CN217120297U - A fluid catalytic cracking regenerator and catalytic cracking system - Google Patents

Abstract

The application relates to a fluidized catalytic cracking regenerator and catalytic cracking system, this fluidized catalytic cracking regenerator from the bottom up includes in proper order: a pre-lift zone, a char formation zone, a pre-combustion zone, and a main combustion zone. When the regenerator and the method are used for the fluidized catalytic cracking reaction with less coke generation, not only can the heat balance of the reaction-regeneration process be realized, but also the temperature rise of the catalyst in the coking process of the regenerator is uniform, no local hot spot exists, and the physical and chemical properties of the catalyst are not damaged.

Description

A fluid catalytic cracking regenerator and catalytic cracking system

technical field

The present application relates to the technical field of fluid catalytic cracking, and more particularly, to a fluid catalytic cracking regenerator and a catalytic cracking system.

Background technique

The fluid catalytic cracking reaction process is an autothermal equilibrium process, and a large amount of heat energy at a high temperature released during the catalyst regeneration process can just meet the needs of the lower temperature cracking reaction process. The catalyst circulating between the reactor and the regenerator has a sufficient quantity and heat capacity, so the catalyst can both serve as an active site for the reaction and a heat carrier for transferring thermal energy. The heat carrier flows between the reactor and the regenerator, continuously obtaining heat from one end and supplying heat to the other end. The establishment of heat balance requires certain conditions, on which the cracking and regeneration can be maintained to reach the specified temperature. For a catalytic cracking industrial unit, the basis of the heat balance between the reactor and the regenerator is that the reaction can generate enough coke, and the coke is burned during the regeneration process, releasing heat for the reaction to use.

With the development of oil refining process, especially the intensified trend of crude oil heavier/inferior quality and the improvement of oil product quality, the hydrogenation process is more widely used. When the hydro-upgraded raw material is used as the raw material for catalytic cracking, although the product structure and quality have been greatly improved, the catalytic cracking unit itself has a problem of insufficient coke production and insufficient heat supply. In addition, in the catalytic cracking technology with low-carbon olefins as the main target product, the cracking reaction conversion rate is high, the reaction temperature is high, and the reaction heat is large, and the heat required for the reaction is more than conventional fluidized catalytic regenerators or other catalytic conversion methods. , the coke generated by self-cracking often cannot meet the needs of the heat balance of the reaction-regeneration system. When the coke is insufficient in the reaction process, the method of supplying fuel oil to the regenerator is usually used to provide the required heat for the reaction. Since the catalytic cracking uses a catalyst with molecular sieve as the active component, the local high temperature generated by the combustion of the fuel oil in the regenerator gradually releases the molecular sieve framework aluminum, resulting in damage to the catalyst, and this damage is irreversible.

The prior art does not fundamentally solve the influence of the high temperature hot spot generated by the partial combustion of the externally-supplemented fuel oil on the skeleton structure and reaction performance of the catalyst.

Utility model content

The purpose of the present application is to provide a catalytic cracking regenerator, which solves the problem of insufficient heat in the catalytic cracking reaction process without affecting the physical and chemical properties of the catalyst.

The present application provides a fluidized catalytic cracking regenerator, which sequentially includes from bottom to top:

pre-lift area,

coke area,

pre-combustion zone, and

main combustion zone,

Wherein, the outlet of the pre-lifting zone is in fluid communication with the inlet of the coking zone, the outlet of the coking zone is in fluid communication with the inlet of the pre-combustion zone, and the outlet of the pre-burning zone is in fluid communication with the inlet of the main combustion zone; The pre-combustion area is communicated with the main combustion area through an external catalyst circulation pipe;

One or more supplementary fuel oil inlets are arranged on the side wall of the pre-lifting zone and/or the side wall of the coking zone;

One or more supplementary oxygen-containing gas inlets are arranged on the sidewall of the pre-combustion zone;

One or more main oxygen-containing gas inlets are arranged on the side wall of the main combustion zone.

In one embodiment, one or more of the supplementary fuel oil inlets are provided on the side wall of the pre-lift area, and the distances between the fuel oil inlets and the outlet end of the pre-lift area are independently pre-lift area. 0% to 15% of the height of the lift zone; preferably 0% to 10%.

In one embodiment, one or more supplementary fuel oil inlets are provided on the sidewall of the green coke zone, and the distances between the fuel oil inlets and the bottom of the green coke zone are independently the height of the green coke zone 0% to 15%, preferably 0% to 10%.

In one embodiment, the supplemental oxygen-containing gas inlet is disposed at the lower part of the pre-combustion zone, and the distances between the supplementary oxygen-containing gas inlet nozzles and the bottom of the pre-combustion zone are independently the height of the pre-combustion zone. 15% to 30%.

In one embodiment, the axial angle of the supplemental oxygen-containing gas nozzle line is 5°-85°, preferably 15°-75°.

In one embodiment, the distance between the connection position of the catalyst circulation pipe and the pre-combustion zone and the bottom of the pre-combustion zone is independently 0% to 10% of the height of the pre-combustion zone.

In one embodiment, the main combustion zone, the coke generating zone, and the pre-combustion zone are arranged coaxially.

In one embodiment, a catalyst lead-out pipe is provided on the top of the outlet of the pre-combustion area, and the outlet of the pre-combustion area and the catalyst lead-out pipe are located inside the main combustion area.

In one embodiment, the lower portion of the primary combustion zone is provided with a gas distributor configured to distribute input through one or more primary oxygen-containing gas inlets provided on the sidewall of the primary combustion zone The main regeneration oxygen-containing gas.

In one embodiment, the ratio of the inner diameter of the pre-lifting zone to the coke green zone is 0.2:1 to 0.8:1, and the ratio of the height of the pre-lift zone to the height of the coke green zone is 0.5 : 1 to 1.5: 1.

In one embodiment, the pre-combustion zone includes a partial combustion section and an outlet section, and the inner diameter of the partial combustion section is larger than the inner diameter of the outlet section.

In one embodiment, the ratio of the inner diameter of the partial combustion section to the inner diameter of the outlet section is 10:1 to 2:1, and the ratio of the height of the partial combustion section to the height of the outlet section is 10 :1 to 2:1.

The present application provides a catalytic cracking regeneration method, which is carried out in the above-mentioned fluid catalytic cracking regenerator of the present application, comprising the following steps:

The catalyst to be produced is introduced into the pre-lifting zone of the regenerator to contact and mix with the pre-lifting medium and move upward;

After the atomization medium is mixed with the combustion oil, it is injected into the fluidized catalytic cracking regenerator at one or more supplementary fuel oil inlets, contacts with the existing stream in the fluidized catalytic cracking regenerator, and a coke-forming reaction occurs to obtain Catalysts with coke;

The coke-bearing catalyst enters the pre-combustion zone, is mixed with the regenerated catalyst circulated back to the pre-combustion zone through the catalyst circulation pipe, and is heated up in the presence of oxygen-depleted gas introduced from one or more of the supplemental oxygen-containing gas inlets. partial combustion reaction;

The partially charred catalyst enters the main combustion zone and undergoes a complete combustion reaction in the presence of the oxygen-enriched gas introduced from one or more of the main oxygen-containing gas inlets to obtain a regenerated catalyst.

In one embodiment, the pre-lifting medium in the pre-lifting zone is nitrogen, water vapor or a mixture thereof; the atomizing medium is nitrogen.

In one embodiment, the mass ratio of the atomizing medium to the combustion oil is 1:1 to 1:100.

In one embodiment, the linear velocity of the pre-combustion zone is 1.2 m/s-2.2 m/s; the oxygen content in the oxygen-depleted gas is 1 vol% to 20 vol%, further preferably, the oxygen-depleted gas The oxygen content in the body is 5% to 10% by volume.

In one embodiment, the temperature in the pre-combustion zone is 550-650°C.

In one embodiment, the oxygen content of the oxygen-enriched gas in the main combustion zone is 21 to 100 vol%, and further preferably, the oxygen content of the oxygen-enriched gas is 21 to 85 vol%.

In one embodiment, the temperature in the primary combustion zone is 600-800°C.

The present application also provides a catalytic cracking system comprising the above-mentioned fluid catalytic cracking regenerator of the present application.

When the regenerator and method of the present application are used in the fluidized catalytic cracking reaction with less coke, not only the heat balance of the reaction-regeneration process can be achieved, but also the temperature rise of the catalyst during the coking process of the regenerator is uniform, and there is no local hot spot. and chemical properties without damage.

Description of drawings

The accompanying drawings are used to provide a further understanding of the present application, and constitute a part of the specification, and together with the following specific embodiments, are used to explain the present application, but do not constitute a limitation to the present application. In the attached image:

FIG. 1 is a schematic diagram of an embodiment of a catalytic cracking regenerator provided by the application.

Detailed ways

The present application will be further described in detail below through the accompanying drawings and embodiments. From these descriptions, the features and advantages of the present application will become more apparent.

The word "exemplary" is used exclusively herein to mean "serving as an example, embodiment, or illustration." Any embodiment described herein as "exemplary" is not necessarily to be construed as preferred or advantageous over other embodiments. While various aspects of the embodiments are shown in the drawings, the drawings are not necessarily drawn to scale unless otherwise indicated.

In addition, the technical features involved in the different embodiments of the present application described below can be combined with each other as long as there is no conflict with each other.

Any specific numerical value disclosed herein, including the endpoints of a numerical range, is not limited to the precise value of the numerical value, but is to be understood to encompass values approximating the precise value, such as within ±5% of the precise value. all possible values. And, for the disclosed numerical range, between the endpoint values of the range, between the endpoint values and the specific point values in the range, and between the specific point values, one or more new values can be obtained in any combination. Numerical ranges, these new numerical ranges should also be considered to be specifically disclosed herein.

In this application, the terms "upstream" and "downstream" are both based on the flow direction of the reaction material. For example, "upstream" refers to a position below and "downstream" refers to a position above when the reactant stream flows from the bottom up.

Unless otherwise specified, terms used herein have the same meaning as commonly understood by those skilled in the art, and if a term is defined herein and its definition is different from that commonly understood in the art, the definition herein shall prevail.

The present application provides a fluidized catalytic cracking regenerator 100, which includes, from bottom to top, interconnected:

pre-lift zone 1,

coke zone 2,

pre-combustion zone 3, and

main combustion zone 4,

Wherein, the outlet of the pre-lifting zone is in fluid communication with the inlet of the coking zone, the outlet of the coking zone is in fluid communication with the inlet of the pre-combustion zone, and the outlet of the pre-burning zone is in fluid communication with the inlet of the main combustion zone; The pre-combustion zone 3 is communicated with the main combustion zone 4 through an external catalyst circulation pipe 12;

One or more supplementary fuel oil inlets 10 are provided on the side wall of the pre-lifting zone 1 and/or the side wall of the coking zone 2;

One or more supplementary oxygen-containing gas inlets 11 are arranged on the side wall of the pre-combustion zone 3;

One or more main oxygen-containing gas inlets 14 are provided on the side wall of the main combustion zone 4 .

The fluid catalytic cracking regenerator 100 of the present application includes a pre-lift zone 1 , which is disposed at the lowermost part of the fluid catalytic cracking regenerator 100 , but upstream of the flow direction of the fluid catalytic cracking regenerator 100 of the to-be-grown catalyst. The lower part of the pre-lifting zone 1 is also provided with a catalyst-to-be-grown inlet 9 for delivering the catalyst to be generated from the catalytic cracking reaction unit to the fluidized catalytic cracking regenerator 100 for regeneration. The pre-lift medium is input from the lower inlet 8 of the pre-lift zone 1, and is used to lift the input to-be-grown catalyst upward. The pre-lift medium used in the pre-lift zone can be nitrogen, water vapor or a mixture thereof.

In one embodiment, the pre-lifting zone 1 may be in the form of a hollow cylinder of equal diameter, and its aspect ratio may be 30:1 to 3:1.

As described above, in the fluidized catalytic cracking regenerator 100 of the present application, one or more supplementary fuel oils are provided on the side wall of the pre-lift zone 1 and/or the side wall of the coking zone 2 The inlet 10 is used for injecting supplementary fuel oil.

In one embodiment, one or more supplementary fuel oil inlets 10 are provided on the side wall of the pre-lift area 1 . In this embodiment, the distances L ₁₀ of the fuel oil inlet 10 from the outlet end of the pre-lift area are each independently 0% to 15% of the pre-lift area height h ₁ ; preferably 0% to 10%.

In one embodiment, one or more of the supplementary fuel oil inlets 10 are provided on the side wall of the coking zone 2, and the distances between the fuel oil inlets and the bottom of the coking zone are independently coke 0% to 15% of the zone height, preferably 0% to 10%.

By injecting supplementary fuel oil into the pre-lifting zone and/or the coking zone, the injected fuel oil can be mixed with the catalyst and form coke under low temperature, oxygen-free or oxygen-depleted fluidization conditions, and the coke-attached catalyst can be The coking zone is further rectified, which can make the coke evenly distributed on the catalyst.

The fluidized catalytic cracking regenerator 100 of the present application includes a coke producing zone 2, which is arranged above the pre-lifting zone 1, and is used to further rectify the coke-attached catalyst in the coke producing zone 2, so that the coke is evenly distributed on the catalyst. In one embodiment, the coking zone is a pneumatically conveyed bed or a fast fluidized bed.

In one embodiment, the coke green zone 2 can also be in the form of a hollow cylinder with equal diameter, and its aspect ratio can be 30:1 to 3:1. In one embodiment, the ratio of the inner diameters of the pre-lifting zone 1 to the coke-green zone 2 may be 0.2:1 to 0.8:1, and the height h1 of the pre-lift zone 1 and the coke-green zone 2 The ratio of height h2 can be from 0.5:1 to 1.5:1.

In an embodiment, the coke green zone 2 and the pre-lift zone 1 may be connected by a first connection section 21 . In one embodiment, the longitudinal section of the first connecting segment 21 is an isosceles trapezoid, and the camber angle β of the side of the isosceles trapezoid is 5-85°.

The fuel oil injected through the supplemental fuel oil inlet 10 may include straight run distillates or secondary processed distillates. Preferably, the secondary processed distillate may be selected from a blend of one or more of catalytically cracked diesel, coker gasoline, coker diesel and coker wax oil. In order to better disperse the fuel oil, the fuel oil can be mixed with the atomizing medium, and the mixture of the two can be injected through the supplementary fuel oil inlet 10 . The atomizing medium may include nitrogen and the like. In one embodiment, the mass ratio of fuel oil to atomizing medium is 1:1 to 100:1, for example, 1:1 to 50:1, or 1:1 to 20:1.

The fluid catalytic cracking regenerator 100 of the present application includes a pre-combustion zone 3, and one or more supplementary oxygen-containing gas inlets 11 are provided on the side wall of the pre-combustion zone 3. By setting the pre-combustion zone 3, the catalyst with evenly attached coke enters the pre-combustion zone, and contacts the oxygen-containing gas at a relatively low temperature and a fast gas linear velocity, so that the coke on the catalyst is partially burned, and the surface temperature of the catalyst is reduced. Step up.

In an embodiment, the supplemental oxygen-containing gas inlet ₁₁ is arranged at the lower part of the pre-combustion zone 3, and the distance L11 of the supplementary oxygen-containing gas inlet nozzle from the bottom of the pre-combustion zone is independently a pre-combustion zone. 15% to ₃₀ % of the height h3 of the combustion zone.

In one embodiment, the axial angle α of the supplemental oxygen-containing gas nozzle line is 5°-85°, preferably 15°-75°.

The pre-combustion area 3 is also communicated with the main combustion area 4 through an external catalyst circulation pipe 12 . In one embodiment, the distance L ₁₂ between the connection position of the catalyst circulation pipe 12 and the pre-combustion zone 3 and the bottom of the pre-combustion zone is independently 0% to 10% of the pre-combustion zone height h ₃ . A part of the regenerated catalyst in the main combustion zone 4 can be circulated back to the pre-combustion zone 3 through the catalyst circulation pipe 12 and mixed with the catalyst from the coking zone 2 to increase its temperature.

As shown in FIG. 1 , in one embodiment, the pre-combustion zone 3 includes a partial combustion section 31 and an outlet section 32 , and the inner diameter of the partial combustion section 31 is larger than the inner diameter of the outlet section 32 . In one embodiment, the ratio of the inner diameter of the partial combustion section 31 to the inner diameter of the outlet section 32 is 10:1 to 2:1, and the height of the partial combustion section 31 is equal to the height of the outlet section 32 The ratio is 10:1 to 2:1.

In one embodiment, the pre-lifting zone, the coke-generating zone, and the pre-combustion zone are all in the form of hollow cylinders, and can be arranged coaxially.

The fluidized catalytic cracking regenerator 100 of the present application includes a main combustion zone 4, which is used for contacting the catalyst partially coked in the pre-combustion zone with oxygen-rich gas in the main combustion zone, and a complete combustion reaction occurs, releasing heat and burning The high-temperature regenerated catalyst from which the coke has been removed is used for the reaction cycle.

In one embodiment, the main combustion zone and the pre-combustion zone may be coaxially arranged or arranged in a high and low parallel arrangement. In one embodiment, a catalyst lead-out pipe 13 is provided at the top of the outlet of the pre-combustion area, and the outlet of the pre-combustion area together with the catalyst lead-out pipe 13 is located inside the main combustion area 4, so that the The catalyst in the pre-combustion zone 3 is directly introduced into the main combustion zone 4 through the catalyst lead-out pipe 13 , so as to be completely burned and regenerated in the main combustion zone 4 . The main combustion zone 4 of the present application can adopt the structure of the existing conventional catalytic cracking single-stage regenerator, and can be opened at its lower part, so that the outlet of the pre-combustion zone together with the catalyst lead-out pipe 13 is accommodated in the main combustion zone through the opening. Inside of Zone 4. In the main combustion zone 4, under the action of high temperature and oxygen-enriched gas, the catalyst with part of the coke is fully burned and exothermic, and the heat required for the reaction is supplied, so that the coking environment on the catalyst can be relaxed, and the catalyst The gradual temperature rise is achieved, which protects the physical and chemical properties of the catalyst to the greatest extent.

As mentioned above, the lower part of the main combustion zone 3 is provided with a connection of the catalyst circulation pipe 12 , so that a part of the regenerated catalyst in the main combustion zone 4 is circulated back to the pre-combustion zone 3 .

In the catalytic cracking regenerator 100 provided in the present application, one or more main oxygen-containing gas inlets 14 are provided on the side wall of the main combustion zone 4 for feeding oxygen-enriched gas to the main combustion zone 4 . In one embodiment, the bottom of the main combustion zone 4 is provided with a main air distributor 7, and the lower side wall is provided with one or more main oxygen-containing gas inlets 14, and the gas distributor 7 is configured to distribute through the main air distributor 7. One or more main oxygen-containing gas inlets 14 provided on the side walls of the combustion zone input the main regeneration oxygen-containing gas. The main air distributor 7 can be a main air distributor well known to those skilled in the art. For example, the main air distributor can be a distribution plate and a distribution pipe, for example, the distribution pipe can be an annular distribution pipe and a dendritic distribution pipe. The catalyst completely regenerated in the main combustion zone 4 is sent out of the regenerator through the outlet 15 for recycling in the catalytic cracking reaction.

The main combustion zone 4 is also in fluid communication with the inlet of the gas-solid separation device 5 , and the regenerated flue gas is separated from the entrained catalyst by the gas-solid separation device 5 and then enters the energy recovery system through the pipeline 6 . The gas-solid separation equipment 5 may adopt equipment well known to those skilled in the art. For example, the gas-solid separation apparatus may comprise a cyclone.

The catalytic cracking regenerator of the present application is simple in structure, easy to implement, and can be implemented by adapting the existing industrial device regenerator, and has strong operability, especially the catalytic cracking with chemical raw materials such as low-carbon olefins as the main target products The device can not only fundamentally solve the problem of heat balance, but also reduce the damage to the catalyst and regeneration equipment caused by the traditional fuel injection method, which not only saves the cost of the catalyst, but also improves the economic benefit of the refinery.

The present application also provides a catalytic cracking regeneration method, which is carried out in the above-mentioned fluid catalytic cracking regenerator of the present application, comprising the following steps:

The catalyst to be produced is introduced into the pre-lifting zone of the regenerator to contact and mix with the pre-lifting medium and move upward;

After the atomization medium is mixed with the combustion oil, it is injected into the fluidized catalytic cracking regenerator at one or more supplementary fuel oil inlets, contacts with the existing stream in the fluidized catalytic cracking regenerator, and a coke-forming reaction occurs to obtain Catalysts with coke;

The coke-bearing catalyst enters the pre-combustion zone, is mixed with the regenerated catalyst circulated back to the pre-combustion zone through the catalyst circulation pipe, and is heated up in the presence of oxygen-depleted gas introduced from one or more of the supplemental oxygen-containing gas inlets. partial combustion reaction;

The partially charred catalyst enters the main combustion zone and undergoes a complete combustion reaction in the presence of the oxygen-enriched gas introduced from one or more of the main oxygen-containing gas inlets to obtain a regenerated catalyst.

In one embodiment, the pre-lifting medium in the pre-lifting zone is nitrogen, water vapor or a mixture thereof; the atomizing medium is nitrogen.

In one embodiment, the mass ratio of the atomizing medium to the combustion oil is 1:1 to 1:100. In actual operation, the injection amount of the mixture of the atomizing medium and the combustion oil is adjusted according to the feed amount of the raw material oil in the reactor connected to the regenerator, and is used to control the temperature of the regenerated regenerated catalyst to be 600-800 °C .

In one embodiment, the linear velocity of the pre-combustion zone is 1.2 m/s-2.2 m/s; the oxygen content in the oxygen-depleted gas is 1 vol% to 20 vol%, further preferably, the oxygen-depleted gas The oxygen content in the body is 5% to 10% by volume.

In one embodiment, the temperature in the pre-combustion zone is 550-650°C.

In one embodiment, the oxygen content of the oxygen-enriched gas in the main combustion zone is 21 to 100 vol%, and further preferably, the oxygen content of the oxygen-enriched gas is 21 to 85 vol%.

In one embodiment, the temperature in the primary combustion zone is 600-800°C.

It should be noted that the above embodiments of the fluidized catalytic cracking regenerator are also applicable to the regeneration method of the present application, which will not be repeated here.

The present application also provides a catalytic cracking system comprising the fluid catalytic cracking regenerator of the present application.

In addition, the catalytic cracking system also includes a catalytic cracking reaction device, an oil separation device, a stripping device and an optional reaction product separation device.

In one embodiment, the catalytic cracking reaction unit includes one or more catalytic cracking reactors. The fluid catalytic cracking regenerator of the present application can be connected with the one or more catalytic cracking reactors, so that the catalyst to be produced from the one or more catalytic cracking reactors enters the fluid catalytic cracking regenerator of the present application for processing. Regenerate and recycle the regenerated catalyst back to the one or more catalytic cracking reactors for reuse.

In the catalytic cracking system provided by the present application, the catalytic cracking reactor, the stripping device, the oil separation device, the reaction product separation device, etc. can all use equipment known to those skilled in the art, and the connection between these devices is also This can be done in a manner known in the art. For example, the oil separation device may include a cyclone separator and an outlet quick separator. In some specific embodiments, the oil separation device includes a settler arranged coaxially with the catalytic cracking reactor or arranged in parallel with each other.

The regenerator and method of the present application are especially suitable for the fluidized catalytic cracking reaction with less coke, not only can realize the heat balance of the reaction-regeneration process, but also can make the temperature rise of the catalyst uniform during the coking process of the regenerator, without local hot spots, and The physical and chemical properties of the catalyst are not impaired.

The present application will be further described below with reference to the preferred embodiments shown in the accompanying drawings, but the present application will not be limited thereby.

FIG. 1 shows a preferred embodiment of the catalytic cracking regenerator of the present application, wherein the catalytic cracking regenerator includes a pre-lifting zone 1 , a coking zone 2 , a pre-combustion zone 3 and a main combustion zone 4 sequentially from bottom to top. The lower part of the pre-lifting area 1 is provided with a catalyst inlet 9 to be produced, and the end of the pre-lifting area 1 is provided with a fuel oil inlet 10 . The lower sidewall of the pre-combustion zone 3 is provided with one or more oxygen-containing gas inlets 11 . The bottom of the main combustion zone is provided with a main air distributor 7 , and the lower side wall is provided with one or more, for example, one, two or more main air inlets 14 .

The pre-lifting medium enters the catalytic cracking regenerator from the bottom of the pre-lifting zone 1 through the pipeline 8, and the pre-lifting medium can be nitrogen, water vapor or a mixture thereof. The to-be-grown catalyst from the to-be-grown catalyst inlet 9 enters the lower part of the pre-lift zone 1 and moves upward under the lifting action of the pre-lift medium. The fuel oil and atomizing medium are injected into the end of the pre-lifting zone 1 through the fuel oil inlet 10, mixed and contacted with the existing catalyst in the regenerator, and a coke reaction occurs. The catalyst with coke flows upward, enters the pre-combustion zone 3, is mixed with the high-temperature regenerant returned by the catalyst circulation pipe 12 and warms up, and then contacts with the oxygen-containing gas injected through the oxygen-containing gas inlet 11 and undergoes a partial scorching reaction. Part of the coke on the catalyst was removed. Part of the charcoaled catalyst enters the main combustion zone 4 through the lead-out pipe 13, contacts with the main air injected through the main air inlet 14 and the main air distributor 7 and undergoes a complete combustion reaction, completely releasing heat, and the regenerated catalyst is sent out through the outlet 15. The regenerator is used for the reaction cycle; the regenerated flue gas is separated from the entrained catalyst by the cyclone separator 5 and then enters the energy recovery system through the pipeline 6.

Example

The following examples will further illustrate the application, but do not limit the application accordingly. The catalyst used in the test is a ready-made catalyst, the carbon content is 0.8% by weight, and the combustion oil is catalytic cracking diesel.

Example 1

The structure of the regenerator used in this embodiment is shown in FIG. 1 , which includes, from bottom to top, a pre-lifting zone 1 , a coking zone 2 , a pre-combustion zone 3 and a main combustion zone 4 that are connected to each other in sequence. The lower part of the pre-lifting area 1 is provided with a catalyst inlet 9 to be produced, and the end of the pre-lifting area 1 is provided with a fuel oil inlet 10 . The lower sidewall of the pre-combustion zone 3 is provided with one or more oxygen-containing gas inlets 11 . The bottom of the main combustion zone is provided with a main air distributor 7, and the lower side wall is provided with a main air inlet 14;

Among them, the inner diameter of the pre-lifting zone 1 is 0.05 m and the length is 1 m; the inner diameter of the coking zone 2 is 0.08 m and the length is 1; the inner diameter of the pre-burning zone 3 is 0.3 m and the length is 2 m. The distance between the fuel oil inlet 10 and the outlet end of the pre-lift area is 5% of the height of the pre-lift area, and the distance between the position of the supplementary oxygen-containing gas inlet 11 and the bottom of the pre-combustion area is 20% of the height of the pre-combustion area .

The pre-lifted nitrogen enters the bottom of the pre-lift zone 1, mixes with the catalyst to be produced and moves upward, contacts with the fuel oil injected from the bottom of the pre-lift, mixes into the coke-producing zone 2, and undergoes a charring reaction. The distribution is uniform; the catalyst after charring enters the pre-combustion zone 3, contacts with the oxygen-depleted gas injected from the side wall of the pre-combustion zone and undergoes a pre-combustion reaction to burn off part of the coke; the catalyst with part of the coke enters the main combustion zone 4 , when contacted with air, a complete reaction occurs and heat is released.

At the same height that the main combustion zone is axially away from the bottom and 40% of the axial height of the main combustion zone, two temperature measuring points are set near the wall of the main combustion zone (the angle between the two relative to the axial direction is 180 degrees) , measure the temperature in the middle of different positions at the same height; set a temperature measurement point at the top of the main combustion area to measure the upper temperature of the main combustion area.

The main operating conditions of regeneration and the temperature distribution changes of the regenerator are shown in Table 1. It can be seen from Table 1 that the temperatures in the middle of the main combustion zone at different positions at the same radial height in the regenerator of this embodiment are 683°C and 687°C respectively, the radial temperature difference is 4°C, and the temperature in the upper part of the main combustion zone is 701°C , the temperature difference from the central temperature is small.

Comparative Example 1

The comparative example adopts a conventional catalytic cracking single-stage regenerator, which has the same structure and size as the main combustion zone of Example 1, and only has a fuel oil injection port in the lower catalyst dense bed zone.

The to-be-grown catalyst enters the lower part of the regenerator and contacts with the air distributed into the regenerator through the main air distributor to cause a coking reaction. The fuel oil is injected into the catalyst dense bed, and the fuel oil contacts the high-temperature air to cause a coking reaction and release heat.

Similarly, at the same height where the axial distance of the regenerator from the bottom is 40% of the axial height of the regenerator, two temperature measurement points are set near the regenerator wall (the angle between the two relative to the axial direction is 180 degrees), Measure the middle temperature at different positions at the same height; set a temperature measuring point on the top of the regenerator to measure the upper temperature of the regenerator.

The main operating conditions of the regenerator and the temperature distribution changes of the regenerator are shown in Table 1. It can be seen from Table 1 that the temperature in the middle of the regenerator at the same radial height in this comparative example is 668 °C and 725 °C, respectively, the radial temperature difference is 57 °C, and the temperature in the upper part of the regenerator is as high as 737 °C.

From the results of the above examples and comparative examples, it can be seen that using the regenerator and method of the present application for catalyst regeneration, the coke combustion environment in the regenerator is moderate and stable, and the radial and axial catalyst temperature gradients are small, which is helpful to maintain the catalyst. physical and chemical properties.

The regeneration results comparison of the embodiment of table 1 and the comparative example

Example Comparative ratio pre-lift area The temperature of the catalyst to be grown, °C 580 / coke area temperature, °C 570 / Amount of fuel oil, grams 216 211 pre-combustion zone temperature, °C 635 / Oxygen content in oxygen-depleted gas, wt% 5 / main combustion area The temperature in the middle of the main combustion zone is 1, ℃ 683 725 The temperature in the middle of the main combustion zone is 2, ℃ 687 668 The temperature of the upper part of the main combustion zone, °C 701 737

In the description of the present application, it should be noted that, unless otherwise expressly specified and limited, the terms "installed", "connected" and "connected" should be construed in a broad sense. For those of ordinary skill in the art, the specific meanings of the above terms in this application can be understood in specific situations.

The present application has been described above with reference to the preferred embodiments, but these embodiments are only exemplary and only serve for illustrative purposes. On this basis, various substitutions and improvements can be made to the present application, which all fall within the protection scope of the present application.

Claims (16)

1. A fluid catalytic cracking regenerator, comprising from bottom to top:

the pre-lifting area is provided with a pre-lifting area,

a coke-producing area, wherein the coke-producing area,

a precombustion zone, and

the main combustion area is provided with a main combustion area,

wherein the pre-lift zone outlet is in fluid communication with the green coke zone inlet, the green coke zone outlet is in fluid communication with the pre-combustion zone inlet, and the pre-combustion zone outlet is in fluid communication with the primary combustion zone inlet; the pre-combustion zone is communicated with the main combustion zone through an external catalyst circulating pipe;

one or more supplementary fuel oil inlets are arranged on the side wall of the pre-lifting area and/or the side wall of the coking area;

one or more supplementary oxygen-containing gas inlets are formed in the side wall of the pre-combustion zone;

one or more main oxygen-containing gas inlets are arranged on the side wall of the main combustion area.

2. The fcc regenerator of claim 1, wherein one or more of the supplemental fuel oil inlets are disposed on the sidewall of the pre-lift zone, the fuel oil inlets being each independently at a distance of 0% to 15% of the height of the pre-lift zone from the outlet end of the pre-lift zone.

3. The fcc regenerator of claim 2, wherein the fuel oil inlet is each independently located at a distance of 0% to 10% of the height of the pre-lift zone from the outlet end of the pre-lift zone.

4. The fcc regenerator of claim 1, wherein one or more of the supplemental fuel oil inlets are provided in the side wall of the coking zone, the fuel oil inlets being each independently at a distance from the bottom of the coking zone of from 0% to 15% of the height of the coking zone.

5. The fcc regenerator of claim 4, wherein the fuel oil inlet is each independently at a distance from the bottom of the coking zone of from 0% to 10% of the height of the coking zone.

6. The fcc regenerator of claim 1, wherein the supplemental oxygen-containing gas inlet is disposed in a lower portion of the pre-combustion zone, and the supplemental oxygen-containing gas inlet nozzles are each independently at a distance from the bottom of the pre-combustion zone of from 15% to 30% of the height of the pre-combustion zone.

7. The fluid catalytic cracking regenerator of claim 6, wherein the axial angle of the make-up oxygen-containing gas nozzle line is between 5 ° and 85 °.

8. The fluid catalytic cracking regenerator of claim 7, wherein the axial angle of the make-up oxygen-containing gas nozzle line is between 15 ° and 75 °.

9. The fcc regenerator of claim 1, wherein the catalyst circulation tubes are connected to the pre-combustion zone at a location that is each independently 0% to 10% of the height of the pre-combustion zone from the bottom of the pre-combustion zone.

10. The fcc regenerator of claim 1, wherein the primary combustion zone, the coking zone, and the pre-combustion zone are coaxially arranged.

11. The fcc regenerator of claim 10, wherein a catalyst delivery pipe is provided at the top of the pre-combustion zone outlet, and the pre-combustion zone outlet together with the catalyst delivery pipe is located inside the main combustion zone.

12. The fcc regenerator of claim 1, wherein the lower portion of the primary combustion zone is provided with a gas distributor configured to distribute primary regeneration oxygen-containing gas input through one or more primary oxygen-containing gas inlets provided in the sidewall of the primary combustion zone.

13. The fcc regenerator of claim 1, wherein the ratio of the internal diameters of the pre-lift zone and the coking zone is 0.2: 1 to 0.8: 1, the ratio of the height of the pre-lifting area to the height of the coking area is 0.5: 1 to 1.5: 1.

14. the fluid catalytic cracking regenerator of claim 1, wherein the pre-combustion zone comprises a partial combustion section and an outlet section, the partial combustion section having an inner diameter greater than an inner diameter of the outlet section.

15. The fcc regenerator of claim 14, wherein the ratio of the internal diameter of the partial combustion section to the internal diameter of the outlet section is 10: 1 to 2: 1, the ratio of the height of the partial combustion section to the height of the outlet section being 10: 1 to 2: 1.

16. a catalytic cracking system, characterized in that it comprises a fluid catalytic cracking regenerator according to any of claims 1-15.

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