor to be circularly used. The bottom of each of the catalyst coolers is provided with at least one fluidized medium distributor, the range of the superficial gas velocity is 0-0.7 m/s (preferably 0.005-0.3 m/s, and most preferably 0.01-0.15 m/s), and the temperature of the cold regenerated catalyst is controlled mainly by adjusting a flow rate of the fluidized medium. The method of cooling and cycling a regenerated catalyst of the present invention has extensive application, and can be used for various fluidized catalytic cracking processes, including heavy oil catalytic cracking, wax oil catalytic cracking, gasoline catalytic conversion reforming and the like, and can also be used for other gas-solid reaction processes, including residual oil pretreating, methanol to olefin, methanol to aromatics, methanol to propylene, fluid coking, flexicoking and the like.

Claims

1. A cycling method of cold regenerated catalyst, comprising a fluidized catalytic cracking process, wherein: a hydrocarbon raw material performs a contact reaction with a catalyst in a riser reactor having or not having a fluidized bed reactor, a reactant stream enters a settler to perform a separation of the catalyst and an oil gas, the separated spent catalyst is steam stripped by a steam stripping section, and enters a regenerator to be charring regenerated, and the regenerated catalyst after being cooled and/or without being cooled directly returns to the riser reactor to be circularly used, wherein: 1) the regenerator is provided with one, two or more catalyst coolers, for adjusting reaction temperatures of reaction zones of the riser reactors (and/or the fluidized bed reactors) that are individually connected, and/or adjusting the temperature of the regenerator, to maintain them at the optimum values; and each of the catalyst coolers is provided with one, two or more catalyst outlets, for transporting the cold regenerated catalyst to the reaction zones of the one, two or more riser reactors (and/or fluidized bed reactors) and/or for transporting the cold regenerated catalyst to the regenerator; 2) part of the regenerated catalyst from the regenerator is cooled by the catalyst cooler to 200-720 C., directly enters a pre-lift zone and/or the reaction zones of the riser reactor (and/or the reaction zones of the fluidized bed reactor) and/or mixes with another part of hot regenerated catalyst that has not been cooled to obtain a mixed regenerated catalyst with a temperature below the regenerator temperature, and enters a pre-lift zone and/or the reaction zones of the riser reactor (and/or the reaction zones of the fluidized bed reactor); or the cold regenerated catalyst and the hot regenerated catalyst individually directly enter pre-lift zones of the riser, are lifted by a pre-lift medium to reach an equilibrium temperature, enter the reaction zones of the riser reactor (and/or the reaction zones of the fluidized bed reactor) or without passing through the catalyst cooler directly enter a pre-lift zone and/or the reaction zones of the riser reactor (and/or the reaction zones of the fluidized bed reactor), to be circularly used; and each of the riser reactors is provided with one, two or more reaction zones having or not having a fluidized bed reactor, before the cold regenerated catalyst enters the riser reactor and/or the fluidized bed reactor a pre-riser and/or mixer is or is not provided, and a pre-lift medium transports the cold regenerated catalyst to the riser reactor (and/or the fluidized bed reactor); and 3) the bottom of each of the catalyst coolers is provided with at least one fluidized medium distributor, a fluidized medium mainly enters the catalyst cooler from the distributor, a range of a superficial gas velocity (a ratio of a volume flow rate of the fluidized medium to the cooler cross-section) is greater than 0-0.7 m/s, and the temperature of the cold regenerated catalyst is controlled mainly by adjusting a flow rate of the fluidized medium; and the regenerated catalyst that enters each of the catalyst coolers is a regenerated catalyst or a regenerated catalyst without completed regeneration with any carbon content, or is a spent catalyst or contact agent or coking particles with any carbon content.

2. The method according to claim 1, wherein the superficial gas velocity in Step 3) is 0.005-0.3 m/s.

3. The method according to claim 1, wherein the superficial gas velocity in Step 3) is 0.01-0.15 m/s.

4. The method according to claim 1, wherein the temperature of the cold regenerated catalyst is controlled by adjusting the flow rate of the fluidized medium and/or a heat removing medium and/or a transporting medium and/or other parameters; or is controlled by adjusting the flow rate of the fluidized medium and/or a heat removing medium and/or a transporting medium and/or the flow rate of a cold catalyst that returns to the regenerator and/or other parameters; or the temperature of the mixed regenerated catalyst is controlled by adjusting a proportion of the cold regenerated catalyst and the hot regenerated catalyst and/or other parameters.

5. The method according to claim 1, wherein the reaction temperatures of the reaction zones of the riser reactor and/or the fluidized bed reactor are controlled by adjusting a catalyst-to-oil ratio, and/or by adjusting the temperature of the cold regenerated catalyst or the mixed regenerated catalyst, and/or by employing a multiple feeding technique, and/or by injecting a cold-shocking agent into the riser reactor.

6. The method according to claim 1, wherein a cold catalyst transporting channel to the reaction zones of the riser reactor (or the fluidized bed reactor) is wholly or partially provided outside a catalyst cooler shell or inside a catalyst cooler shell; a transporting channel of the cold catalyst that returns to the regenerator is wholly or partially provided outside a catalyst cooler shell or inside a catalyst cooler shell; and the pre-lift section is wholly (or partially) provided outside or inside the catalyst cooler shell that is connected thereto.

7. The method according to claim 1, wherein one, two or more auxiliary risers are provided, for transporting the cold regenerated catalyst to reaction zones of the one, two or more riser reactors and/or the fluidized bed reactors, as the cold-shocking agent, and/or as the cold-shocking agent after being mixed with another gaseous or liquid cold-shocking agent; and the gaseous or liquid cold-shocking agent is water, oil products including gasoline, recycle oil and clarified oil, and a mixture of one, two or more kinds of catalysts with any carbon content including a cold regenerated catalyst, a spent catalyst and a cold half-regenerated catalyst.

8. The method according to claim 1, wherein the cycling method of cold regenerated catalyst is singly implemented, for the reaction zones of the riser reactor and/or the fluidized bed reactor of fluidized catalytic cracking processes; or is jointly implemented, for the reaction zones of one, two or more riser reactors and/or fluidized bed reactors in two or more riser reactors that have different functions, including for the reaction zones of a heavy oil riser and a gasoline riser of a double riser catalytic cracking device or one, two or more riser reactors in two or more risers for processing different raw materials.

9. The method according to claim 1, wherein the method is used for various fluidized catalytic cracking processes, including heavy oil catalytic conversion, wax oil catalytic conversion, gasoline catalytic reforming, light hydrocarbon catalytic conversion, or used for other gas-solid fluidization reaction charring processes, including residual oil pretreating, methanol to olefin, methanol to propylene, methanol to aromatics, fluid coking and flexicoking.

10. A cycling device of cold regenerated catalyst, which is a device that implements the method according to claim 1.

11. A cycling device of cold regenerated catalyst, which is a device that implements the method according to claim 2.

12. A cycling device of cold regenerated catalyst, which is a device that implements the method according to claim 3.

13. A cycling device of cold regenerated catalyst, which is a device that implements the method according to claim 4.

14. A cycling device of cold regenerated catalyst, which is a device that implements the method according to claim 5.

15. A cycling device of cold regenerated catalyst, which is a device that implements the method according to claim 6.

16. A cycling device of cold regenerated catalyst, which is a device that implements the method according to claim 7.

17. A cycling device of cold regenerated catalyst, which is a device that implements the method according to claim 8.

18. A cycling device of cold regenerated catalyst, which is a device that implements the method according to claim 9.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0069] The features of the invention believed to be novel and the elements characteristic of the invention are set forth with particularity in the appended claims. The figures are for illustration purposes only and are not drawn to scale. The invention itself, however, both as to organization and method of operation, may best be understood by reference to the detailed description which follows taken in conjunction with the accompanying drawings in which:

[0070] FIG. 1 is a typical schematic representation of the present invention; and

[0071] FIG. 2 to FIG. 4 are typical schematic representations of a heavy oil catalytic conversion device that applies the present invention.

DESCRIPTION OF THE PREFERRED EMBODIMENT(S)

[0072] In order to make the objects, the technical solutions and the advantages of the embodiments of the present invention clearer, the technical solutions of the embodiments of the present invention will be described clearly and completely below by referring to the drawings of the embodiments of the present invention. Apparently, the described embodiments are part of embodiments of the present invention, rather than all embodiments. On the basis of the described embodiments of the present invention, all the other embodiments that a person skilled in the art obtains without paying creative work are within the protection scope of the present invention.

[0073] The present invention will be further described by referring to the drawings below.

[0074] FIG. 1 is a typical schematic representation of the present invention (1 cold regenerated catalyst cycling process)

[0075] As shown in FIG. 1: the cold regenerated catalyst cycle of the present invention comprises the settler 1, and the riser reactor 2 comprises the pre-lift zone 4 and the regenerator 5. The spent catalyst transporting pipe 7 and the controlling valve 20 are provided between the regenerator 5 and the steam stripping section 1A of the settler 1 to communicate the regenerator 5 and the steam stripping section 1A, to transport the spent catalyst to the regenerator 5.

[0076] The regenerator is provided with 2 inner or outer heat removing equipments, that is, catalyst coolers, which comprise a catalyst inlet, a lower mixing buffering space, an inner heat removing element (including telescope type and coil pipe type) and a lower fluidized medium distributing installation, which are directly (or by pipeline) connected to the regenerator dense phase.

[0077] The catalyst cooler 8A is mainly for adjusting the reaction temperature of a first reaction zone, to maintain it at the optimum value. The other catalyst cooler (not shown in the figure) is mainly for adjusting the regenerator temperature, to maintain it at the optimum value. 35A is the fluidized medium such as air and steam, 36A is the rising medium such as air and steam, and 37A is the heat removing medium, including water, steam, air, oil products and the like.

[0078] The regenerator 5 is connected to the catalyst cooler 8A by the regenerated catalyst transporting pipe 10A, and the regenerated catalyst after being cooled enters the lower mixing buffering space 9A. The cold regenerated catalyst is connected to the riser reactor pre-lift zone 4 by the cold regenerated catalyst transporting pipe 11A. The temperature of the cold regenerated catalyst that leaves the catalyst cooler 8A (lower mixing buffering space 9A) is controlled by adjusting the flow rate of the fluidized medium 35A (including air, steam and the like) and/or the flow rate of the rising medium 36A (including air, steam and the like) on the cold regenerated catalyst returning pipe 12A. The controlling valve 21A is a special controlling element that is provided for conveniently controlling the flow rate of the cold regenerated catalyst.

[0079] In order to conveniently control the temperature of the reaction zones of the riser reactor, a hot regenerated catalyst transporting pipe (including a controlling valve) (not shown in the figure) may be provided to connect the regenerator 5 directly to the heavy oil riser reactor pre-lift zone 4, the cold regenerated catalyst and the hot regenerated catalyst, after being mixed in the riser reactor pre-lift zone 4, raise the temperature by the pre-lift medium 32 (including water, steam, refinery dry gases and the like) to reach the equilibrium.

[0080] The heavy oil riser reactor may also be provided with 2 reaction zones, and the cold regenerated catalyst enters the auxiliary riser via the cold regenerated catalyst transporting pipe, and is transported by the pre-lift medium to the second reaction zone of the riser reactor as the cold-shocking agent (not shown in the figure).

[0081] According to the process requirements, the catalyst cooler mainly for adjusting the regenerator temperature may be not provided. The temperature of the regenerator 5 is controlled by adjusting the flow rate of the fluidized medium 35A, including air, steam and the like, and the flow rate of the rising medium 36A, including air, steam and the like, on the cold regenerated catalyst returning pipe 12A.

[0082] Certainly, there may be many other controlling equipments and controlling methods, and that does not limit any special implementation of the concept of the present invention.

[0083] The catalyst cooler may be integral with the regenerator and the riser, and may also be connected thereto by pipeline.

[0084] The cold regenerated catalyst that has been cooled to 200-720 C. (preferably 360-650 C.) enters the riser reactor 2 via the pre-lift zone 4. The hydrocarbon raw material performs the contact reaction with the catalyst in the riser reactor 2, the reactant stream enters the settler 1 to perform the separation of the catalyst and the oil gas, and the separated spent catalyst is steam stripped by the steam stripping section 1A, enters the regenerator 5, and is charring regenerated in the present of the oxygen-containing gas 38 (including air and the like). The regenerated catalyst after being cooled or directly returns to the riser reactor to be circularly used.

[0085] The catalyst cooler is provided with at least one fluidized medium distributor. The fluidized medium enters the catalyst cooler via the bottom distributor of the catalyst cooler, wherein the superficial gas velocity is 0-0.7 m/s (preferably 0.005-0.3 m/s, and most preferably 0.01-0.15 m/s), and the temperature of the cold regenerated catalyst is controlled mainly by adjusting a flow rate of the fluidized medium.

[0086] FIG. 2 is a typical schematic representation of a heavy oil catalytic conversion device that applies the present invention.

[0087] As shown in FIG. 2: the method of heavy oil catalytic conversion and the equipment thereof of the present invention comprises the settler 1, the heavy oil riser reactor comprises the pre-lift zone 4, the first reaction zone 3, the second reaction zone 2, the regenerator 5 and the charring tank 5A. The spent catalyst transporting pipe 75 and the controlling valve 20 are provided between the charring tank 5A and the steam stripping section 1A of the settler 1 to communicate the charring tank 5A and the steam stripping section 1A, to transport the spent catalyst to the charring tank 5A. In order to ensure the initial charring temperature of the charring tank 5A, the regenerated catalyst cycling pipe 16 and the controlling valve 23 are provided.

[0088] The regenerator is provided with 2 inner or outer heat removing equipments, that is, catalyst coolers, which comprise a catalyst inlet, a lower mixing buffering space, an inner heat removing element (including telescope type and coil pipe type) and a lower fluidized medium distributing installation, which are directly (or by pipeline) connected to the regenerator dense phase.

[0089] 35A, 35B are the fluidized medium such as air, water and steam, 36A, 36B are the rising medium such as air and steam, and 37A, 376 are the heat removing medium, including water, steam, air, oil products and the like. The catalyst cooler 8A is mainly for adjusting the reaction temperature of a first reaction zone, to maintain it at the optimum value. The catalyst cooler 8B is mainly for adjusting the regenerator temperature, to maintain it at the optimum value.

[0090] According to the process requirements, any one or two of the catalyst cooler 8A and the catalyst cooler 8B may be not provided.

[0091] The regenerator 5 is connected to the catalyst cooler 8A by the regenerated catalyst transporting pipe 10A, and the regenerated catalyst after being cooled enters the lower mixing buffering space 9A. The cold regenerated catalyst is connected to the heavy oil riser reactor pre-lift zone 4 by the cold regenerated catalyst transporting pipe 11A. The temperature of the cold regenerated catalyst that leaves the catalyst cooler 8A is controlled by adjusting the flow rate of the fluidized medium 35A (including air, steam and the like) and/or the flow rate of the rising medium 36A (including air, steam and the like) on the cold regenerated catalyst returning pipe 12A. The controlling valve 21A is a special controlling element that is provided for conveniently controlling the flow rate of the cold regenerated catalyst.

[0092] In order to conveniently control the temperature of the first reaction zone of the heavy oil riser reactor, a hot regenerated catalyst transporting pipe (including a controlling valve) (not shown in the figure) that is directly connect to the heavy oil riser reactor pre-lift zone 4 may be provided. The cold regenerated catalyst and the hot regenerated catalyst, after being mixed in the heavy oil riser reactor pre-lift zone 4, raise the temperature by the pre-lift medium 32 (including water, steam, refinery dry gases and the like) to reach the equilibrium.

[0093] Certainly, there may be many other controlling equipments and controlling methods, and that does not limit any special implementation of the concept of the present invention.

[0094] In order to conveniently control the temperature of the second reaction zone 2 of the riser reactor, the cold-shocking agent 34 may be injected into the downstream of the first reaction zone, to conveniently control the temperature of the second reaction zone 2. The cold-shocking agent may be any one of a gas or a liquid (including water, oil products and the like) and a cold catalyst, and may also be two or more of them. The cold catalyst may be any one of a cold regenerated catalyst, a cold spent catalyst and a cold half-regenerated catalyst, and may also be two or more of them.

[0095] The cold regenerated catalyst, when it is as the cold-shocking agent, may enter the auxiliary riser via the cold regenerated catalyst transporting pipe, and is transported by the pre-lift medium to the second reaction zone of the riser reactor (not shown in the figure).

[0096] The regenerator 5 is connected to the catalyst cooler 8B by the regenerated catalyst transporting pipe 10B, and the regenerated catalyst after being cooled enters the lower mixing buffering space 9B. The temperature of the regenerator 5 is controlled by adjusting the flow rate of the fluidized medium 35B (including air, steam and the like) and/or the flow rate of the rising medium 36B (including air, steam and the like) on the cold regenerated catalyst returning pipe 12B.

[0097] The catalyst cooler 8A, 8B are provided with at least one fluidized medium distributor. The fluidized medium enters the catalyst cooler via the bottom distributor of the catalyst cooler, wherein the superficial gas velocity is 0-0.7 m/s (preferably 0.005-0.3 m/s, and most preferably 0.01-0.15 m/s), and the temperature of the cold regenerated catalyst is controlled mainly by adjusting a flow rate of the fluidized medium.

[0098] Certainly, there may be many other controlling equipments and controlling methods, and that does not limit any special implementation of the concept of the present invention.

[0099] The catalyst cooler may be integral with the regenerator and the riser, and may also be connected thereto by pipeline.

[0100] The heavy oil raw material 33 is mixed with the regenerated catalyst that is from the heavy oil riser reactor pre-lift zone 4, enters the first reaction zone 3 of the heavy oil riser reactor, and performs a reaction under the catalytic cracking condition. The main operation conditions are as follows: reaction temperature 400-650 C. (preferably 480-560 C.), reaction pressure 0.11-0.4 MPa, contact time 0.05-5 seconds (preferably 0.1-3 seconds), and the weight ratio of the catalyst to the raw material generally 3-15, and preferably 5-12.

[0101] The cold-shocking agent 34 is mixing cooled with the mixture of the reactant oil gas and the catalyst that is from the first reaction zone 3, enters the second reaction zone 2 of the heavy oil riser reactor, to mainly perform secondary reactions such as hydrogen transfer, isomerization and aromatization, to further reduce the contents of olefins and sulfur, to increase the octane value. The main operation conditions are as follows: reaction temperature 350-620 C. (preferably 450-530 C.), reaction pressure 0.11-0.4 MPa, and contact time 0.5-30 seconds (preferably 1-5 seconds).

[0102] The mixture of the reactant oil gas and the catalyst that is from the second reaction zone 2 enters the settler 1, and perform the separation of the oil gas and the catalyst. The oil gas enters the fractionation and absorbing-stabilizing system, to perform fractionation and liquefied petroleum gas (LPG) recycling, and obtains products, including catalytic cracking gasoline, and unconverted oil.

[0103] The spent catalyst, after being steam stripped by the steam stripping section 1A of the settler 1, enters the charring tank 5A via the spent catalyst transporting pipe 7 and the controlling valve 20, undergoes quick charring in the present of the main air 38A (oxygen-containing gas including air and the like), and is transported upwardly to the regenerator 5 to be further charring regenerated, and secondary air 38B (oxygen-containing gas including air and the like) is supplemented from the bottom of the regenerator 5. The regenerated catalyst is outputted via the bottom of the regenerator 5, and enters the catalyst cooler 8A and the catalyst cooler 8B in two flows, wherein one flow of the cold regenerated catalyst is circularly used after or not after being mixed with the hot regenerated catalyst, and the other flow returns to the regenerator.

[0104] The injection point of the gas or liquid cold-shocking agent may be upstream or downstream of the injection point of the cold catalyst, to conveniently control the temperatures of the reaction zones, or to form another reaction zone.

[0105] FIG. 3 is a typical schematic diagram of applying the heavy oil catalytic conversion device of the present invention (jointly implemented with gasoline upgrading).

[0106] As shown in FIG. 3: the method of heavy oil catalytic conversion and the equipment thereof of the present invention comprises the heavy oil settler 1 and the gasoline settler 18. The heavy oil riser reactor comprises the pre-lift zone 4, the first reaction zone 3, the second reaction zone 2, the regenerator 5 and the gasoline riser 6. The spent catalyst transporting pipe 7 and a controlling valve (not shown in the figure) are provided between the regenerator 5 and the steam stripping section 1A of the settler 1 to communicate the regenerator 5 and the steam stripping section 1A of the heavy oil settler 1, to transport the spent catalyst to the regenerator 5. The spent catalyst transporting pipe 15 and the controlling valve 23 are provided to communicate the regenerator 5 and the steam stripping section 18A of the settler 18. The controlling valve 23 is a special controlling element that is provided for conveniently controlling the flow rate of the spent catalyst used for cold shock. Certainly, there may be many other controlling equipments and controlling methods, and that does not limit any special implementation of the concept of the present invention.

[0107] The regenerator is provided with 3 inner or outer heat removing equipments, that is, catalyst coolers, which comprise a catalyst inlet, a lower mixing buffering space, an inner heat removing element (including telescope type and coil pipe type) and a lower fluidized medium distributing installation, which are directly (or by pipeline) connected to the regenerator dense phase.

[0108] The catalyst cooler 8A is mainly for adjusting the reaction temperature of the first reaction zone of the heavy oil riser, to maintain it at the optimum value. The catalyst cooler 8B is mainly for adjusting the reaction temperature of the gasoline riser, to maintain it at the optimum value. The other catalyst cooler (not shown in the figure) is mainly for adjusting the regenerator temperature, to maintain it at the optimum value.

[0109] 35A, 35B are the fluidized medium such as air and steam, 36A, 36B are the rising medium such as air and steam, and 37A, 37B are the heat removing medium, including water, steam, air, oil products and the like.

[0110] According to the process requirements, any one or two of the three catalyst coolers may be not provided.

[0111] When the catalyst cooler mainly for adjusting the regenerator temperature is not provided, the regenerator temperature is controlled by adjusting the flow rate of the fluidized medium 35A, 35B (including air, steam and the like) of the catalyst cooler 8A and/or the catalyst cooler 8B and/or the quantity of the catalyst that returns to the regenerator and/or the thermal balance of the reaction regeneration system.

[0112] In order to conveniently control the temperature of the second reaction zone 2 of the heavy oil riser reactor, the cold-shocking agent 34 may be injected into the downstream of the first reaction zone, to conveniently control the temperature of the second reaction zone 2. The cold-shocking agent may be any one of a gas or a liquid (including water, oil products and the like) and a cold catalyst, and may also be two or more of them. The cold catalyst may be any one of a cold regenerated catalyst, a cold spent catalyst and a cold half-regenerated catalyst, and may also be two or more of them. The cold regenerated catalyst, when it is as the cold-shocking agent, may enter the auxiliary riser via the cold regenerated catalyst transporting pipe, and is transported by the pre-lift medium to the second reaction zone of the riser reactor (not shown in the figure).

[0113] The regenerator 5 is connected to the catalyst cooler 8A by the regenerated catalyst transporting pipe 10A, and the regenerated catalyst after being cooled enters the lower mixing buffering space 9A. The cold regenerated catalyst is connected to the heavy oil riser reactor pre-lift zone 4 by the cold regenerated catalyst transporting pipe 11A. The temperature of the cold regenerated catalyst that leaves the catalyst cooler 8A is controlled by adjusting the flow rate of the fluidized medium 35A (including air, steam and the like) and/or the flow rate of the rising medium 36A (including air, steam and the like) on the cold regenerated catalyst returning pipe 12A. The controlling valve 21A is a special controlling element that is provided for conveniently controlling the flow rate of the cold regenerated catalyst.

[0114] In order to conveniently control the temperature of the first reaction zone of the heavy oil riser reactor, a hot regenerated catalyst transporting pipe (including a controlling valve) that is connect to the heavy oil riser reactor pre-lift zone 4 is provided. The cold regenerated catalyst and the hot regenerated catalyst, after being mixed in the heavy oil riser reactor pre-lift zone 4, raise the temperature by the pre-lift medium 32 (including water, steam, refinery dry gases and the like) to reach the equilibrium. Certainly, there may be many other controlling equipments and controlling methods, and that does not limit any special implementation of the concept of the present invention.

[0115] The regenerator 5 is connected to the catalyst cooler 8B by the regenerated catalyst transporting pipe 10B, and the regenerated catalyst after being cooled enters the lower mixing buffering space 9B. The cold regenerated catalyst is connected to a gasoline riser pre-lift zone via the cold regenerated catalyst transporting pipe 11B. The temperature of the cold regenerated catalyst that leaves the catalyst cooler 8B is controlled by adjusting the flow rate of the fluidized medium 35B (including air, steam and the like) and/or the flow rate of the rising medium 36B (including air, steam and the like) on the cold regenerated catalyst returning pipe 12B. The controlling valve 21B is a special controlling element that is provided for conveniently controlling the flow rate of the cold regenerated catalyst.

[0116] The catalyst cooler 8A, 8B are provided with at least one fluidized medium distributor. The fluidized medium enters the catalyst cooler via the bottom distributor of the catalyst cooler, wherein the superficial gas velocity is 0-0.7 m/s (preferably 0.005-0.3 m/s, and most preferably 0.01-0.15 m/s), and the temperature of the cold regenerated catalyst is controlled mainly by adjusting a flow rate of the fluidized medium.

[0117] In order to conveniently control the temperature of the gasoline riser reactor, the hot regenerated catalyst transporting pipe 19B (including the controlling valve 22B) that is connect to the gasoline riser reactor pre-lift zone 4 is provided. The cold regenerated catalyst and the hot regenerated catalyst, after being mixed in the gasoline riser reactor pre-lift zone 4, raise the temperature by the pre-lift medium 30 (including water, steam, refinery dry gases and the like) to reach the equilibrium. Certainly, there may be many other controlling equipments and controlling methods, and that does not limit any special implementation of the concept of the present invention.

[0118] The catalyst cooler may be integral with the regenerator and the riser, and may also be connected thereto by pipeline.

[0119] The heavy oil raw material 33 is mixed with the regenerated catalyst that is from the heavy oil riser reactor pre-lift zone 4, after the cooling enters the first reaction zone 3 of the heavy oil riser reactor, and performs a reaction under the catalytic cracking condition. The main operation conditions are as follows: reaction temperature 400-650 C. (preferably 480-560 C.), reaction pressure 0.11-0.4 MPa, contact time 0.05-5 seconds (preferably 0.1-3 seconds), and the weight ratio of the catalyst to the raw material generally 5-15, and preferably 5-12.

[0120] The cold-shocking agent 34 is mixing cooled with the mixture of the reactant oil gas and the catalyst that is from the first reaction zone 3, enters the second reaction zone 2 of the heavy oil riser reactor, to mainly perform secondary reactions such as hydrogen transfer, isomerization and aromatization, to further reduce the contents of olefins and sulfur, to increase the octane value. The main operation conditions are as follows: reaction temperature 350-620 C. (preferably 450-530 C.), reaction pressure 0.11-0.4 MPa, and contact time 0.5-30 seconds (preferably 1-5 seconds).

[0121] Inferior gasoline 31 is mixed with a regenerated catalyst that is from the gasoline riser pre-lift zone, enters the gasoline riser reactor, contacts under the following conditions: reaction temperature 300-650 C. (preferably 400-500 C.), reaction pressure 0.11-0.4 MPa, contact time 0.5-30 seconds (preferably 1-15 seconds), and the weight ratio of the catalyst to the raw material generally 1-50, and preferably 2-20, to mainly perform gasoline upgrading reactions such as isomerization and aromatization, to reduce the contents of olefins and sulfur, to increase the octane value.

[0122] The mixture of the reactant oil gas and the catalyst that is from the second reaction zone 2 enters the settler 1, and performs the separation of the oil gas and the catalyst. The oil gas enters the fractionation and absorbing-stabilizing system singly or after being mixed with the oil gas that is from the settler 18, to perform fractionation and LPG recycling, and obtains products, including catalytic cracking gasoline, and unconverted oil. The spent catalyst, after being steam stripped by the steam stripping section 1A of the settler 1, enters the regenerator 5 via the spent catalyst transporting pipe 7 and the controlling valve (not shown).

[0123] The reactant stream that is from the gasoline riser 6 enters the settler 18 to perform the separation of the oil gas and the catalyst, and the oil gas singly enters the fractionation and absorbing-stabilizing system to perform fractionation and LPG recycling, and obtains products including catalytic cracking gasoline; or after being mixed with the oil gas that is from the settler 1, enters the commonly used fractionation and absorbing-stabilizing system to perform fractionation and liquefied petroleum gas (LPG) recycling.

[0124] The spent catalyst, after being steam stripped by the steam stripping section 18A of the settler 18, enters the regenerator 5 via the spent catalyst transporting pipe 15 and the controlling valve 23.

[0125] The spent catalyst that is from the steam stripping sections of the two settlers enters the regenerator 5, is charring regenerated in the present of the oxygen-containing gas 38 (including air and the like), and enters the catalyst cooler 8A and the catalyst cooler 86 in two flows, wherein the two flows of the cold regenerated catalyst are circularly used after or not after being mixed with the hot regenerated catalyst.

[0126] The injection point of the gas or liquid cold-shocking agent may be upstream or downstream of the injection point of the cold catalyst, to conveniently control the temperatures of the reaction zones, or to form another reaction zone.

[0127] FIG. 4 is a typical schematic diagram of applying the heavy oil catalytic conversion device of the present invention (commonly used settler).

[0128] As shown in FIG. 4: the method of heavy oil catalytic conversion and the equipment thereof of the present invention comprises the settler 1, two heavy oil riser reactors (comprising pre-lift zone 4A, 4B, first reaction zone 3A, 3B and second reaction zone 2A, 2B) that commonly use one settler, the regenerator 5 and the charring tank 5A. The spent catalyst transporting pipe 7 and the controlling valve 20 are provided between the charring tank 5A and the steam stripping section 1A of the settler 1 to communicate the charring tank 5A and the steam stripping section 1A, to transport the spent catalyst to the charring tank 5A. In order to ensure the initial charring temperature of the charring tank 5A, the regenerated catalyst cycling pipe 16 and the controlling valve 23 are provided.

[0129] The regenerator is provided with 3 inner or outer heat removing equipments, that is, catalyst coolers, which comprise a catalyst inlet, a lower mixing buffering space, an inner heat removing element (including telescope type and coil pipe type) and a lower fluidized medium distributing installation, which are directly (or by pipeline) connected to the regenerator dense phase.

[0130] The catalyst coolers 8A, 8B is mainly for adjusting the reaction temperatures of the first reaction zones of the two heavy oil riser reactors, to maintain them at the optimum values. The other catalyst cooler (not shown in the figure) is mainly for adjusting the regenerator temperature, to maintain it at the optimum value.

[0131] 35A, 35B are the fluidized medium such as air and steam, 36A, 36B are the rising medium such as air and steam, and 37A, 376 are the heat removing medium, including water, steam, air, oil products and the like.

[0132] According to the process requirements, any one or two of the three catalyst coolers may be not provided.

[0133] The regenerator 5 is connected to the catalyst cooler 8A by the regenerated catalyst transporting pipe 10A, and the regenerated catalyst after being cooled enters the lower mixing buffering space 9A. The cold regenerated catalyst is connected to the heavy oil riser reactor pre-lift zone 4A by the cold regenerated catalyst transporting pipe 11A. The temperature of the cold regenerated catalyst that leaves the catalyst cooler 8A is controlled by adjusting the flow rate of the fluidized medium 35A (including air, steam and the like) and/or the flow rate of the rising medium 36A (including air, steam and the like) on the cold regenerated catalyst returning pipe 12A. The controlling valve 21A is a special controlling element that is provided for conveniently controlling the flow rate of the cold regenerated catalyst.

[0134] The regenerator 5 is connected to the catalyst cooler 8B by the regenerated catalyst transporting pipe 10B, and the regenerated catalyst after being cooled enters the lower mixing buffering space 9B. The cold regenerated catalyst is connected to the heavy oil riser reactor pre-lift zone 4B by the cold regenerated catalyst transporting pipe 11B. The temperature of the cold regenerated catalyst that leaves the catalyst cooler 8A is controlled by adjusting the flow rate of the fluidized medium 35B, including air, steam and the like, and/or the flow rate of the rising medium 366, including air, steam and the like, on the cold regenerated catalyst returning pipe 12B. The controlling valve 21A is a special controlling element that is provided for conveniently controlling the flow rate of the cold regenerated catalyst.

[0135] The catalyst cooler 8A, 8B are provided with at least one fluidized medium distributor. The fluidized medium enters the catalyst cooler via the bottom distributor of the catalyst cooler, wherein the superficial gas velocity is 0-0.7 m/s (preferably 0.005-0.3 m/s, and most preferably 0.01-0.15 m/s), and the temperature of the cold regenerated catalyst is controlled mainly by adjusting a flow rate of the fluidized medium.

[0136] Certainly, there may be many other controlling equipments and controlling methods, and that does not limit any special implementation of the concept of the present invention.

[0137] In order to conveniently control the temperature of the first reaction zone of the two riser reactors, a hot regenerated catalyst transporting pipe (including a controlling valve) (not shown in the figure) that is connect to the heavy oil riser reactor pre-lift zones 4A, 4B may be provided. The cold regenerated catalyst and the hot regenerated catalyst, after being mixed in the heavy oil riser reactor pre-lift zones 4A, 4B, raise the temperature by the pre-lift mediums 32A, 32B (including water, steam, refinery dry gases and the like) to reach the equilibrium. Certainly, there may be many other controlling equipments and controlling methods, and that does not limit any special implementation of the concept of the present invention.

[0138] In order to conveniently control the temperature of the second reaction zone 2 of the two riser reactors, the cold-shocking agents 34A, 34B may be injected into the downstream of the first reaction zone, to conveniently control the temperature of the second reaction zone 2. The cold-shocking agent may be any one of a gas or a liquid (including water, oil products and the like) and a cold catalyst, and may also be two or more of them. The cold catalyst may be any one of a cold regenerated catalyst, a cold spent catalyst and a cold half-regenerated catalyst, and may also be two or more of them. The cold regenerated catalyst, when it is as the cold-shocking agent, may enter the auxiliary riser via the cold regenerated catalyst transporting pipe, and is transported by the pre-lift medium to the second reaction zone of the riser reactor (not shown in the figure).

[0139] The catalyst cooler may be integral with the regenerator and the riser, and may also be connected thereto by pipeline.

[0140] The heavy oil raw material (fresh raw material) 33A is mixed with the regenerated catalyst that is from the heavy oil riser reactor pre-lift zone 4A, enters the first reaction zone 3A of the heavy oil riser reactor, and performs a reaction under the catalytic cracking condition. The main operation conditions are as follows: reaction temperature 400-650 C. (preferably 480-560 C.), reaction pressure 0.11-0.4 MPa, contact time 0.05-5 seconds (preferably 0.1-3 seconds), and the weight ratio of the catalyst to the raw material generally 3-15, and preferably 5-12.

[0141] The cold-shocking agent 34A is mixing cooled with the mixture of the reactant oil gas and the catalyst that are from the first reaction zone 3A, enters the second reaction zone 2A of the heavy oil riser reactor, to mainly perform secondary reactions such as hydrogen transfer, isomerization and aromatization, to further reduce the contents of olefins and sulfur, to increase the octane value. The main operation conditions are as follows: reaction temperature 350-620 C. (preferably 450-530 C.), reaction pressure 0.11-0.4 MPa, and contact time 0.5-30 seconds (preferably 1-5 seconds).

[0142] The mixture of the reactant oil gas and the catalyst that is from the second reaction zone 2A enters the commonly used settler 1, to perform the separation of the oil gas and the catalyst.

[0143] The heavy oil raw material (recycle oil, slurry and the like) 33B is mixed with the regenerated catalyst that is from the heavy oil riser reactor pre-lift zone 4B, enters the first reaction zone 3B of the heavy oil riser reactor, and performs a reaction under the catalytic cracking condition. The main operation conditions are as follows: reaction temperature 400-650 C. (preferably 480-600 C.), reaction pressure 0.11-0.4 MPa, contact time 0.05-5 seconds (preferably 0.1-3 seconds), and the weight ratio of the catalyst to the raw material generally 3-15, and preferably 5-12.

[0144] The cold-shocking agent 346 is mixing cooled with the mixture of the reactant oil gas and the catalyst that is from the first reaction zone 3B, enters the second reaction zone 2B of the heavy oil riser reactor, to mainly perform secondary reactions such as hydrogen transfer, isomerization and aromatization, to further reduce the contents of olefins and sulfur, to increase the octane value. The main operation conditions are as follows: reaction temperature 350-620 C. (preferably 450-530 C.), reaction pressure 0.11-0.4 MPa, and contact time 0.5-30 seconds (preferably 1-5 seconds).

[0145] The mixture of the reactant oil gas and the catalyst that is from the second reaction zone 2B enters the commonly used settler 1, to perform the separation of the oil gas and the catalyst (the separation installation is not shown).

[0146] The mixtures of the oil gas and the catalyst that are from two heavy oil riser reactors are mixed, and perform further separation of the oil gas and the catalyst. The reactant oil gas after the separation enters a commonly used fractionation and absorbing-stabilizing system, to perform fractionation and liquefied petroleum gas (LPG) recycling.

[0147] The spent catalysts that are from two heavy oil riser reactors are mixed, enter the steam stripping section 1A of the settler 1, after steam stripping enter the charring tank 5A via the spent catalyst transporting pipe 7 and the controlling valve 20, undergo quick charring in the present of the main air 38A (oxygen-containing gas including air and the like), and are transported upwardly to the regenerator 5 to be further charring regenerated, and secondary air 38B (oxygen-containing gas including air and the like) is supplemented from the bottom of the regenerator 5. The regenerated catalyst is outputted via the bottom of the regenerator 5, and enters the catalyst cooler 8A, the catalyst cooler 8B and the catalyst cooler 8C in 3 flows, wherein one flow of the cold regenerated catalyst is circularly used after or not after being mixed with the hot regenerated catalyst, and the other flows return to the regenerator.

[0148] The injection point of the gas or liquid cold-shocking agent may be upstream or downstream of the injection point of the cold catalyst, to conveniently control the temperatures of the reaction zones, or to form another reaction zone.

[0149] The present application claims the right of priority of the Chinese Patent Application No. 201510004405.7, which was filed on Jan. 6, 2015, the disclosure of which is hereby incorporated in entirety as part of the present application.