WO2017118301A1

WO2017118301A1 - Method and apparatus for catalytic cracking reaction and regeneration

Info

Publication number: WO2017118301A1
Application number: PCT/CN2016/111713
Authority: WO
Inventors: 石宝珍
Original assignee: 石宝珍
Priority date: 2016-01-06
Filing date: 2016-12-23
Publication date: 2017-07-13
Also published as: CN105505441A; CN105505441B

Abstract

A method and an apparatus for a catalytic cracking reaction and regeneration. The method consists of two reaction parts, a raw material reaction and a catalyst regeneration. The regenerator is divided from top to bottom into a gas-solid separation zone, a catalyst regeneration reaction zone, and a charred gas preheating zone, wherein the charred gas is directly mixed and heat exchanged with a regenerant in the charred gas preheating zone to achieve preheating, such that the NOx generated during the charring is reduced, and at the same time the regenerant is also cooled by the charred gas to increase the catalyst-to-oil ratio of the reactor, to improve the product distribution of the reaction, while providing the reactor with an additional cryogenic catalyst. The cryogenic catalyst may be an agent to be regenerated or a cooled regenerant, thereby further optimizing the reactor conditions and controlling the product distribution.

Description

Catalytic cracking reaction regeneration method and device

Technical field

The invention relates to a gas solid phase catalytic reaction technology in the chemical field, in particular to a regeneration method and device for a petroleum hydrocarbon catalytic cracking reaction.

Background technique

The catalytic cracking reaction of petroleum hydrocarbons is a secondary processing process of crude oil, which consists of two reaction processes of raw material reaction and catalyst regeneration reaction. The raw material reaction process generally produces coke having a feed amount of 5.5% to 10.0%. These cokes adhere to the surface of the catalyst, block the pores of the catalyst, and must be circulated and charred to restore the activity of the catalyst. Both the raw material catalytic reaction and the catalyst regeneration reaction are important technical links.

The raw material reaction determines the intended product, but the catalyst regeneration process plays a major role in plant investment, operating energy consumption, and equipment maintenance costs.

The typical catalyst regeneration technology includes two-stage regeneration and counter-current two-stage regeneration technology. In particular, the countercurrent two-stage regeneration technology developed by UOP and Sinopec Beijing Design Institute reflects high efficiency. UOP Corporation and Ashland Corporation disclose a two-stage countercurrent regeneration reaction regeneration technology jointly developed by U.S. Patent No. 4,299,687. CN 97121795.5 discloses a two-stage regeneration technology for heavy oil fluid catalytic conversion.

Prior art catalyst regeneration processes focus only on coke combustion reactions, but nitrogen reacts with nitrogen (NOx) during coke and char gas contact reactions. With the improvement of environmental protection requirements, the traditional scheme uses the construction of flue gas denitration device to control NOx emissions, increase investment, energy consumption and operating costs, and affect economic benefits. A technique for directly reducing NOx formation in a combustion reaction process during charring is a better approach.

In the prior art, a char gas (generally air) from about 190 ° C in the catalyst regeneration (scorch) reaction directly participates in the catalyst coke scorch reaction. Increasing the temperature of the char gas burned by coke and lowering the temperature of the combustion zone, especially the local "high temperature" can effectively reduce NOx formation.

In the catalytic cracking process of the regenerator setting regenerator cooler, the low-temperature regenerant produced by the regenerator cooler in the prior art returns to the char reaction reaction zone, which lowers the temperature of the scorch reaction and affects the scorch reaction speed. The efficiency of the scorch reaction is reduced; it is often necessary to increase the circulation amount of the regenerant to make up for the regeneration zone temperature. However, the recycled regenerant has a low carbon content, which in turn reduces the coke content in the combustion reaction zone and also increases the energy consumption of the catalyst circulation.

In the process of catalytic cracking of petroleum hydrocarbons, the catalyst is the core problem, but the performance of the catalyst in the reactor and the performance of the unreacted procatalyst are different during the reaction. Taking the catalytic cracking reaction of hydrocarbon compounds as an example, the catalyst will be gradually degraded due to coke, alkaline components and metal contamination and passivation during the reaction. The performance of the catalyst in the reactor, especially in the tubular reactor, is different, and the catalytic efficiency is also different. In addition, the activity of the catalyst, the ratio of the reactant oil or the space velocity, the reaction temperature of the reaction raw materials and the catalyst, and the temperature difference are all important factors affecting the reaction results of the raw materials. The change and control of these conditions will change the reaction results.

The catalytic cracking of petroleum hydrocarbons is mainly for the component with carbon number greater than C3, and the small molecular products of C2 and below are mainly products of thermal cracking. Strengthening the catalytic cracking reaction and reducing the thermal cracking reaction are the goals that the catalytic cracking process has been pursuing. The selection and control of the reaction conditions during the catalytic cracking reaction is directly related to the reaction conversion rate and the selectivity of the reaction product. There are many techniques for optimizing the operation of the reaction system. The catalytic conversion reaction of petroleum hydrocarbon raw materials is taken as an example. The dry gas pre-lifting technology, the mixed temperature control technology that changes the injection point of the raw material and the injection medium, the rapid separation technology in the export zone, the quenching reaction technology, etc. Both have obvious influence on the reaction results and have been well applied in industry. Improvement and control of catalyst performance during the reaction are also critical.

Since the 1970s, petroleum hydrocarbon catalytic cracking reactions have replaced riser reactors with riser reactors. The catalytic cracking reaction of petroleum hydrocarbon feedstock is a gas-solid endothermic reaction. The reaction feedstock is generally a liquid feed. The liquid feedstock first needs endothermic gasification, and then the gaseous reactants enter the catalyst microporous passage for catalytic reaction. The heat of vaporization of the liquid feedstock is provided by the regenerated catalyst. Both liquid phase gasification and gas phase reaction processes exist in the liquid feedstock catalytic reaction using a tubular reactor. The gasification process is achieved by heating in contact with the catalyst. Since the gasification is not instantaneous and completed at the same time, there is more or less certain reaction in the gasification process. The essential advantage of a tubular reactor lies in the existence of a "gradient" in order to achieve the goal of increasing the "pushing force" (reactant concentration) of the reaction and improving the efficiency and selectivity of the reaction. This is one of the main reasons for replacing the fluidized bed with a riser. The petroleum hydrocarbon feedstock is complex in composition, the feedstock entering the reactor inlet has a molecular weight of approximately 300, and the reactor outlet product has a molecular weight of approximately 100 or less. Different reactant properties and reaction processes are exhibited at different positions in the riser reactor, and also Different reaction conditions. For example, above the atomization nozzle and at the beginning of the gas phase reaction zone, the main oil oil is subjected to gasification and is mainly a macromolecular cracking reaction of the feedstock oil. This process generally takes about 1.0-1.5 seconds of reaction time to raise the second half of the tube. The gas phase reaction zone mainly performs reactions such as re-reaction of small molecules such as diesel oil, gasoline, and liquefied gas, as well as isomerization and hydrogen transfer. Therefore, the entire gas phase reaction is often classified into a "cracking reaction zone, a reforming reaction zone" and the like. The temperature difference between the catalyst and the raw material in the liquid phase gasification reaction and the high temperature of the catalyst increase the thermal cracking reaction, increase the proportion of by-products below C2, and affect the economic benefits; the gas phase cracking reaction zone, the temperature of the reforming reaction zone, the ratio of the agent to the oil, and the catalyst The activity and the like all have a significant influence on the reaction results of the entire reaction zone.

Taking the catalytic conversion of petroleum hydrocarbon raw materials as an example, the research results at home and abroad have long confirmed that the high temperature of the regenerant leads to a relatively low reactant oil, and the contact temperature difference between the regenerant and the reaction raw material is large, which leads to high dry gas yield. Liquid collection The rate has a significant effect; as the reaction progresses, the activity of the catalyst decreases rapidly, and the efficiency of the reaction zone downstream of the riser decreases, which affects the reaction effect. Reducing the temperature of the regenerant, increasing the ratio of the agent to the oil and increasing the activity of the catalyst in the riser are the goals that the catalytic cracking unit has been pursuing for many years.

There are many technical measures in reducing the temperature difference between the regenerant and the feedstock in the liquid phase gasification contact zone of the reaction raw material. The most conceivable way to reduce the initial contact temperature with the feedstock oil is to "inject the low temperature catalyst from the external heat extractor into the riser pre-lift section". In U.S. Patent No. 5,800,697, UOP introduced a method for feeding a low temperature catalyst in an external heat extractor to a riser prelifting section. There are many patent applications in this respect, such as US6059958, US6558530B1, CN01119805.1, CN1664074A, CN101191067A, CN101191072A, and the like.

No. 5,800,697 discloses a catalytic conversion reaction-regeneration method in which a catalyst cooling zone is arranged beside the regenerator, and the thermal regenerant from the dense phase bed is exchanged from the outlet into the cooling zone to a suitable temperature, and then passed through the regeneration riser and the slide valve into the riser. The bottom of the reactor participates in the reaction so that the reactant oil ratio becomes an independent variable. CN101161786A discloses a method for converting petroleum hydrocarbons. The hot regenerated catalyst is cooled and returned to the bottom of the reactor through a cooler to participate in the contact of the feedstock oil and undergo a cracking reaction. After the catalyst is stripped, it is sent to the regenerator for charring regeneration. Recycle or partially enter the mixer at the bottom of the reactor.

Another way to reduce the initial temperature difference between the feedstock and regenerant is to increase the temperature of the feedstock. CN101144028A discloses a hydrocarbon oil cracking process in which a hydrocarbon oil and a regenerated catalyst are heated in a heat exchanger, and then the heat-exchanged hydrocarbon oil is brought into contact with the regenerated catalyst after heat exchange in a reactor.

In addition, the factors affecting the reaction of the catalyst include not only the catalyst temperature in the pre-elevation section before the reaction, the contact temperature difference between the liquid phase (feedstock oil) gasification zone and the ratio of the agent to the oil, but also the catalyst activity and the ratio of the agent to the oil in the gas phase cracking reaction zone after the oil gasification of the raw material. It also has an important influence on the reaction process.

The control and improvement of the catalyst action in the reaction process at various positions in the reactor, in addition to the liquid phase gasification zone, should also include the improvement of the catalyst in the gas phase reaction zone after the oil gasification of the raw material, and the control of the state of the supplied catalyst.

In summary, the conditions and means for the catalyst to enter the reactor are important for improving the reaction effect of the raw materials. It is more meaningful to optimize the regeneration and reaction to form a matching and complete reaction regeneration system. The catalyst regeneration reaction can improve the smoke by using high temperature scorch gas. Gas emission indicator.

Summary of the invention

In order to solve the above problems, an object of the present invention is to provide a catalytic cracking reaction regeneration method and apparatus, which preheats a charred gas by a regeneration process to achieve high temperature gas scorching and reduce NOx emissions.

In order to achieve the above object, the present invention provides a catalytic cracking reaction regeneration method comprising two reaction parts of a raw material reaction and a catalyst regeneration, and the equipment involved includes a catalyst regenerator (referred to as a regenerator) and a tubular reactor (referred to as a reaction). And reactor settler (referred to as settler) and so on. Wherein, the inside and outside of the shell of the regenerator is divided into a gas-solid separation zone, a catalyst regeneration reaction zone (also referred to as a catalyst regeneration zone, a regeneration zone), and a scorch gas preheating zone;

a dense phase fluidized bed catalyst storage zone is provided in the cone section below the gas-solid separation zone for providing a regenerant catalyst for the regenerant transport pipe and the external heat extractor (if any); the dense phase fluidized bed catalyst storage zone It is disposed inside the catalyst regeneration reaction zone or independently outside the catalyst regeneration reaction zone; a regenerant transport pipe is arranged between the dense phase fluidized bed catalyst storage zone and the scorch gas preheating zone; in the scorch gas preheating zone and the catalyst An orifice plate is disposed between the regeneration reaction zones; when a catalyst cooler (external heat collector) is required for the regenerator, and a reaction regenerant desuperheater is provided for the reactor, the catalyst inlet of the regenerated catalyst cooler and the reaction regenerant desuperheater is also Provided in the dense phase fluidized bed catalyst storage area;

The reactor main body is a riser reaction section, and the raw material oil inlet port is followed by a raw material oil-gas zone and a catalytic cracking reaction zone, and a settler is arranged downstream of the catalytic cracking reaction zone, and a reaction product gas-solid separator is disposed therein, and the separated catalyst is disposed. Gravity down into the stripping section; the stripped catalyst (abbreviated as a living agent) enters the regenerator catalyst regeneration reaction zone, and is in contact with the scorched gas (usually using air) from the scorched gas preheating zone Charring reaction

The regeneration method includes:

1. The reaction raw materials are introduced into the reactor at different parts of the reactor, contacted with the catalyst and heated by the catalyst, and then reacted; the reaction product and the catalyst are discharged from the outlet of the reactor to separate the catalyst and the product gas, and the product gas is passed through. The settler oil and gas outlet flows out;

2. After completion of the reaction of the raw material, the catalyst enters the stripping section of the settler for stripping, and the stripped catalyst enters the bottom of the regeneration reaction zone in the middle of the regenerator, and is regenerated by the preheated charred gas from below ( Also referred to as charring), at the same time, the catalyst is transported upward together with the regeneration reaction gas and the flue gas generated by the regeneration reaction, and the gas and the catalyst are separated in the gas-solid separation zone of the regenerator, and the separated catalyst first enters the dense phase in the regenerator. The fluidized bed catalyst storage zone is sent from the dense phase fluidized bed catalyst storage zone (preferably through the regenerant transport pipe) to the charred gas preheating zone at the bottom of the regenerator, in the charred gas preheating zone, the catalyst and the charred gas Direct mixing causes the char gas to be heated while the catalyst itself is cooled; the cooled regenerated catalyst (referred to as regenerant) enters the reactor below the inlet of the reaction raw material, and is contacted with the reaction raw material under the action of the pre-lifting medium;

3. The first part of the charred gas (also called the main wind) enters the scavenging gas preheating zone in the scorch gas preheating zone at the bottom of the regenerator (preferably through the gas distributor), and directly forms a fluidized state contact with the regenerant. After the heat is heated, the gas flows upward and flows into the catalyst regeneration zone; after completion of the charging, the gas carries part of the catalyst to perform full gas-solid separation in the gas-solid separation zone of the regenerator, and the gas flows out of the regenerator from the flue gas outlet, and the separated catalyst relies on gravity sedimentation. Enter dense phase fluidization The bed catalyst storage area is then passed to the reactor to participate in the reaction.

In the above regeneration method, preferably, in 1, the reaction product and the catalyst are discharged together from the outlet of the reactor, and then enter the first-stage gas-solid separator and the second-stage gas-solid separator in the settler to realize the catalyst and the product. Separation of gas.

In the above regeneration method, preferably, in 2, the stripped spent agent passes through the inclined tube to enter the bottom of the regeneration reaction zone in the middle of the regenerator. The cooled regenerant enters the reactor from the charred gas preheater through the regeneration inclined tube under the reaction feed inlet, and is contacted with the reaction raw material under the action of the pre-lifting medium.

In the above regeneration method, preferably, the regenerator is provided with a regenerator catalyst cooler (also referred to as an external heat extractor), and the reactor is provided with a reaction catalyst desuperheater (or a reaction regenerant desuperheater), which can be separately set. , can also be set at the same time. The regenerator catalyst cooler and the catalyst inlet of the reaction catalyst desuperheater are disposed in a regenerator dense phase fluidized bed storage zone.

In the above regeneration method, preferably, in the third portion, the first portion of the scorched gas enters the scorched gas preheating zone through the first gas distributor at the scorch gas preheating zone at the bottom of the regenerator.

In the above regeneration method, preferably, in 3, a scorch gas inlet pipe and a second gas distributor (distribution pipe) are disposed above or below the orifice plate between the scorch gas preheating zone and the catalyst regeneration reaction zone, Introducing a second portion of charring gas (also called main wind) into the regenerator through the second distributor;

The second part of the char gas enters the regenerator below the orifice level in the preheating zone of the regenerated catalyst, below the orifice between the charred gas preheating zone and the regeneration zone, and is mixed with the high temperature gas from the charred gas preheater. And then enter the regeneration reaction zone through the orifice plate to participate in the charring reaction.

In the above regeneration method, preferably, when the catalyst is sent from the dense phase fluidized bed catalyst storage zone of the regenerator to the scorch gas preheating zone, the preheating zone of the charred gas is controlled by a valve provided on the regenerant conveying pipe. The amount or level of catalyst.

In the above regeneration method, preferably, the preheating temperature of the scorched gas is adjusted by the change in the amount of the catalyst or the level of the catalyst in the preheating zone of the charred gas, and the amount of the scorch gas entering the preheating zone of the scorch gas. And the cooling temperature of the regenerant itself.

In the above regeneration method, preferably, the catalyst regeneration reaction of the regenerator is divided into a first regeneration zone and a second regeneration zone; the first regeneration zone is at a lower portion, the second regeneration zone is at an upper portion of the first regeneration zone; the first regeneration zone and Preferably, a flow orifice plate (distributor) is disposed in each section of the second regeneration zone; the catalyst and gas (preferably via the orifice plate) of the first regeneration zone are sent to the second regeneration zone to continue scorching; the upper boundary of the second regeneration zone (catalyst) The feed level extends upward to the tapered section of the regenerative regeneration reaction zone and the gas-solid separation zone; in the cone section, the gas flow rate is gradually reduced, the catalyst The density increases to become a dense phase fluidized bed (i.e., a dense phase fluidized bed catalyst storage zone) which simultaneously becomes a regenerant storage zone. a flue gas gas-solid separation zone is disposed above the second regeneration zone; a regenerant transport pipe is disposed between the dense phase fluidized bed zone and the scorch gas preheating zone of the second regeneration zone, and the regenerant is burned through the regenerant transport pipe The regenerant after the coke is sent to the preheating zone of the charred gas; the spent agent enters the first regeneration zone; part of the charred gas (generally referred to as the main wind) enters the gas preheating zone through the gas distribution pipe, and is in the preheating zone The regenerant is directly contacted, heated by the regenerant, and then enters the first regeneration zone through the orifice plate; the regenerant is cooled by itself while heating the charred gas, and the regenerant cooled by the charred gas passes through the catalyst conduit from the preheating zone ( Generally referred to as the regeneration riser) enters the bottom of the reactor (generally referred to as the pre-lift section).

In the above regeneration method, preferably, an inner tub connected to the first regeneration zone (lower regeneration zone) is disposed in a cone section below the gas-solid separation zone of the regenerator, and the inner bucket divides the second regeneration into two inner and outer zones, The outer zone becomes a catalyst recovery storage zone (also referred to as a regenerant recovery and storage zone); the flue gas and catalyst of the first regeneration zone enters the inner barrel to continue the scorch reaction; the inner barrel is designed as a cylinder or cross section of equal cross section a charred reaction zone in which the cross-sectional area is gradually increased and the gas flow rate is gradually decreased; a charred gas delivery pipe and a distributor (also referred to as a third distributor) may be disposed outside the inner tub to supplement the scorched gas to the catalyst storage region, ie The third part is charred. A flow orifice plate (also referred to as a second orifice plate) may be disposed between the first regeneration zone and the second regeneration zone, and the catalyst and gas of the first regeneration zone are simultaneously transported to the second regeneration zone through the orifice plate to continue scorching.

In the above regeneration method, preferably, the casing of the second regeneration zone is disposed in the regenerator cone section and the gas-solid separation zone casing, the first regeneration zone and the second regeneration zone are directly connected, and the outlet area of the second regeneration zone is gradually set. a reduced cone section and a conveying pipe, the flue gas gas-solid initial separator is arranged at the outlet of the conveying pipe; the casing of the second regeneration zone separates the second regeneration zone from the regenerator gas-solid separation zone and the catalyst storage zone into two independent Space, the catalyst and gas in the regeneration reaction zone are directly separated from the outlet of the regeneration reaction zone, and the gas is separated in the gas-solid separation zone of the regenerator through two-stage rotation between the regeneration zone and the regenerator casing. The catalyst exits the regenerator and the catalyst enters the catalyst storage zone between the regeneration reaction zone and the regenerator housing.

In the above regeneration method, preferably, a catalyst circulation pipe is disposed between the catalyst storage zone (also referred to as a regenerant storage zone, that is, a dense phase fluidized bed catalyst storage zone) and the first regeneration zone, and the first regeneration zone catalyst is controlled ( Also referred to as the combustion reaction temperature of the first regeneration zone.

In the above regeneration method, preferably, when the catalyst regeneration reaction requires heat extraction, the catalyst is introduced into the catalyst cooler from the dense phase fluidized bed catalyst storage zone (ie, the regenerant storage zone), and the regenerated regenerant after cooling (preferably from the catalyst) Tube) directly into the charred gas preheating zone.

In the above regeneration method, preferably, the regeneration method further comprises adding a scorch gas, that is, a third portion of the scorched gas, to the second regeneration zone, where the third distributor may be disposed, and the third distributor is regenerated to the second Area supplement burnt gas body. More preferably, the third portion of the char gas enters the regenerator below the orifice plate of the first regeneration zone and the second regeneration zone, and the third portion of the char gas is directly replenished to the second regeneration zone or to the dense phase flow. The bed catalyst storage area is supplemented. When the inner tub is not disposed, the second regeneration zone and the first regeneration zone are directly connected in series, and the third portion of the scorched gas directly enters the second regeneration zone; when the inner tub is set, the second regeneration zone is disposed outside the first regeneration zone, Three portions of charred gas enter the dense phase fluidized bed catalyst storage zone outside the inner tub.

In the above regeneration method, preferably, a reactor reflux pipe is disposed between the reactor stripping section and the reactor bottom (pre-lift section) or the gasification cracking reaction section to control the temperature inside the reactor and the agent oil. Ratio and catalyst activity.

In the above regeneration method, preferably, the reaction regenerant is cooled between the regenerator dense fluidized bed catalyst storage zone (second regeneration zone) and the reactor bottom (pre-lifting section) or the gasification cracking reaction section. And the reaction regenerating agent conveying pipe after cooling, the regenerant which has been cooled by the regenerant desuperheater enters the reactor, and controls the temperature inside the reactor, the ratio of the agent to the oil, and the activity of the catalyst.

According to a specific embodiment of the present invention, in the regeneration method of the present invention, a first orifice plate is disposed under the inlet of the regenerant in the regeneration zone of the regenerator, and the regenerator is divided into a regeneration zone and a gas preheating zone; The orifice plate may be a porous separator, or may be other forms of distribution plates, one of which functions to allow gas (portable part of the catalyst) from the preheating zone below the distribution plate to uniformly enter the orifice plate through the first distribution plate. a first regeneration zone; the other function of the first orifice plate is to separate the regenerant of the gas preheating zone from the catalyst of the regeneration zone to prevent the regenerant from being carried by the gas stream into the regeneration zone; it is understood that, in the present invention, The position of the first distribution plate can be appropriately adjusted or the catalyst level of the gas preheating zone can be controlled to control the amount of catalyst entering the first regeneration zone from the preheating zone. In addition, in the method of the present invention, a portion of the charred gas may be introduced into the first regeneration zone through the second gas distributor as needed, and the gas distributor may be above the first orifice plate or below the first orifice plate; Preferably, the distributor is disposed below the first orifice plate.

According to a specific embodiment of the present invention, in the regeneration method of the present invention, in the regeneration zone of the regenerator, a second orifice plate is further disposed above the inlet of the green agent; the second orifice plate may be a porous separator. Or other forms of distribution plates; the main function of the second orifice plate is to uniformly pass the gas and catalyst in the first regeneration zone into the second regeneration zone, so that the catalyst in the second regeneration zone is well fluidized and mixed to improve the scorching effect; In addition, in the method of the present invention, a portion of the charred gas may be introduced into the second regeneration zone through the third gas distributor as needed, and the gas distributor may be above the second orifice plate or below the second orifice plate; Preferably, the distributor is disposed below the second orifice plate.

In the above regeneration method, preferably, the amount of the first portion of the scorched gas directly introduced into the scavenging gas preheating zone from the bottom is 35-85%, based on 100% of the total amount of scorch gas introduced into the regenerator. Left and right, the flow rate of the gas empty tower in the preheating zone of the charred gas is 0.3m/s-1.0m/s; the amount of the scorched gas in the second part is about 30-60%, and the amount of the third part of the scorched gas is 0. -10% or so. Each part of the gas can be introduced into the regenerator through a gas distributor, the specific gas The volume distributor can be selected from the prior art in the prior art, and the present invention will not be described again.

The invention also provides a catalytic cracking reaction regeneration device comprising a reactor, a regenerator and a settler arranged side by side, wherein:

The regenerator is used for charring regeneration of the catalyst to be produced from the reactor, the regenerator is installed vertically, and the inside of the casing is divided into a bottom charred gas preheating zone, a catalyst regeneration zone and a regenerator gas-solid separation zone;

a charred gas tube is arranged at the bottom of the preheating zone of the charred gas for introducing the first portion of the charred gas;

The catalyst regeneration is divided into a lower first regeneration zone and an upper second regeneration zone;

A second regeneration zone barrel connected to the first regeneration zone is disposed in the cone section below the gas-solid separation zone of the regenerator, and the second regeneration is divided into two inner and outer zones, and the outer zone is a dense phase fluidized bed catalyst storage zone, first The flue gas and catalyst in the regeneration zone enter the interior of the barrel in the second regeneration zone to continue the charring reaction;

The upper boundary of the second regeneration zone extends upward to a tapered section of the regenerative regeneration reaction zone and the regenerator gas-solid separation zone, wherein a gas-solid separator is disposed in the middle of the cone section (preferably two stages, That is, the first-stage gas-solid separator and the second-stage gas-solid separator), and the top is provided with a burnt flue gas outlet for the flue gas F to leave;

An inclined tube is arranged between the stripping section of the settler and the first regeneration zone, and a regenerative inclined pipe is arranged between the preheating zone of the scorch gas and the bottom of the reactor;

a charred gas inlet pipe is provided in the charred gas preheating zone and the first regeneration zone for introducing a second portion of the scorched gas;

a regenerant transport tube is disposed between the dense phase fluidized bed catalyst storage area and the charred gas preheating zone, and a regenerant circulation pipe is disposed between the dense phase fluidized bed catalyst storage area and the bottom of the first regeneration zone;

A gas pipe is provided at the bottom of the second regeneration zone for introducing a third portion of the char gas.

In the above regenerating apparatus, preferably, a second regeneration zone casing is disposed in the casing of the regenerator and the casing of the regenerator gas-solid separation zone, the first regeneration zone and the second regeneration zone are directly connected, and the second regeneration zone is A cone-shaped section whose outlet setting area is gradually reduced and an outlet pipe of the regeneration zone, and a gas-solid initial separator of the flue gas at the outlet of the outlet pipe of the regeneration zone.

According to the technical scheme of the present invention, the scorched gas reacts with the coke on the catalyst after the preheater itself is preheated to form a flue gas having a low NOx content; the scorching gas simultaneously cools the regenerant to provide a low temperature regenerant for the reactor. A low-temperature regenerant cycle is formed between the reactor and the regenerator, which can reduce the thermal cracking reaction of the thermal cracking, especially the gasification and cracking reaction zone, can adjust the heat balance relationship between the gasification and the reaction, and conveniently and flexibly realize the catalyst in each reaction zone. Multiple controls and reduced energy consumption.

In general, the catalytic cracking regeneration method of the present invention is applied to a catalytic cracking process of petroleum hydrocarbon raw materials, and the regeneration process itself preheats the charred gas to achieve high temperature gas scorching and reduce NOx emissions; a warm regenerant, which is provided with an independent regenerative catalyst cooling device without providing a low temperature regenerant for the reactor; the regenerant after cooling or the cooled regenerant is replenished into the reactor in the cracking reaction zone after the reaction raw material is vaporized, as a reactor The double catalyst cycle is formed, and different catalyst conditions can be provided according to the needs of the reaction conditions at different positions, thereby realizing convenient and flexible multiple control of the catalyst in each reaction zone.

DRAWINGS

Figure 1 is a schematic representation of a reaction-regeneration portion of a catalytic cracking reaction process in accordance with an embodiment of the present invention.

Fig. 2 is a schematic view showing a catalytic cracking reaction-regeneration portion of another mode of the present invention.

Fig. 3 is a schematic view showing a catalytic cracking reaction-regeneration portion of another mode of the present invention.

Fig. 4 is a schematic view showing a catalytic cracking reaction-regeneration portion of another embodiment of the present invention.

Fig. 5 is a schematic view showing a catalytic cracking reaction-regeneration portion of another embodiment of the present invention.

Figure 6 is a schematic representation of the reaction-regeneration portion of the present invention containing heat taken by the regenerator.

Figure 7 is a schematic view showing the structure of an embodiment of the regeneration section distribution plate of the present invention.

Figure 8 is a schematic view showing the structure of another embodiment of the regeneration section distribution plate of the present invention.

Description of the reference numerals:

1 reactor; 2 charred gas preheating zone; 3 first regeneration zone; 4 second regeneration zone; 5 regenerator gas-solid separation zone; 6 settler stripping section; 7 settler dilute phase zone; Cooler; 9 reaction regenerant desuperheater; 11 regeneration inclined pipe; 12 regeneration slide valve; 13 reactor bottom catalyst section; 14, 14B reaction raw material, 14C reaction raw material or quenching raw material; 15 reaction raw material reaction zone; ; 17 waiting agent return port; 18 waiting agent return pipe valve; 19 waiting agent return pipe; 20 scorched gas preheating zone housing; 22 charred gas preheating zone gas distributor; 23 charred gas pipe; 24 low temperature regenerant outlet; 25 gas preheating zone catalyst level; 26 regenerant distributor; 27 regenerant delivery pipe valve; 28 regenerant delivery pipe; 29 regenerant delivery pipe; 30 first regeneration zone housing; First orifice plate; 31B flow hole; 31C hole cap; 32 combustion gas distributor, 33 charred gas pipe; 34 standby inclined pipe valve; 35 standby inclined pipe; 36 standby catalyst distributor; 37 regenerant circulation pipe Valve; 38 regenerant circulation pipe; 39 regenerant circulation pipe; 40 regenerator cone section housing; 41 Orifice plate; 41B flow hole; 41C hole cap; 41D regenerant storage area grid; 42 gas distributor; 43 gas tube; 44A, 44B, 44C, 44D regenerant outlet; 45 regenerant storage area catalyst level; Second regeneration zone shell; 46B second regeneration zone barrel; 46C cone section; 47 regeneration zone outlet delivery pipe; 48 gas-solid initial separator; 49 regenerator dense-phase fluidized bed catalyst storage zone; 50 regenerator gas-solid separation Zone shell; 51 regenerator primary gas-solid separator; 52 regenerator secondary gas-solid separator; 53 gas collection chamber; 54 charred flue gas outlet; 60 settler stripping zone shell; 61 stripping internals ; 62 stripping steam distributor; 63 stripping steam pipe; 64 waiting agent outlet; 65 waiting inclined pipe; 67 waiting agent return outlet; 70 settler casing; 71 settler first gas solid Separator; 72 settler secondary gas-solid separator; 73 gas collection chamber; 74 product gas outlet; 81 regenerator catalyst cooler catalyst inlet; 82 regenerator catalyst cooler catalyst outlet; 83 regenerator catalyst cooler outlet valve; 91 reaction regenerant desuperheater catalyst inlet; 92 reaction regenerant desuperheater outlet; 93 reaction regenerant desuperheater outlet valve; 94 reaction low temperature regenerant inlet; A compressed scorch gas; C catalyst; F flue gas; S steam; Pre-lifting medium; O-reaction feedstock oil; H scorch gas preheating zone catalyst level height.

detailed description

The technical solutions of the present invention are described in detail below with reference to the accompanying drawings and embodiments. The scope of protection of the present invention includes but is not limited thereto. The device structure not specifically mentioned in the present invention can adopt the conventional techniques in the art.

Referring to Figures 1 - 6, the apparatus for carrying out the reaction regeneration method of the present invention comprises a reactor and a regenerator arranged side by side, wherein:

The regenerator is used for charring regeneration of the spent agent from the reactor 1, the regenerator is installed vertically, and the inside of the casing is divided into a bottom charred (regenerated) gas preheating zone 2, a catalyst regeneration zone and a regenerator gas-solid separation. Area (smoke gas-solid separation zone) 5;

The charred gas preheating zone 2 is disposed inside the charred gas preheating zone casing 20, and is provided with a charred gas pipe 23 at the bottom thereof, and the compressed scorch gas (the first partially scorched gas) A passes through the charred gas pipe 23 through the gas. The distributor 22 enters the charred gas preheating zone 2 to contact heat exchange with the catalyst C; the catalyst material preheating zone 2 has a catalyst material level height H of 2.0-6.0 m, preferably H is 2.5 m-3.5 m;

The catalyst regeneration is divided into a lower first regeneration zone 3 and an upper second regeneration zone 4; the first regeneration zone 3 is disposed in the first regeneration zone casing 30, and the second regeneration zone 4 is disposed in the second regeneration zone casing 46. a second orifice plate 41 may be disposed between the first regeneration zone 3 and the second regeneration zone 4, and the catalyst and gas of the first regeneration zone 3 are simultaneously transported to the second regeneration zone 4 through the second orifice plate 41 to continue burning. The height of the first regeneration zone 3 is 8.0m-15.0m, designed according to the apparent flow rate of the gas of 1.4m/s-2.5m/s;

The regenerator gas-solid separation zone 5 is disposed in the regenerator gas-solid separation zone shell 50, and is designed according to the apparent flow velocity of the gas of less than 0.8 m/s, and the cone section below (the interior of the regenerator cone section shell 40) is disposed a second regeneration zone bucket 46B connected to the first regeneration zone 3, the second regeneration zone bucket 46B dividing the second regeneration zone 4 into two inner and outer zones, the outer zone being a dense phase fluidized bed catalyst storage zone 49; the first regeneration zone The flue gas and catalyst of 3 enter the interior of the barrel 46B in the second regeneration zone to continue the scorch reaction;

The upper boundary of the second regeneration zone 4 extends upwardly to a tapered section of the regenerator regeneration reaction zone and the regenerator gas-solid separation zone 5 (inside the regenerator cone section shell 40), in which the cone section Gas flow rate gradually decreases, reminder The density of the agent is increased to form a dense phase fluidized bed catalyst storage zone 49 (with a regenerant storage zone grid 41D disposed therein, and a regenerant storage zone catalyst level 45 is controlled by a regenerative spool 12 on the regeneration ramp 11 Increasing the regenerant flowing out of the regenerative inclined tube 11, reducing the amount of catalyst in the regenerator, increasing the amount of catalyst in the reaction part, the level in the regenerator will naturally decrease), and the first stage is equipped with a regenerator level gas-solid separation And the regenerator secondary gas-solid separator 52 may be gas-solid separated by a cyclone, and a gas collecting chamber 53 and a scorched flue gas outlet 54 are provided at the top for the flue gas F to leave;

The stripped spent agent passes through the waiting tube 35 through the standby catalyst distributor 36 to enter the bottom of the first regeneration zone 3 in the middle of the regenerator, and then enters and exchanges heat with the charred gas, and the green agent is used in the first orifice plate 31. The upper 1.0m-4.0m enters the first regeneration zone 3; the inclined pipe 35 is provided with the inclined pipe valve 34; the cooled catalyst (low temperature regenerant) passes from the charred gas preheating zone 2 through the low temperature regenerant outlet 24 passes through the regeneration inclined tube 11 to enter the bottom catalyst section 13 of the reactor at the bottom of the reactor 1 under the reaction raw material inlet, and is in contact with the reaction raw material 14 under the action of the pre-lifting medium G; the regeneration inclined valve 11 is provided with a regenerative slide valve 12, In the control gas preheating zone catalyst level 25;

A first orifice plate 31 is disposed between the charred gas preheating zone 2 and the first regeneration zone 3, and a charred gas inlet pipe 33 and a char gas distributor (second gas) are disposed below the first orifice plate 31. a distributor 32, through which the compressed char gas (second partial scorched gas) A is introduced into the regenerator;

The high-temperature regenerated catalyst (referred to as high-temperature regenerant) from the regenerator dense-phase fluidized-bed catalyst storage zone 49 is taken out through the

regenerant outlets

44A, 44B, and a part passes through the

regenerant delivery tubes

28, 29 through the regenerant distributor 26 into the burning. The coke gas preheating zone 2, a part of which passes through the

regenerant circulation pipes

38, 39 enters the bottom of the first regeneration zone 3, and the circulation amount of the regenerant in the regenerant circulation pipe 38 is the amount of catalyst entering the reactor 1 through the regeneration inclined pipe 11. 0.5-1.5 times; the

regenerant delivery pipe

28, 29 is provided with a regenerant delivery pipe valve 27 to control the storage or level of the catalyst in the scorched gas preheating zone 2, and the catalyst in the preheating zone 2 through the charred gas The change of the storage amount or the material level, and the amount of the scorched gas which is changed into the preheating zone 2 of the charred gas, adjust the preheating temperature of the scorched gas and the cooling temperature of the catalyst itself; the

regenerant circulation pipes

38, 39 are provided. Regenerant delivery tube valve 37;

The compressed char gas (third portion scorch gas) A may be introduced into the second regeneration zone 4 through the gas pipe 43 through the third gas distributor 42 as needed, and the third gas distributor 42 is located below the second orifice plate 41;

According to a preferred embodiment of the present invention (as shown in FIG. 3, as shown in FIG. 4), a second regeneration zone 46 housing, a first regeneration zone 3 and a first regeneration zone are provided in the regenerator cone section and the regenerator gas-solid separation zone housing 50. The second regeneration zone 4 is directly connected, the outlet of the second regeneration zone 4 is provided with a taper section 46C whose area is gradually reduced, and the regeneration zone outlet conveyance pipe 47, and the gas-solid primary separator 48 of the regeneration zone outlet delivery pipe 47 is provided with the flue gas F. ;

The specific structure of the reactor 1 is shown in FIG. 5 and FIG. 6 , wherein the main body of the reactor 1 is a riser reaction section, and the original The feed oil inlet port is followed by a raw material oil-gas zone, a catalytic cracking reaction zone, and a settler downstream of the catalytic cracking reaction zone;

The reaction feedstock oil O enters the reactor 1 at different parts of the reactor 1, and the reaction raw material 14 is contacted with the catalyst and heated and vaporized by the catalyst, and enters the reaction raw material reaction zone 15 for reaction. The reaction product and the catalyst are discharged from the reactor outlet immediately. The first stage gas-solid separator 71 and the second-stage gas-solid separator 72 entering the settler dilute phase zone 7 realize separation of the catalyst and the product gas, and the product gas enters the gas collection chamber 73 at the top of the settler, and passes through the product gas. The outlet 74 flows out, and the separated catalyst enters the settler stripping section 6 by gravity; the catalytic reaction raw material often has multiple sources, and the properties and temperatures are different, and the reaction raw material 14B (generally may be refining oil, hydrogenated wax oil, etc.) ), the reaction raw material or quenching raw material 14C (the purpose of quenching is to terminate the reaction as soon as possible, and the quenching raw material generally uses water, gasoline, etc., which does not need to be re-reacted but can lower the temperature) can enter the reactor at a higher position;

In the settler stripping section 6, the catalyst is stripped by the steam entering by the stripping steam pipe 63; the settler stripping section 6 is disposed in the settler stripping zone casing 60, and the stripping inner part 61 is provided inside. , stripping steam distributor 62;

The stripped spent agent exits through the outlet of the green agent 64, passes through the inclined tube 65, and the inclined tube 35 to enter the bottom of the first regeneration zone 3 in the middle of the regenerator;

For light raw materials, when the reaction regeneration system does not need to take heat, the spent agent leaves through the 67 outlet of the raw agent reflux outlet 67, passes through the standby agent return pipe 19 (on which the waiter return pipe valve 18 is provided) and the spent agent The return port 17 returns to the catalyst mixing zone 16 of the reactor 1 at 2.0 m-10.0 m above the feedstock inlet, or to the bottom catalyst section 13 (not shown) at 2.0 m-7.0 m below the feedstock inlet. The return amount of the living agent is 0.2-1.0 times the amount of the catalyst entering the reactor 1 through the regeneration inclined tube 11;

For the reaction raw materials with excess heat (heat required), a reaction regenerant desuperheater (or reaction catalyst desuperheater) 9 (shown in Figure 6) may be provided, and the heat load is determined by the following method: regeneration after cooling The temperature of the catalyst is 500 ° C - 580 ° C; the flow rate of the catalyst is determined by 0.2-1.0 times the amount of the catalyst entering the reactor 1 through the regeneration inclined tube 11; the catalyst passes through the dense phase fluidized bed catalyst storage area 49 (providing a regenerant outlet 44D) The connected reaction regenerant desuperheater inlet 91 enters, and the regenerated regenerant exits through the reaction regenerant desuperheater outlet 92, and returns to the reactor 1 through the reaction low-temperature regenerant inlet 94 at 2.0 m-10.0 m above the feedstock inlet. The catalyst mixing zone 16 is returned to the bottom catalyst section 13 (not shown) at 2.0 m-7.0 m below the feedstock inlet; the reaction regenerant desuperheater outlet 92 is provided with a reaction regenerant desuperheater outlet valve 93. ;

When the regenerator catalyst cooler 8 is provided (as shown in Figure 6), the catalyst enters through a regenerator catalyst cooler catalyst inlet 81 connected to a dense phase fluidized bed catalyst storage zone 49 (provided with a regenerant outlet 44C). The cooled regenerant directly enters the charred gas preheating zone 2 through the regenerator catalyst cooler catalyst outlet 82, Then enter the catalyst regeneration zone as in the conventional technology; a regenerator catalyst cooler outlet valve 83 is disposed outside the regenerator catalyst cooler catalyst outlet 82; the regenerator cooler can be designed by a general technician;

As shown in FIGS. 7 and 8, an orifice plate, for example, a first orifice plate 31 and a second orifice plate 41 are provided in each section, and the orifice plate is of a porous type, and the flow holes 31B and 41B are rising holes of the flue gas F and the catalyst C. The total area is 12m/s-40m/s, the aperture is 50mm-200mm, the preheating zone 2 is 3.0m-7.0m, and the apparent flow rate is less than 1.2m/s. The flow holes 31B, 41B Hole caps (distribution plate escutcheons) 31C, 41C may be provided thereon.

The general technician of the settler and settler stripping zone can complete the design; according to the above parameters, the technician can complete the application design of the method of the present invention; the present invention will not be described again.

The reaction regeneration method of the invention provides the regenerator of the reactor with different conditions; the reaction condition is optimized; the NOx content in the flue gas can be reduced due to the high temperature gas reaction; the scorch is realized in the regenerator itself by the improvement of the regenerator structure Gas preheating simplifies plant design by reducing investment and reducing energy consumption while optimizing raw material reactions and improving product distribution.

Example

The apparatus for the reaction zone catalyst control and the regenerant heat removal method used in this embodiment is shown in Fig. 3.

A petroleum hydrocarbon catalytic cracking unit with an annual output of 150×10 ⁴ t/a, the reaction regeneration is arranged side by side, the scorch gas preheating zone 2 is in the form of a fluidized bed, and the first regeneration zone 3 is in the form of a circulating fluidized bed, the second regeneration The zone 4 is disposed in the regenerator cone section between the first regeneration zone 3 and the regenerator gas-solid separation zone 5, in the form of a fluidized bed; the charred gas preheating zone 2, the first regeneration zone 3, and the second regeneration zone 4 is provided between the first orifice plate 31 and the second orifice plate 41 respectively; the reactor 1 is in the form of a riser; the reaction regenerant desuperheater 9 is arranged, the reaction regenerant desuperheater 9 generates medium pressure steam, and the reaction regenerator desuperheater 9 The self-contained water vapor separator type is adopted, and the water vapor separator is directly connected to the reaction regenerant desuperheater 9 with the same diameter as the regenerant desuperheater; the catalyst after the reaction regenerator desuperheater 9 is cooled enters the reactor 1 above the feedstock oil, specifically The entry position is shown in the following table; the amount of gas participating in the preheating of the scorched gas is 52% of the total amount, and the amount of scorched gas fed to the first regeneration zone 3 is 48% of the total amount, and the gas distributor and the delivery pipe are provided at Below the second orifice plate 41; the second regeneration zone 4 is no longer supplemented with charring Gas; reaction materials and comparative examples of the examples and the prior art are shown in Table 1 below.

Table 1

The dimensions of the anti-return device of the embodiment of the present invention in comparison with the crude oil technology are shown in Table 2 below.

Table 2

The distribution prediction of the reaction products of the examples and the prior art is shown in Table 3 below.

table 3

Claims

The invention discloses a catalytic cracking reaction regeneration method, which is composed of two reaction parts: a raw material reaction and a catalyst regeneration, wherein a casing of the regenerator is divided into a gas-solid separation zone, a catalyst regeneration reaction zone, and a scorch gas preheating zone;

a dense phase fluidized bed catalyst storage zone is disposed in the cone section below the gas-solid separation zone; the dense phase fluidized bed catalyst storage zone is disposed inside the catalyst regeneration reaction zone or independently outside the catalyst regeneration reaction zone; in the dense phase flow a regenerant conveying pipe is disposed between the catalytic bed catalyst storage zone and the charred gas preheating zone; and an orifice plate is disposed between the charred gas preheating zone and the catalyst regeneration reaction zone;

The reactor main body is a riser reaction section, and the raw material oil inlet port is followed by a raw material oil-gas zone and a catalytic cracking reaction zone, and a settler is arranged downstream of the catalytic cracking reaction zone, and a reaction product gas-solid separator is disposed therein, and the separated catalyst is disposed. Gravity down into the stripping section; the stripped catalyst enters the regenerator catalyst regeneration reaction zone, and is in contact with the charred gas from the scorched gas preheating zone to perform a scorch reaction;

The regeneration method includes:

1. The reaction raw materials are introduced into the reactor at different parts of the reactor, contacted with the catalyst and heated by the catalyst, and then reacted; the reaction product and the catalyst are discharged from the outlet of the reactor to separate the catalyst and the product gas, and the product gas is passed through. The settler oil and gas outlet flows out;

2. The catalyst after completion of the raw material reaction enters the stripping section of the settler for stripping, and the catalyst to be produced after stripping enters the bottom of the regeneration reaction zone in the middle of the regenerator, and is regenerated by the preheated charred gas from below;

The catalyst, the regenerated reaction gas and the flue gas generated by the regeneration reaction are transported upward together, and the gas and the catalyst are separated in the gas-solid separation zone of the regenerator, and the separated catalyst first enters the dense phase fluidized bed catalyst storage area in the regenerator. The dense phase fluidized bed catalyst storage area is sent to a scorch gas preheating zone at the bottom of the regenerator, and in the scorch gas preheating zone, the catalyst is directly mixed with the char gas to heat the scorched gas while the catalyst itself is cooled; The cooled regenerated catalyst enters the reactor below the inlet of the reaction raw material, and reacts with the reaction raw material under the action of the pre-lifting medium;

3. The first part of the charred gas enters the preheating zone of the charred gas in the scintillating gas preheating zone at the bottom of the regenerator, and directly forms a fluidized state contact heat exchange with the regenerated catalyst, and the gas is heated and flows upward into the catalyst regeneration zone; The charred gas carries a part of the catalyst to perform full gas-solid separation in the gas-solid separation zone of the regenerator, and the gas flows out of the regenerator from the flue gas outlet, and the separated catalyst enters the dense phase fluidized bed catalyst storage area by gravity sedimentation, and then enters the reaction. Instrument, participate in the reaction.
The regeneration method according to claim 1, wherein in 1 the reaction product and the catalyst are discharged together from the outlet of the reactor, and then enter the first-stage gas-solid separator and the second-stage gas-solid separator in the settler, thereby realizing Catalysis Separation of the agent and product gas.
The regeneration method according to claim 1, wherein in 2, the stripped spent catalyst passes through the inclined tube to enter the bottom of the regeneration reaction zone in the middle of the regenerator; the cooled regenerated catalyst is from the charred gas preheater The reactor is introduced into the reactor through the regeneration inclined tube under the inlet of the reaction raw material, and is contacted with the reaction raw material under the action of the pre-lifting medium.
The regeneration method according to claim 1, wherein said regenerator is provided with a regenerator catalyst cooler and/or said reactor is provided with a reaction catalyst desuperheater, a regenerator catalyst cooler and a catalyst for a reaction catalyst desuperheater The inlet is located in the regenerator dense phase fluidized bed storage area.
The regeneration method according to claim 1, wherein in 3, a char gas inlet pipe and a second gas distributor are disposed above or below the orifice plate between the scorch gas preheating zone and the catalyst regeneration zone, The second distributor introduces a second portion of the charred gas into the regenerator.
The regeneration method according to claim 5, wherein said second portion of the scorched gas is above the orifice level in the preheating zone of the regenerated catalyst, below the orifice between the charred gas preheating zone and the catalyst regeneration reaction zone Entering the regenerator, mixing with the high temperature gas from the charred gas preheater, and then entering the regeneration reaction zone through the orifice plate to participate in the scorch reaction.
The regeneration method according to claim 1, wherein when the catalyst is fed from the dense phase fluidized bed catalyst storage zone of the regenerator to the burned gas preheating zone, the burned gas is controlled by a valve provided on the regenerant transport pipe. The amount or level of catalyst in the hot zone.
The regeneration method according to claim 1, wherein the scorch gas is adjusted by a change in the amount or level of the catalyst in the scorch gas preheating zone and a change in the amount of scorch gas entering the preheating zone of the scorch gas The preheating temperature and the cooling temperature of the regenerated catalyst itself.
The regeneration method according to claim 1, wherein the catalyst regeneration reaction of the regenerator is divided into a first regeneration zone and a second regeneration zone; the first regeneration zone is at a lower portion, and the second regeneration zone is at an upper portion;

The catalyst and gas of the first regeneration zone are sent to the second regeneration zone to continue to burn;

The upper boundary of the second regeneration zone extends upwardly to a tapered section of progressively larger diameter between the regenerator regeneration reaction zone and the gas-solid separation zone; the dense phase fluidized bed catalyst storage zone is located within the cone section.
The regeneration method according to claim 9, wherein an inner tub connected to the first regeneration zone is disposed in a taper section below the gas-solid separation zone of the regenerator, and the inner tub divides the second regeneration into two inner and outer zones, the outer zone Forming the dense phase fluidized bed catalyst storage zone; the flue gas and the catalyst of the first regeneration zone enter the inner barrel to continue the charring reaction;

The inner tub is a cylinder of equal cross section or a scorch reaction zone in which the cross-sectional area is gradually increased upward and the gas flow rate is gradually decreased.
The regeneration method according to claim 9, wherein a casing of the second regeneration zone is disposed in the cone section of the regenerator and the gas-solid separation zone casing, and the first regeneration zone and the second regeneration zone are directly in communication, and the second regeneration zone is a taper section and a conveying pipe whose outlet setting area is gradually reduced, and a flue gas gas-solid initial separator is arranged at the outlet of the conveying pipe;

The casing of the second regeneration zone separates the second regeneration zone and the regenerator gas-solid separation zone into two separate spaces, and the catalyst and gas in the regeneration reaction zone are directly separated from the outlet of the regeneration reaction zone for preliminary gas-solid separation. The gas-solid separation zone of the regenerator is separated from the regenerator by a two-stage cyclone disposed between the regeneration zone and the regenerator casing, and the catalyst enters the catalyst storage zone between the regeneration reaction zone and the regenerator casing.
The regeneration method according to claim 9, wherein a catalyst circulation pipe is provided between the dense phase fluidized bed catalyst storage zone and the first regeneration zone to control a combustion reaction temperature of the first regeneration zone standby catalyst.
The regeneration method according to claim 4, wherein when the catalyst regeneration reaction requires heat extraction, the catalyst is introduced from the dense phase fluidized bed catalyst storage zone into the regenerator catalyst cooler, and the cooled regenerated catalyst directly enters the charring Gas preheating zone.
The regeneration method according to claim 9, wherein the regeneration method further comprises replenishing the second regeneration zone with a scorched gas, that is, a third portion of the scorched gas.
The regeneration method according to claim 14, wherein said third portion of scorched gas enters a regenerator below an orifice plate disposed between said first regeneration zone and said second regeneration zone;

Alternatively, the third portion of the char gas is replenished directly to the second regeneration zone or to the dense phase fluidized bed catalyst storage zone.
The regeneration method according to claim 1, wherein a retentate reflux pipe is disposed between the reactor stripping section and the bottom of the reactor or the gasification cracking reaction section to control the temperature inside the reactor, the ratio of the agent to the oil, and Catalyst activity.
The regeneration method according to claim 1, wherein a reaction regenerant desuperheater and a reaction regenerant after cooling are disposed between the regenerator dense phase fluidized bed catalyst storage zone and the bottom of the reactor or the cracking reaction section after gasification The conveying pipe allows the regenerant which has been cooled by the regenerant desuperheater to enter the reactor, and controls the temperature inside the reactor, the ratio of the agent to the oil, and the activity of the catalyst.
The regeneration method according to claim 14, wherein the amount of the first portion of the scorched gas directly introduced into the scorched gas preheating zone from the bottom is 35% based on the total amount of the scorch gas introduced into the regenerator. -85%, the gas empty tower flow rate of the charred gas preheating zone is 0.3m/s-1.0m/s; the second part of the scorched gas is 30-60%, and the third part of the scorched gas is 0-10%.
A catalytic cracking reaction regeneration device comprising a reactor, a regenerator, a settler, and a reactor and a regenerator arranged side by side, wherein:

The regenerator is used for charring regeneration of the catalyst to be produced from the reactor, the regenerator is installed vertically, and the inside of the casing is divided into a bottom charred gas preheating zone, a catalyst regeneration zone and a regenerator gas-solid separation zone;

a charred gas tube is arranged at the bottom of the preheating zone of the charred gas for introducing the first portion of the charred gas;

The catalyst regeneration is divided into a lower first regeneration zone and an upper second regeneration zone;

a second regeneration zone barrel connected to the first regeneration zone is disposed in the cone section below the gas-solid separation zone of the regenerator, and the second regeneration is divided into two inner and outer zones, and the outer zone is a dense phase fluidized bed catalyst storage zone;

The upper boundary of the second regeneration zone extends upward to a tapered section of the regenerative regeneration reaction zone and the regenerator gas-solid separation zone, wherein a gas-solid separator is disposed in the middle portion and the top portion is provided with a burning portion. Coke flue gas outlet;

An inclined tube is arranged between the stripping section of the settler and the first regeneration zone, and a regenerative inclined pipe is arranged between the preheating zone of the scorch gas and the bottom of the reactor;

a charred gas inlet pipe is provided in the charred gas preheating zone and the first regeneration zone for introducing a second portion of the scorched gas;

a regenerant transport tube is disposed between the dense phase fluidized bed catalyst storage area and the charred gas preheating zone, and a regenerant circulation pipe is disposed between the dense phase fluidized bed catalyst storage area and the bottom of the first regeneration zone;

A gas pipe is provided at the bottom of the second regeneration zone for introducing a third portion of the char gas.
The regenerating apparatus according to claim 19, wherein a second regeneration zone casing is disposed in the casing of the regenerator and the casing of the regenerator gas-solid separation zone, and the first regeneration zone and the second regeneration zone are directly connected, The outlet of the second regeneration zone is provided with a tapered cone section and a regeneration zone outlet delivery pipe, and a gas-solid primary separator for the flue gas is disposed at the outlet of the regeneration zone outlet delivery pipe.