METHOD AND EQUIPMENT FOR CIRCULATING COOLED REGENERATED CATALYST

Abstract

A method for circulating a cooled regenerated catalyst comprises the following steps: a regenerated catalyst derived from a regenerator is cooled to 200-720° C. by a catalyst cooler, which either directly enters into a riser reactor without mixing with hot regenerated catalyst, or enters the same after mixing with another portion of uncooled hot regenerated catalyst and thereby obtaining a hybrid regenerated catalyst with its temperature lower than that of the regenerator; a contact reaction between a hydrocarbon raw materials and the catalyst is performed in the riser reactor; the reaction product is introduced into a settling vessel to separate the catalyst and oil gas; the separated catalyst ready for regeneration is stream-stripped in a stream stripping phase and enters the regenerator for regeneration through charring; after cooling, the regenerated catalyst returns to the riser reactor for recycling.

Claims

1. A reaction method for Fluid Catalytic Cracking, comprising: reacting a hydrocarbon material with a catalyst in a riser reactor to generate gas and oil products and a reacted catalyst; separating the gas and oil products from the reacted catalyst in a settler; stripping the separated catalyst in a stripping section; burning and regenerating the stripped catalyst in a regenerator to obtain a hot regenerated catalyst; and cooling the hot regenerated catalyst by a regenerated catalyst cooler to form a cooled regenerated catalyst having a temperature in a range of 200° C. to 720° C., for cycling use; wherein blending and buffering the cooled regenerated catalyst in a device that provides a catalyst mixing buffer space being disposed in a downstream location of the regenerated catalyst cooler and before the cooled regenerated catalyst entering the reactor.

2. The method of claim 1, wherein the catalyst cooler is additionally used to adjust the temperature in the regenerator.

3. The method of claim 1, wherein the reactor comprises at least one reaction zones, wherein the regenerated catalyst cooler is connected to the reactor and is used to adjust the reaction temperature of the reactor; wherein the regenerated catalyst cooler is in a structure form of upflow type or downflow type and is used to adjust the reaction temperature of each reaction zone of the reactor.

4. The method of claim 1, wherein the temperature of a cold regenerated catalyst ranges from 360° C. to 650° C.

5. The method of claim 1, further comprising controlling the temperature of a cold regenerated catalyst by adjusting a flow rate of a fluidized medium, a heat-taking medium, the cold catalyst returning to the regenerator, or a combination thereof.

6. The method of claim 1, wherein the reaction temperature of the reactor is controlled by adjusting a ratio of a cold regenerated catalyst that enters the reactor and feed of the hydrocarbon materials that enter the reactor, adjusting the temperature of the cold regenerated catalyst, using a multi-point feeding technology, adding a quenching agent to the reactor, or a combination thereof.

7. The method of claim 1, wherein a heat-taking medium is selected from the group consisting of water, steam, air, and oils.

8. The method of claim 1, wherein a cold regenerated catalyst exiting from the catalyst cooler is a regenerated catalyst with a carbon content, an incompletely regenerated catalyst, or a contact agent with carbon content or coking particles.

9. The method of claim 1, wherein the method is used in FCC selected from the group consisting of heavy oil catalytic cracking, gas oil catalytic cracking, gasoline catalytic modification for improving quality, or light hydrocarbon catalytic conversion, or for other coke-burning process of gas-solid fluidized reaction including residue pre-processing, ethylene made by methanol, fluidize coking or flexible coking.

10. The method of claim 1, wherein the method is implemented independently for each reaction zone of a reactor (or fluidized bed reactor) of all kinds of FCC; or jointed to be implemented for each reaction zone of one, two or more reactors (or fluidized bed reactor) selected from the group consisting of tar risers and gasoline risers of the dual risers FCC units or different feeds reactors.

11. The method of claim 1, wherein the hydrocarbon material is a gasoline distillate; the reaction temperature of the gasoline riser reactor is 350° C.-650° C.

12. The method of claim 1, wherein the hydrocarbon material is a heavy oil; the reaction temperature of the gasoline riser reactor is 400° C.-650° C.

13. A reaction equipment for Fluid Catalytic Cracking, comprising a reactor, a regenerator, a regenerated catalyst cooler and a device that provides a catalyst mixing buffer space; wherein the reactor is configured to react a hydrocarbon material with a catalyst to generate gas and oil products and a reacted catalyst, the regenerator is configured to burn the reacted catalyst to obtain a hot regenerated catalyst, the regenerated catalyst cooler is configured to cool the hot regenerated catalyst to form a cooled regenerated catalyst having a temperature in a range of 200° C. to 720° C., for cycling use, and wherein the device that provides the catalyst mixing buffer space is disposed in a downstream location of the regenerated catalyst cooler and before a location that the cooled regenerated catalyst enters the reactor, and is configured to blend and buffer the cooled regenerated catalyst entering the reactor.

14. The reaction equipment of claim 13, wherein the catalyst cooler is additionally configured to adjust the temperature in the regenerator.

15. The reaction equipment of claim 13, wherein the reactor comprises at least one reaction zones, wherein the regenerated catalyst cooler is connected to the reactor and is used to adjust the reaction temperature of the reactor; wherein the regenerated catalyst cooler is in a structure form of upflow type or downflow type and is used to adjust the reaction temperature of each reaction zone of the reactor.

16. The reaction equipment of claim 13, wherein the regenerated catalyst cooler uses heat-taking medium selected from the group consisting of water, steam, air, and oils.

17. The reaction equipment of claim 13, wherein the reactor is gasoline riser reactor, a hydrocarbon material is reacted with the catalyst in the gasoline riser reactor to generate gas and oil products and a reacted catalyst, the hydrocarbon material is a gasoline distillate; the reaction temperature of the gasoline riser reactor is 350° C.-650° C.

18. The reaction equipment of claim 17, wherein the hydrocarbon material is a heavy oil; the reaction temperature of the gasoline riser reactor is 400° C.-650° C.

Description

DRAWING DESCRIPTION

[0072] The drawing is for the description of the present invention, it will not be restricted by any specific implement.

[0073] FIG. 1 is a schematic diagram of the cycling instruments of cold regenerated catalyst of the present invention.

[0074] FIG. 2 is a schematic diagram for heavy oil catalytic cracking units of one embodiment of the present invention.

[0075] FIG. 3 is a schematic diagram for heavy oil catalytic cracking units of another embodiment of the present invention.

[0076] FIG. 4 is a schematic diagram for heavy oil catalytic cracking units of yet another embodiment of the present invention.

DETAILED DESCRIPTION

[0077] As following, the present invention is further illustrated by the drawings.

[0078] Drawing 1: A special schematic diagram (a cold regenerated catalyst cycle process)

[0079] As FIG. 1 shown: the cycling instruments of cold regenerated catalyst of the present invention include the disengager 1, the riser 2 with the pre-lift sect 4 and the regenerator 5. For transporting the spent catalyst to the regenerator 5, the pipeline 7 of spent catalyst is set between the regenerator 5 and the stripping section 1A and the control valve 20 can connect the regenerator 5 and stripping section 1A.

[0080] The regenerator has two inside or outside taking-heat equipment, comprising the catalyst coolers, including the catalyst entrance connecting directly with the dense of the regenerator (or through a pipe), the mixing and buffering space in the lower part of the heat-taking equipment, internal heat-exchanging element (including bayonet-type or coil-type, etc.), the facilities for distribution of fluidizing media in the lower part of the heat-taking equipment.

[0081] Catalyst cooler 8A is mainly used to adjust the reaction temperature of the first reaction zone, to keep it in the best value. Another catalyst cooler (not shown) is primarily used for regulating the temperature of the regenerator to keep it in the best value. 35A is fluidized media, such as air, steam, etc., 36A is lifting media, such as air, steam, etc., 37A is taking-heat medium, including water, steam, air, and all kinds of oil.

[0082] The regenerator 5 is connected with the catalyst cooler 8A through regenerator duct 10A and the regenerated catalyst after being cooled enters the mixing and buffering space 9A in the lower part of the heat-taking equipment. The cold regenerated catalyst is connected with the pre-lift sect 4 of the riser reactor through the cold pipeline 11. Leaving the catalyst cooler 8A (the mixing buffer space 9A in the lower part of the heat-taking equipment), the temperature of the cold regenerated catalyst can be controlled by regulating the flow rate of the fluidizing media 35A (including air, steam, etc.) and/or the flow rate of the lifting media 36A (including air, steam, etc.) of the return pipe 12A of the cold regenerated catalyst. The control valve 21A is set as one of control components in order to facilitate the control of the flow rate of the cold regenerated catalyst.

[0083] For conveniently controlling the temperature of the reaction zone of the riser reactor, the pipeline of the hot regenerated catalyst (including the control valve) (not drawn) can connect the regenerator 5 directly with the pre-lift sect 4 of the heavy oil riser reactor. After lifting the cold regenerated catalyst mixed with hot regenerated catalyst in the pre-lift sect 4 of the riser reactor by the mixed media 32 of pre-lift area (including water, steam, and refinery gas, etc.), the temperature can reach to equilibrium.

[0084] Heavy oil riser reactor can also set the two reaction zones. The cold regenerated catalyst can enter the auxiliary riser through the pipeline of the cold regenerated catalyst, and reach the second reaction zone of the riser reactor as the cold-shocking agent by the lifting medium (not drawn).

[0085] According to requirements of the process, the catalyst cooler mainly used to adjust the temperature of the regenerator cannot be set. The temperature of the regenerator 5 can be controlled by regulating the flow rate of the medium 35A including the flow rates of air, steam, etc. and the lifting media 36A of the return pipe 12A of the cold regenerated catalyst.

[0086] Of course, There are also many other control equipment and control methods, which do not limit any specific implementations of the present invention.

[0087] The above-mentioned catalyst cooler can also be connected with the regenerator and the riser as a single entity, or connected through the pipelines.

[0088] Cooling to 200-720° C. (preferably 360-650° C.), the cold regenerated catalyst can enter into the riser reactor through pre-lift sect 4. Hydrocarbon raw materials in the riser reactor 2 react with the catalyst, and the flow after reaction can enter the disengager 1 for separation of catalysts and oil/gas, the spent catalyst after separation can be stripped by stripping section 1A, then enters into the regenerator 5 in the presence of the oxygen-containing gas 38 (including air) to be burnt for the regeneration. the regenerated catalyst after cooling can return directly to the riser reactor for cycling use.

[0089] FIG. 2 is a typical scheme of the heavy oil catalytic device of the present invention.

[0090] Such as shown in FIG. 2: the method and its equipment of the present invention for the heavy oil catalytic conversion, include the disengager 1, heavy oil riser reactor, which can include the pre-lift sect 4, the first reaction zone 3, the second reaction zone 2, the regenerator 5, the combustor 5A. The part between the combustor 5A and the stripper 1A of the disengager 1 set the pipeline 7 of the spent catalyst and control valve 20 to connect the combustor 5A and the stripping section 1A for transporting the spent catalyst to the combustor 5A. In order to ensure the start combusting temperature of the combustor 5A, the pipe 16 of the regenerated catalyst and control valve 23 can be set.

[0091] The regenerator has two inside or outside taking-heat equipment, comprising the catalyst coolers, including the catalyst entrance connecting directly with the dense of the regenerator (or through a pipe), the mixing and buffering space in the lower part of the heat-taking equipment, internal heat-exchanging element (including bayonet-type or coil-type, etc.), the facilities for distribution of fluidizing media in the lower part of the heat-taking equipment.

[0092] 35A, 35B are fluided media such as air, water, steam, etc. 36A, 36B are lifting media such as air, steam, etc. 37A, 37B are taking-heat media, including water, steam, air, and all kinds of oil. Catalyst cooler 8A is mainly used to adjust the reaction temperature of the first reaction zone, to keep it in the best value. Catalyst cooler 8B can primarily regulate the temperature of the regenerator for keeping it in the best value.

[0093] According to requirements of the process, any one or two of catalyst cooler 8A, 8B cannot be set.

[0094] The regenerator 5 is connected with the catalyst cooler 8A through regenerator duct 10A and the regenerated catalyst after being cooled enters the mixing and buffering space 9A in the lower part of the heat-taking equipment. The cold regenerated catalyst is connected with the pre-lift sect 4 of the riser reactor through the cold pipeline 11. Leaving the catalyst cooler 8A (the mixing buffer space 9A in the lower part of the heat-taking equipment), the temperature of the cold regenerated catalyst can be controlled by regulating the flow rate of the fluidized media 35A (including air, steam, etc.) and/or the flow rate of the lifting media 36A (including air, steam, etc.) of the return pipe 12A of the cold regenerated catalyst. The control valve 21A is set as one of control components in order to facilitate the control of the flow rate of the cold regenerated catalyst.

[0095] For conveniently controlling the temperature of the first reaction zone of the riser reactor, the pipeline of the hot regenerated catalyst (including the control valve) (not drawn) can connect the regenerator 5 directly with the pre-lift sect 4 of the heavy oil riser reactor. After lifting the cold regenerated catalyst mixed with hot regenerated catalyst in the pre-lift sect 4 of the riser reactor by the mixed media 32 of pre-lift area (including water, steam, and refinery gas, etc.), the temperature can reach to equilibrium.

[0096] Of course, there are also many other control equipment and control methods, which do not limit any specific implementations of the present invention.

[0097] In order to easily control the temperature of the second reaction zone 2 of the riser reactor, the cold-shocking agent 34 can be injected into the downstream of the first reaction zone to conveniently control the temperature of the second reaction zone. The above-mentioned cold-shocking agent can be any one of gas or liquid (including water, or any kinds of oil, etc.) and cold catalysts, or two or more of them. The cold catalyst is the one of the cold regenerated catalyst, the spent catalyst, or the cold semi-regenerated catalyst, or two or more of them.

[0098] As the cold-shocking agent, the cold regenerated catalyst can enter the auxiliary riser through the pipeline of the cold regenerated catalyst, and reach the second reaction zone of the riser reactor as the cold shock agent by the lifting medium (not drawn).

[0099] The regenerator 5 is connected with the catalyst cooler 8B through regenerator duct 10B and the regenerated catalyst after cooling enters into the mixing buffer space 9B in the lower part. The temperature of the regenerator 5 can be controlled by regulating the flow rate of the fluidized media 35B (including air, steam, etc.) and/or the flow rate of the lifting media 36B (including air, steam, etc.) of the return pipe 12B of the cold regenerated catalyst.

[0100] Of course, There are also many other control equipment and control methods, which do not limit any specific implementations of the present invention.

[0101] The above-mentioned catalyst cooler can also be connected with the regenerator and the riser as a single entity, or connected through the pipelines.

[0102] Heavy oil as the raw materials 33 and the regenerated catalyst from the pre-lifting zone 4 of the riser reactor with heavy oil are mixed and then enter into the first reaction zone 3 of the riser reactor with heavy oil in FCC. The main operating conditions are as follows: reaction temperature 400-650° C. (preferably 520-600° C.), reaction pressure 0.11˜0.4 MPa, contact time 0.05˜5 seconds (preferably 0.1-3 seconds), the ratio of catalysts and raw materials average of 3 to 15, preferably 5 to 12.

[0103] The cold-shocking agent 34, oil and gas from the first reaction zone 3, and the mixture of catalyst are mixed for cooling, and then enter into the second reaction zone 2 of the riser reactor with heavy oil, in which the secondary reactions such as hydrogen transfer, isomerization, aromatization occur for further reducing the olefin and sulfur content, and increasing octane. The main operating conditions are as follows: reaction temperature of 350-620° C. (preferably 450-530° C.), reaction pressure 0.11˜0.4 MPa, 0.5 to 30 seconds of contact time (preferably 1-5 seconds).

[0104] The mixture of the oil and gas from the second reaction zone 2 and the catalyst enters the disengager 1 and can be separated. The oil and gas enter the system of fractionation and absorption for fractionation and liquefied petroleum gas (LPG) recovery, to obtain catalytic cracking gasoline products and unconverted oil.

[0105] The spent catalyst stripped by the stripper 1A of the disengager 1 enters into the combustor 5A through the pipeline 7 of the spent catalyst and control valve 20. In the presence of the main wind 38A (oxygen-containing gases including air, etc.), the spent catalyst was fast burnt and transports to the regenerator 5 for further burning. The secondary air 38B (oxygen-containing gas, including air) is supplied on the bottom of the regenerator 5. The regenerated catalyst from the regenerator bottom enters the catalyst cooler 8A and catalyst cooler 8B by two routes. One is that the cold regenerated catalyst mixed or not with hot regenerated catalyst for cycling use, the other way is back to the regenerator.

[0106] The gas or liquid injection point of the cold-shocking agent is set at the upstream or downstream of the injection point in the cold catalyst to easily control the temperature of the reaction zone, or form another reaction zone.

[0107] FIG. 3 is a typical schematic diagram of the heavy oil catalytic conversion device (gasoline modified joint implementation) for the application of the present invention.

[0108] Such as shown in FIG. 3: the method and its equipment of the present invention for the heavy oil catalytic conversion, include the disengager 1 of heavy oil, the disengager 18 of gasoline, heavy oil riser reactor, which can include the pre-lift sect 4, the first reaction zone 3, the second reaction zone 2, the regenerator 5, the gasoline riser 6. The part between the regenerator 5 and the stripper 1A of the disengager 1 set the pipeline 7 of the spent catalyst and control valve (not drawn) to connect the regenerator 5 and the stripping section 1A of the disengager 1 of heavy oil for transporting the spent catalyst to the regenerator 5.

[0109] The pipeline 15 of the spent catalyst and the control valve 23 are set for connection with the regenerator 5 and the stripping section 18A of the disengager 18. The control valve 23 is set in order to easily control the flow rate of the spent catalyst for cold-shocking agents. Of course, There are also many other control equipment and control methods, which do not limit any specific implementations of the present invention.

[0110] The regenerator has two inside or outside taking-heat equipment, comprising the catalyst coolers, including the catalyst entrance connecting directly with the dense of the regenerator (or through a pipe), the mixing and buffering space in the lower part of the heat-taking equipment, internal heat-exchanging element (including bayonet-type or coil-type, etc.), the facilities for distribution of fluidizing media in the lower part of the heat-taking equipment.

[0111] Catalyst cooler 8A is mainly used to adjust the reaction temperature of the first reaction zone, to keep it in the best value. Catalyst cooler 8B is mainly used to adjust the reaction temperature of the gasoline riser, to keep it in the best value. Another catalyst cooler (not shown) is primarily used for regulating the temperature of the regenerator to keep it in the best value.

[0112] 35A, 35B are fluidized media, such as air, steam, etc., 36A, 36B are lifting media, such as air, steam, etc. 37A, 37B are taking-heat medium, including water, steam, air, and all kinds of oil.

[0113] According to requirements of the process, these three catalyst coolers in any one or two cannot be set.

[0114] When the catalyst coolers for adjusting the temperature of the regenerator is not set, the temperature of regenerator is controlled by adjusting the catalyst cooler 8A, and/or the flow rate of streaming media 35A, 35B (including air, steam, etc.) of catalyst cooler 8B and/or the content of the catalyst returned to the regenerator and/or controlled by the thermal equilibrium of the reaction and regeneration system.

[0115] In order to easily control the temperature of the second reaction zone 2 of the riser reactor, the cold-shocking agent 34 can be injected into the downstream of the first reaction zone to conveniently control the temperature of the second reaction zone. The above-mentioned cold-shocking agent can be any one of gas or liquid (including water, or any kinds of oil, etc.) and cold catalysts, or two or more of them. The cold catalyst is the one of the cold regenerated catalyst, the spent catalyst, or the cold semi-regenerated catalyst, or two or more of them. As the cold-shocking agent, the cold regenerated catalyst can enter the auxiliary riser through the pipeline of the cold regenerated catalyst, and reach the second reaction zone of the riser reactor as the cold shock agent by the lifting medium (not drawn).

[0116] The regenerator 5 is connected with the catalyst cooler 8A through regenerator duct 10A and the regenerated catalyst after cooling enters into the mixing buffer space 9A in the lower part. The cold regenerated catalyst is connected with the pre-lift sect 4 of the riser reactor through the cold pipeline 11A. Leaving the catalyst cooler 8A, the temperature of the cold regenerated catalyst can be controlled by regulating the flow rate of the fluidized media 35A (including air, steam, etc.) and/or the flow rate of the lifting media 36A (including air, steam, etc.) of the return pipe 12A of the cold regenerated catalyst. The control valve 21A is set as one of control components in order to facilitate the control of the flow rate of the cold regenerated catalyst.

[0117] For conveniently controlling the temperature of the first reaction zone of the riser reactor of heavy oil, the pipeline of the hot regenerated catalyst (including the control valve) can connect directly with the pre-lift sect 4 of the heavy oil riser reactor. After lifting the cold regenerated catalyst mixed with hot regenerated catalyst in the pre-lift sect 4 of the riser reactor by the mixed media 32 of pre-lift area (including water, steam, and refinery gas, etc.), the temperature can reach to equilibrium. Of course, There are also many other control equipment and control methods, which do not limit any specific implementations of the present invention.

[0118] The regenerator 5 is connected with the catalyst cooler 8B through regenerator duct 10B and the regenerated catalyst after cooling enters into the mixing buffer space 9B in the lower part. The cold regenerated catalyst is connected with the pre-lift sect of the riser reactor of gasoline through the cold pipeline 11B. Leaving the catalyst cooler 8B, the temperature of the cold regenerated catalyst can be controlled by regulating the flow rate of the fluidized media 35B (including air, steam, etc.) and/or the flow rate of the lifting media 36B (including air, steam, etc.) of the return pipe 12B of the cold regenerated catalyst. The control valve 21B is set as one of control components in order to facilitate the control of the flow rate of the cold regenerated catalyst.

[0119] To easily control the temperature of the riser reactor of gasoline, the pipeline 19B of the hot regenerated catalyst (including control valve 22B) is set connected with gasoline pre-lift zone 4. The cold regenerated catalyst with hot regenerated catalyst in pre-lift area 4 of gasoline riser reactor can be lifted and mixed by pre-lift medium 30 (including water, steam, and refinery gas and other) and then the temperature reaches equilibrium. Of course, There are also many other control equipment and control methods, which do not limit any specific implementations of the present invention.

[0120] The above-mentioned catalyst cooler can also be connected with the regenerator and the riser as a single entity, or connected through the pipelines.

[0121] Heavy oil as the raw materials 33 and the regenerated catalyst from the pre-lifting zone 4 of the riser reactor with heavy oil are mixed and then enter into the first reaction zone 3 of the riser reactor with heavy oil in FCC. The main operating conditions are as follows: reaction temperature 400-650° C. (preferably 520-600° C.), reaction pressure 0.11˜0.4 MPa, contact time 0.05˜5 seconds (preferably 0.1-3 seconds), the ratio of catalysts and raw materials average of 3 to 15, preferably 5 to 12.

[0122] The cold-shocking agent 34, oil and gas from the first reaction zone 3, and the mixture of catalyst are mixed for cooling, and then enter into the second reaction zone 2 of the riser reactor with heavy oil, in which the secondary reactions such as hydrogen transfer, isomerization, aromatization occur for further reducing the olefin and sulfur content, and increasing octane. The main operating conditions are as follows: reaction temperature of 350-620° C. (preferably 450-530° C.), reaction pressure 0.11˜0.4 MPa, 0.5 to 30 seconds of contact time (preferably 1-5 seconds).

[0123] Poor-quality gasoline 31 and the regenerated catalyst from the pre-lifting zone of the gasoline riser are mixed, and then enter into gasoline riser reactor. Under the conditions of the reaction temperature of 300-650° C. (preferably 400-560° C.), reaction pressure 0.11˜0.4 MPa, the contact time 0.5 to 30 seconds (preferably 1-15 seconds), the weight ratio of the catalyst and the raw materials the average of 1 to 50, preferably 2 to 20, mainly gasoline modification reactions, such as isomerization, aromatization happen to reduce the content of olefins and sulfur, and to improve the octane number.

[0124] The mixture of the oil and gas from the second reaction zone 2 and the catalyst enters the disengager 1 and can be separated. The oil and gas, or mixed with the oil and gas from the disengager 18 enter the system of fractionation and absorption for fractionation and liquefied petroleum gas (LPG) recovery, to obtain catalytic cracking gasoline products and unconverted oil. The spent catalyst stripped by the stripper 1A of the disengager 1 enters into the regenerator 5 through the pipeline 7 of the spent catalyst and control valve (not drawn).

[0125] The reactants from the gasoline riser 6 enter the disengager 18 and can be separated as the gas and oil or the catalyst. The oil and gas, enter the system of fractionation and absorption for fractionation and LPG recovery, to obtain catalytic cracking gasoline products; Or mixed with the oil and gas from the disengager 18 enter the system of fractionation and absorption for fractionation and liquefied petroleum gas (LPG) recovery.

[0126] The spent catalyst can be stripped by stripping section 18A, and then enters into the regenerator 5 by the pipeline 15 of the spent catalyst and the control valve 23. After entering the regenerator 5, the spent catalyst from the stripping sections of the two disengagers is burnt regenerated in the presence of oxygen-containing gas 38 (including air, etc.), then enters into the catalyst cooler 8A and catalyst cooling device 8B by two routes. The cold-regenerated catalyst of these two routes with/or not mixed with hot-regenerated catalyst for cycling use.

[0127] The gas or liquid injection point of the cold-shocking agent is set at the upstream or downstream of the injection point in the cold catalyst to easily control the temperature of the reaction zone, or form another reaction zone.

[0128] FIG. 4 is a typical Scheme of the heavy oil catalytic converter device (shared disengager) for the application of the present invention.

[0129] Such as shown in FIG. 4: the method and its equipment of the present invention for the heavy oil catalytic conversion, include the disengager 1, two heavy oil riser reactor shared one disengager, (which can include the pre-lift sect 4A, 4B, the first reaction zone 3A, 3B, the second reaction zone 2A, 2B), the regenerator 5, the combustor 5A. The part between the combustor 5 and the stripper 1A of the disengager 1 set the pipeline 7 of the spent catalyst and control valve 20 to connect the combustor 5a and the stripping section 1A for transporting the spent catalyst to the combustor 5A. To keep the start combusting temperature of the combustor 5, the cycling pipeline 16 of the spent catalyst and the control valve 23 are set.

[0130] The regenerator has two inside or outside taking-heat equipment, comprising the catalyst coolers, including the catalyst entrance connecting directly with the dense of the regenerator (or through a pipe), the mixing and buffering space in the lower part of the heat-taking equipment, internal heat-exchanging element (including bayonet-type or coil-type, etc.), the facilities for distribution of fluidizing media in the lower part of the heat-taking equipment.

[0131] Catalyst cooler 8A, 8B are mainly used to adjust the reaction temperature of the first reaction zone for two heavy oil riser reactors, to keep it in the best value. Another catalyst cooler (not shown) is primarily used for regulating the temperature of the regenerator to keep it in the best value.

[0132] 35A, 35B are fluidized media, such as air, steam, etc., 36A, 36B are lifting media, such as air, steam, etc. 37A, 37B are taking-heat medium, including water, steam, air, and all kinds of oil.

[0133] According to requirements of the process, any one or two in these three catalyst coolers cannot be set.

[0134] The regenerator 5 is connected with the catalyst cooler 8A through regenerator duct 10A and the regenerated catalyst after cooling enters into the mixing buffer space 9A in the lower part. The cold regenerated catalyst is connected with the pre-lift sect 4A of the riser reactor through the cold pipeline 11A. Leaving the catalyst cooler 8A, the temperature of the cold regenerated catalyst can be controlled by regulating the flow rate of the fluidized media 35A (including air, steam, etc.) and/or the flow rate of the lifting media 36A (including air, steam, etc.) of the return pipe 12A of the cold regenerated catalyst. The control valve 21A is set as one of control components in order to facilitate the control of the flow rate of the cold regenerated catalyst.

[0135] The regenerator 5 is connected with the catalyst cooler 8B through regenerator duct 10B and the regenerated catalyst after cooling enters into the mixing buffer space 9B in the lower part. The cold regenerated catalyst is connected with the pre-lift sect 4B of the riser reactor through the cold pipeline 11B. Leaving the catalyst cooler 8A, the temperature of the cold regenerated catalyst can be controlled by regulating the flow rate of the fluidized media 35B (including air, steam, etc.) and/or the flow rate of the lifting media 36B (including air, steam, etc.) of the return pipe 12B of the cold regenerated catalyst. The control valve 21B is set as one of control components in order to facilitate the control of the flow rate of the cold regenerated catalyst.

[0136] Of course, There are also many other control equipment and control methods, which do not limit any specific implementations of the present invention.

[0137] For conveniently controlling the temperature of the first reaction zone of the riser reactor of heavy oil, the pipeline of the hot regenerated catalyst (including the control valve) (not drawn) can connect directly with the pre-lift sect 4A, 4B of the heavy oil riser reactor. After lifting the cold regenerated catalyst mixed with hot regenerated catalyst in the pre-lift sect 4A, 4B of the riser reactor by the mixed media 32A, 32B of pre-lift area (including water, steam, and refinery gas, etc.), and the temperature can reach to equilibrium. Of course, There are also many other control equipment and control methods, which do not limit any specific implementations of the present invention.

[0138] In order to easily control the temperature of the second reaction zone 2 of the riser reactor, the cold-shocking agent 34A, 34 B can be injected into the downstream of the first reaction zone to conveniently control the temperature of the second reaction zone. The above-mentioned cold-shocking agent can be any one of gas or liquid (including water, or any kinds of oil, etc.) and cold catalysts, or two or more of them. The cold catalyst is the one of the cold regenerated catalyst, the spent catalyst, or the cold semi-regenerated catalyst, or two or more of them. As the cold-shocking agent, the cold regenerated catalyst can enter the auxiliary riser through the pipeline of the cold regenerated catalyst, and reach the second reaction zone of the riser reactor as the cold shock agent by the lifting medium (not drawn).

[0139] The above-mentioned catalyst cooler can also be connected with the regenerator and the riser as a single entity, or connected through the pipelines.

[0140] Heavy oil (as the raw materials) 33A and the regenerated catalyst from the pre-lifting zone 4A of the riser reactor with heavy oil are mixed and then enter into the first reaction zone 3A of the riser reactor with heavy oil in FCC. The main operating conditions are as follows: reaction temperature 400-650° C. (preferably 520-600° C.), reaction pressure 0.11˜0.4 MPa, contact time 0.05˜5 seconds (preferably 0.1-3 seconds), the ratio of catalysts and raw materials average of 3 to 15, preferably 5 to 12.

[0141] The cold-shocking agent 34A, oil and gas from the first reaction zone 3A, and the mixture of catalyst are mixed for cooling, and then enter into the second reaction zone 2A of the riser reactor with heavy oil, in which the secondary reactions such as hydrogen transfer, isomerization, aromatization occur for further reducing the olefin and sulfur content, and increasing octane. The main operating conditions are as follows: reaction temperature of 350-620° C. (preferably 450-530° C.), reaction pressure 0.11˜0.4 MPa, 0.5 to 30 seconds of contact time (preferably 1-5 seconds).

[0142] The mixture of the reactive oil and gas form the second reaction zone 2A and the catalyst enter into the shared disengager 1 for separation.

[0143] Heavy oil as raw materials (back to the refinery, slurry, etc.) 33B and the regenerated catalyst from the pre-lifting zone 4B of the riser reactor with heavy oil are mixed and then enter into the first reaction zone 3B of the riser reactor with heavy oil in FCC. The main operating conditions are as follows: reaction temperature 400-650° C. (preferably 520-600° C.), reaction pressure 0.11˜0.4 MPa, contact time 0.05˜5 seconds (preferably 0.1-3 seconds), the ratio of catalysts and raw materials average of 3 to 15, preferably 5 to 12.

[0144] The cold-shocking agent 34B, oil and gas from the first reaction zone 3B, and the mixture of catalyst are mixed for cooling, and then enter into the second reaction zone 2B of the riser reactor with heavy oil, in which the secondary reactions such as hydrogen transfer, isomerization, aromatization occur for further reducing the olefin and sulfur content, and increasing octane. The main operating conditions are as follows: reaction temperature of 350-620° C. (preferably 450-530° C.), reaction pressure 0.11˜0.4 MPa, 0.5 to 30 seconds of contact time (preferably 1-5 seconds).

[0145] The mixture of the reactive oil and gas form the second reaction zone 2B and the catalyst enter into the shared disengager 1 for separation (the separation device not drawn).

[0146] The mixture of the oil and gas from two heavy oil riser reactors and the catalyst can be further separated, then entered into the system of fractionation and absorption for fractionation and liquefied petroleum gas (LPG) recovery.

[0147] The spent catalysts from two heavy oil riser reactors are mixed and then enter into the stripper 1A of the disengager 1. After stripping, the mixtures enter into the combustor 5A through the pipeline 7 of the spent catalyst and control valve 20. In the presence of the main wind 38A (oxygen-containing gases including air, etc.), the spent catalyst was fast burnt and transports to the regenerator 5 for further burning. The secondary air 38B (oxygen-containing gas, including air) is supplied on the bottom of the regenerator 5. The regenerated catalyst from the regenerator 5 bottom enters the catalyst cooler 8A, catalyst cooler 8B and another catalyst cooler (not draw) by three routes. One is that the cold regenerated catalyst mixed or not with hot regenerated catalyst for recycling use, the other way is back to the regenerator.

[0148] The gas or liquid injection point of the cold-shocking agent is set at the upstream or downstream of the injection point in the cold catalyst to easily control the temperature of the reaction zone, or form another reaction zone.

Embodiment 1

[0149] To confirm the effect of the present invention, the process shown in FIG. 2, the raw materials shown in Table 1, Table 2 shows the process conditions and the GOR catalyst from Changling refinery catalyst plants. The experimental results are shown in Table 3.

TABLE-US-00001 TABLE 1 Flow atmospheric residue density, 20/4° C. 0.928 Carbon residue 7.8% (Wt)  Sulfur content 0.8% (Wt)  Nitrogen content 1800 PPm

[0150] In Table 2, the plan A in the art is conventional FCC process technology: the temperature of regenerator catalyst bed 680° C., the reaction temperature 525° C., the raw material temperature 200° C., the catalyst/oil ratio 6.7. Therefore, the temperature difference of the regenerated catalyst and raw materials is 480° C. The plan A in the art has the following deficiencies:

[0151] (1) raw material temperature of 200° C. to crack residue-containing raw materials is quite low.

[0152] (2) Although the temperature of the regenerator can meet the renewable requirements, but the temperature is too high when contacting with the raw material, prone to thermal cracking.

[0153] It should be understood that Table 2 of the embodiment is not limited. Unlike existing technologies, the plan B of the present invention, any combination of the catalyst circulation rate can be determined between the two risers in order to ensure that the catalyst/oil ratio required by the reaction instead of forcibly determined by the device thermal equilibrium.

TABLE-US-00002 TABLE 2 Plan A Plan B in the Parameter in the art present invention Temperature of riser reactor, ° C. 525 — Temperature of the first reaction zone ° C. — 525 Temperature of the second reaction — 505 zone, ° C. Feed temperature, ° C. 200 350 Regeneration temperature, ° C. 680 700 Temperature of the regenerated 680 630 catalyst in the entrance of riser, ° C. Temperature difference of catalyst 450 287 feed, ° C. Catalyst/oil ratio, weight/weight 6.7 8.6

TABLE-US-00003 TABLE 3 Plan A Plan B in the in the art present invention Product H2S % 0.6 0.7 Fuel gas % 5.5 4.2 LPG % 14.5 14.8 Gasoline % 38.9 41.9 Light cycle oil % 26.2 25.5 Decant oil % 5.0 5.0 Carbon % 9.3 7.9 Total 100.0 100.0 Gasoline Olefin content % 45.6 27.6 Aromatic content % 14.9 18.9 Sulfur content PPm 696 486 Octane number 89.7 90.6

[0154] The results in Table 3 showed that production rate of coke and dry gas decreased by 2.7%, olefin content in gasoline is reduced by 39%, 30% reduction in sulfur content, octane number (RON), increased by 0.9 units.