阅读说明：本技术 一种原油催化转化制乙烯和丙烯的方法及装置 (Method and device for preparing ethylene and propylene by catalytic conversion of crude oil ) 是由 石宝珍 李荻 郭江伟 于 2020-07-09 设计创作，主要内容包括：本发明涉及一种原油直接催化转化制乙烯和丙烯的方法。所述原油经过脱盐脱水后先用闪蒸塔按沸点分成原油轻组分和沸点更高的原油重组分,然后采用流化催化方法进行催化转化,实现原油催化制乙烯和丙烯；原油催化转化在设置第一反应再生系统和第二反应再生系统的装置中进行；先在第一反应再生系统内进行高沸点大分子原油重组分催化裂化反应,然后更换催化剂后在第二反应再生系统逐渐升温条件下进一步催化裂化和热裂化制乙烯和丙烯。本发明方法通过直接使用针对性催化剂对原油不同馏分进行选择性催化转化,实现原油催化制乙烯和丙烯,不需设置常减压系统,能提高乙烯、丙烯产率,使经济性大大增加。本发明同时提供了实现上述方法的装置。(The invention relates to a method for preparing ethylene and propylene by directly catalyzing and converting crude oil. The crude oil is desalted and dehydrated and then is divided into a crude oil light component and a crude oil heavy component with a higher boiling point by a flash tower according to the boiling point, and then catalytic conversion is carried out by adopting a fluidized catalytic method, so that the ethylene and propylene are prepared by crude oil catalysis; the crude oil catalytic conversion is carried out in a device provided with a first reaction regeneration system and a second reaction regeneration system; firstly, carrying out catalytic cracking reaction on heavy components of high-boiling-point macromolecular crude oil in a first reaction regeneration system, then replacing a catalyst, and then further carrying out catalytic cracking and thermal cracking on the heavy components to prepare ethylene and propylene under the condition of gradually increasing the temperature in a second reaction regeneration system. The method of the invention realizes the catalytic preparation of ethylene and propylene by crude oil through directly using the specific catalyst to carry out selective catalytic conversion on different fractions of crude oil, and can improve the yield of ethylene and propylene without arranging an atmospheric and vacuum system, thereby greatly increasing the economy. The invention also provides a device for realizing the method.)

1. A method for preparing ethylene and propylene by catalytic conversion of crude oil, the crude oil (F0) after desalting and dehydrating is preheated and then separated into two components according to boiling points by a crude oil separation tower or a flash tower (T00), namely a crude oil heavy component (R12) and a crude oil light component (F0G), the crude oil heavy component (R12) is subjected to catalytic cracking in a catalytic conversion ethylene preparation device to prepare ethylene, and the crude oil light component (F0G) is sent out or subjected to catalytic cracking in a catalytic conversion ethylene preparation device to prepare ethylene; the device for preparing ethylene by catalytic conversion is provided with a first reaction regeneration system and a second reaction regeneration system which are arranged in parallel, wherein the first reaction regeneration system uses a first catalyst, and the second reaction regeneration system uses a second catalyst; the material flow generated by the first reaction regeneration system is further subjected to catalytic cracking and thermal cracking combined reaction in a second reaction regeneration system to obtain ethylene and propylene products; the method is characterized in that: the method comprises the following steps:

(1) pressurizing and preheating desalted and dehydrated crude oil (F0), and then feeding the crude oil into a crude oil separation tower or a flash tower (T00) to separate the crude oil into a crude oil light component (F0G) and a crude oil heavy component (R12);

(2) the heavy components (R12) of the crude oil are directly or after being heated, firstly catalytically converted in a first reaction regeneration system, enter a first reactor (R10) and are subjected to catalytic cracking reaction under the environment of a first catalyst from a first regenerator (G10); after the stream formed by the reaction in the first reactor (R10) enters a first settler (D10) to separate out the first catalyst, a first reaction system product (R14) is formed; the first catalyst separated by the first settler (D10) enters a first regenerator (G10) for regeneration after being stripped in a first stripping section (S10) and is recycled;

(3) the first reaction system product (R14) enters a second reactor (R20) of a second reaction regeneration system in a gas phase state, or the first reaction system product (R14) is separated into heavy components through a separation tower or a fractionating tower to form a first reaction system product light component (R14G), and the first reaction system product light component (R14G) enters the second reactor (R20) in a gas phase state to continue catalytic conversion; the second catalyst from the second regenerator (G20) enters a second reactor (R20) to further provide heat and raise the temperature to continue the catalytic cracking and thermal cracking reactions to produce ethylene and propylene products; after the material flow formed by the reaction of the second reactor (R20) enters a second settler (D20) to separate the catalyst, a second reaction system product (R24) is obtained; the catalyst separated by the second settler (D20) enters a second regenerator (G20) for regeneration after being stripped in a second stripping section (S20) and is recycled;

(4) when the crude oil light component (F0G) is processed by a catalytic conversion ethylene preparation device, the crude oil light component (F0G) directly enters a second reaction regeneration system, catalytic cracking is carried out in a second reactor (R20), or catalytic cracking is carried out in a third reactor (R30) additionally arranged in the second reaction regeneration system, and a material flow formed by the reaction of the third reactor (R30) enters a second settler (D20).

2. The process for the catalytic conversion of crude oil to ethylene and propylene as claimed in claim 1, wherein: the crude oil heavy component (R12) is a mixture containing a diesel oil component, a wax oil component and a heavy oil component in crude oil, and the boiling point is higher than 145 ℃; the crude oil light component (F0G) is the mixture of non-condensable gas, naphtha or light naphtha in the crude oil, or the mixture of the non-condensable gas, the naphtha or light naphtha and light diesel oil in the crude oil.

3. The process for the catalytic conversion of crude oil to ethylene and propylene as claimed in claim 1, wherein: the reaction temperature of the outlet of the first reactor (R10) is 490-550 ℃, the reaction time is 0.5-5.0 s, and the absolute pressure of the reaction pressure is 0.23-0.40 Mpa; the outlet reaction temperature of the second reactor (R20) is 600-750 ℃, the reaction time is 0.5-5.0 s, and the reaction pressure gauge pressure is 0.10-0.30 MPa.

4. The process for the catalytic conversion of crude oil to ethylene and propylene as claimed in claim 1, wherein: the active component of the first catalyst is selected from one or a mixture of HY, USY, REY, REHY, REUSY and H-ZSM-5; the active component of the second catalyst is selected from Y-type zeolite, L-type zeolite, ZSM-5 zeolite, beta zeolite, aluminum phosphate zeolite, mordenite, or one or a mixture of modified zeolites.

5. The process for the catalytic conversion of crude oil to ethylene and propylene as claimed in claim 1, wherein: the second reactor (R20) is set into two reaction zones with different upper and lower temperature and solvent-oil ratios, and comprises a lower sub-high temperature reaction zone (R27) and an upper high temperature reaction zone (R28), and a second regenerant of the second regenerator (G20) enters the sub-high temperature reaction zone (R27) and the upper high temperature reaction zone (R28) respectively in two paths;

the first reaction system product (R14) or the light component (R14G) of the first reaction system product after the heavy component is separated firstly enters a secondary high-temperature reaction zone (R27), and secondary high-temperature reaction is carried out under the environment of a second regenerant or lower regenerant introduced from a second regenerator (G20) through a second regeneration vertical pipe (G24), wherein the reaction temperature is 530-600 ℃, the reaction time is 0.1-5.0 s, and the reaction pressure gauge pressure is 0.12-0.30 MPa;

the product and the catalyst in the secondary high-temperature reaction zone (R27) flow upwards to enter the high-temperature reaction zone (R28), a second regenerant or an upper regenerant introduced from a second regenerator (G20) through an upper regeneration vertical pipe (G22) enters the second reactor (R20), the material flow of the secondary high-temperature reaction zone is conveyed to the high-temperature reaction zone (R28), and the reaction material flow is continuously subjected to the combined reaction of catalytic cracking and thermal cracking to generate ethylene and propylene products; the high-temperature reaction zone (R28) has the reaction temperature of 600-750 ℃, the reaction time of 0.1-5.0 s and the reaction pressure gauge pressure of 0.10-0.30 MPa.

6. The process for the catalytic conversion of crude oil to ethylene and propylene as claimed in claim 5, wherein: the temperature of the lower regenerant entering the secondary high temperature reaction zone (R27) is 660-760 ℃, and the carbon content of the catalyst is lower than 0.15%; the temperature of the upper regenerant introduced into the high-temperature reaction zone (R28) is 700-800 ℃, and the carbon content of the catalyst is lower than 0.5%.

7. The process for the catalytic conversion of crude oil to ethylene and propylene as claimed in claim 5, wherein: when the crude oil light component (F0G) is subjected to catalytic cracking conversion in the second reactor (R20), the crude oil light component (F0G) is reacted in the high-temperature reaction zone (R28).

8. The process for the catalytic conversion of crude oil to ethylene and propylene as claimed in claim 1, wherein: when the crude oil light component (F0G) is subjected to catalytic cracking conversion in the third reactor (R30), the reaction temperature is 640-750 ℃, the reaction time is 0.3-4.0 seconds, and the reaction pressure gauge pressure is 0.10-0.30 MPa.

9. The process for the catalytic conversion of crude oil to ethylene and propylene as claimed in claim 1, wherein: when the light component (R14G) of the product of the first reaction system enters the second reaction regeneration system, the light component (R14G) of the product of the first reaction system exchanges heat with the product (R24) of the second reaction system, and the heated light component (R14G) of the product of the first reaction system enters the second reaction regeneration system for reaction.

10. The process for the catalytic conversion of crude oil to ethylene and propylene as claimed in claim 1, wherein: the crude oil heavy component (R12) separated in the crude oil separation tower or flash tower (T00) is firstly hydrotreated, and the obtained crude oil heavy component hydrogenated component (R12H) enters a first reaction regeneration system for catalytic conversion.

11. A device for preparing ethylene and propylene by catalytic conversion of crude oil is characterized in that:

a first reaction regeneration system and a second reaction regeneration system are arranged at the downstream of a crude oil heating furnace or a heat exchanger (A0) and a crude oil separation tower or a flash tower (T00);

the first reaction regeneration system is provided with a first reactor (R10), a first settler (D10), a first stripping section (S10) and a first regenerator (G10), a flow line is arranged between a first reactor reaction raw material inlet (R12A) at the lower part of the first reactor (R10) and the bottom of the crude oil separation tower or flash tower (T00), and a first reactor regeneration agent inlet (R15A) at the lower part of the first reactor (R10) is communicated with a first regeneration agent outlet (G14A) of the first regenerator (G10) through a first regeneration riser (G14);

the second reaction regeneration system is provided with a second reactor (R20), a second settler (D20), a second stripping section (S20) and a second regenerator (G20); a second regenerant inlet (R25A) at the lower portion of the second reactor (R20) is in communication with a second regenerant outlet (G24A) of the second regenerator (G20) through a second regeneration riser (G24);

-a stream line is provided between the first reaction gas product outlet (R14A) of the first settler (D10) and the bottom of the second reactor (R20), or a stream line is provided between the first reaction gas product outlet (R14A) and the bottom of the second reactor (R20), while a separation or fractionation column is provided on the stream line; the first reactor (R10) and the second reactor (R20) are selected from a riser, a fluidized bed single or composite reactor.

12. The apparatus for the catalytic conversion of crude oil to ethylene and propylene as claimed in claim 11, wherein: a heavy oil and light component inlet is arranged at the lower part of a second reactor (R20) of the second reaction regeneration system, and a material flow pipeline is arranged between the heavy oil and light component inlet and the top of the crude oil separation tower or the flash tower (T00);

or a third reactor (R30) is arranged in the second reaction regeneration system, the third reactor (R30) and the second reactor (R20) share a second settler (D20), a second stripping section (S20) and a second regenerator (G20), a heavy oil light component inlet is arranged at the lower part of the third reactor (R30), a material flow pipeline is arranged between the heavy oil light component inlet and the top of the crude oil separation tower or flash tower (T00), and a second regenerant III inlet (R35A) at the lower part of the third reactor (R30) is communicated with a second regenerant III outlet (G34A) of the second regenerator (G20) through a third regeneration riser (G34).

13. The apparatus for the catalytic conversion of crude oil to ethylene and propylene as claimed in claim 12, wherein: the second reactor (R20) comprising a lower, secondary high temperature reaction zone (R27) and an upper high temperature reaction zone (R28); a second regenerant inlet (R25A) at the lower portion of the secondary high temperature reaction zone (R27) is communicated with a second regenerant outlet (G24A) of the second regenerator (G20) through a second regeneration riser (G24), and an upper regenerated catalyst inlet (R22A) at the lower portion of the high temperature reaction zone (R28) is communicated with an upper regenerant outlet (G22A) of the second regenerator (G20) through an upper regeneration riser (G22).

Technical Field

The invention belongs to the technical field of crude oil catalytic conversion, and particularly relates to a method for preparing ethylene and propylene by crude oil catalytic conversion. The invention also provides a device for realizing the method.

Background

The low-carbon olefin represented by ethylene and propylene is the most basic raw material in chemical industry, and the existing catalytic conversion technology is used for producing gasoline and diesel oil and simultaneously producing the low-carbon olefin as a byproduct, so that the requirement of the current market on organic chemical raw materials can not be met. Aromatic hydrocarbon is an important organic chemical raw material with the yield and the scale second only to ethylene and propylene, and derivatives thereof are widely used for producing chemical products such as chemical fibers, plastics, rubber and the like and fine chemicals, and with the continuous development of petrochemical industry and textile industry, the demand of aromatic hydrocarbon in the world is continuously increased. Natural gas or light petroleum fractions are mostly used as raw materials at home and abroad, low-carbon olefin is produced by adopting a steam cracking process in an ethylene combined device, and a large amount of other basic raw materials such as olefin, aromatic hydrocarbon and the like are produced as byproducts during the production of ethylene. Although the steam cracking technology is developed for decades and the technology is continuously improved, the steam cracking technology still has the advantages of high energy consumption, high production cost and CO₂The discharge amount is large, the product structure is not easy to adjust, and other technical limitations, and the traditional technology for producing ethylene and propylene by steam cracking is facing a severe test. The catalytic conversion method for preparing ethylene and the byproduct of low-carbon olefins such as propylene and butylene and chemical raw materials such as aromatic hydrocarbon are new ways to solve the problem of resource shortage and low-cost production of chemical products, and become important research subjects and hot problems at present.

In the aspect of preparing low-carbon olefins such as ethylene, propylene, butylene and the like by fluidized catalytic conversion, the following ideas are mainly provided:

1. the reaction raw material is divided into different fractions by a distillation tower, and the different fractions are respectively subjected to catalytic reaction in different reactors. For example, CN109575982A provides a method for preparing low-carbon olefins and aromatics by catalytic cracking of crude oil, which comprises desalting and dehydrating crude oil, heating in a heating furnace, and then feeding into a distillation tower to separate the crude oil into light and heavy components with a cutting point of 150-300 ℃; the light components coming out of the top of the tower and the heavy components coming out of the bottom of the tower contact and react with the high-temperature catalyst in the atmosphere of water vapor in the two reactors.

2. The materials in the reactor are fed and reacted layer by layer. For example, CN1898362 provides a method for producing light olefins and aromatics, in which a raw material is contacted with a catalytic cracking catalyst, the reaction is divided into at least two layers of feeding materials according to the nature of the raw material, and different liquid reaction products from a fractionating tower are returned to a reactor from different positions to be converted again except for target products. CN1215041A provides a method for preparing ethylene, propylene, aromatic hydrocarbon and the like by directly converting various feeding hydrocarbons, wherein a plurality of groups of feeding holes are arranged on a reactor, so that hydrocarbons with different properties enter a device from different feeding holes, and the cracking reaction is carried out under the same process conditions of all parts. CN104560154A provides a hydrocarbon catalytic conversion method for increasing the yield of light olefins and light aromatics, which comprises the following steps: contacting a heavy hydrocarbon raw material with a cracking catalyst in a first reactor to perform catalytic cracking reaction, and then separating to obtain a first carbon deposition catalyst and a first reaction product; injecting light hydrocarbon raw materials from the upstream of the second reactor, and injecting medium hydrocarbon raw materials from the middle part of the second reactor to perform catalytic cracking reaction; and introducing the reaction mixture generated in the second reactor into a third reactor for continuous reaction, and then separating to obtain a second carbon deposition catalyst and a second reaction product. Wherein the cracking catalyst is a cracking catalyst containing modified beta zeolite, and the modified beta zeolite is beta zeolite modified by phosphorus and transition metal M.

3. Outside the raw oil riser, additionally establishing a reactor to convert different fractions by catalysis again, namely adopting a multi-reactor form, carrying out conventional raw oil reaction in the first reactor, and feeding one or more fractions such as crude gasoline into the additionally established reactor for further conversion to obtain a target product after fractionation; for example, CN1388216 discloses a catalytic conversion method for preparing propylene, butylene and gasoline with low olefin content, comprising the following steps: (1) injecting preheated hydrocarbon oil (still liquid) into a riser, contacting and reacting with a catalyst containing pentasil zeolite and Y-type zeolite, and introducing an oil agent mixture into a fluidized bed through the riser; (2) injecting gasoline into the fluidized bed, contacting and reacting with the catalyst from the riser; (3) separating the oil mixture, stripping the reacted catalyst, regenerating in a regenerator, and returning the regenerated catalyst to the riser for reuse. The method can not only increase the yield of low-carbon olefin, but also produce high-quality gasoline with low olefin content. CN1258580C discloses a method and a system for upgrading gasoline by deeply reducing olefin and increasing octane number by catalytic conversion, wherein a catalytic upgrading reactor is added in a reaction-regeneration system of a heavy oil catalytic conversion device to perform catalytic upgrading reaction on gasoline fraction by catalytic conversion. The upgraded catalytically converted gasoline fraction may be a naphtha whole fraction, a naphtha light fraction or a naphtha heavy fraction obtained by establishing a secondary condensation system at the top of the fractionator.

4. The light raw material is used for producing low-carbon olefin. CN104557378A discloses a method for producing propylene by naphtha catalytic cracking. The method comprises the following steps: (1) under the pretreatment condition, contacting naphtha with a pretreatment agent to obtain treated oil with reduced alkaline nitrogen content; (2) and (2) under the condition of naphtha catalytic cracking reaction, contacting the treated oil and water obtained in the step (1) with a catalyst to obtain a catalytic cracking product.

5. In order to increase the yield of the light olefins, a 'cocatalyst' suitable for cracking the small-molecular hydrocarbons can be added, and the propylene can be increased by 1-1.5% by adding 5-8% of the heavy oil reaction catalyst.

The above technologies for reducing olefins by Fluidized Catalytic Conversion (FCC) and increasing the production of chemical feedstocks have some common drawbacks as follows:

1. different raw materials require different catalysts, heavy oil cracking requires high macromolecule cracking capability of the catalyst, and generally requires a larger aperture; c4 and C5 cracking need catalysts with low carbon olefin selectivity, and generally need smaller pore diameter; the prior art processes described above all use the same catalyst, i.e., only one catalyst. Although 5-8% of auxiliary agent can be added into the regenerator to further convert the small molecules in order to increase the yield of the low-carbon olefins, when the auxiliary agent is added into the FCC catalyst, the catalyst cracking activity is inevitably reduced due to the dilution effect on the catalyst. The heavy oil cracking conversion rate is reduced by 1 percentage point per 5% of the addition of the promoter, which is an important factor that seriously affects the economy of the FCC technology, and the improvement of the objective product is limited due to the low concentration of the promoter after mixing with the heavy oil cracking catalyst.

2. Because the second reaction system needs more reaction heat and generally has less coke formation, the heat generated by the regeneration of the coke formation can not provide the heat required by the reaction, and if the independent second reaction system is established by utilizing the prior art, the heat balance problem is restricted.

3. In all the recycling methods, the fraction is separated by a fractionating tower, cooled into liquid by heat exchange and then returned to the reactor, different fractions are firstly cooled into liquid by the heat exchange of the fractionating tower, and the liquid is returned to the original reactor or is further converted by another reactor directly after separation or after proper re-preheating (still liquid). Through the processes of cooling and heating, the investment of equipment and energy consumption is increased, and the economical efficiency of the process technology is greatly reduced.

4. The ethylene preparation from the crude oil requires higher reaction temperature, generally higher than 650 ℃; the reaction process of catalytically preparing olefin from catalytically cracked material oil, especially heavy material oil, is a process of gradually cracking and gradually reducing molecular weight; smaller molecules are more difficult to activate, the required reaction temperature is higher, the temperature is high, and the thermal cracking reaction is naturally performed, so that the selectivity of a target product is influenced; how to allocate the reaction temperature and the molecular characteristics of petroleum hydrocarbon well, balance the catalytic cracking reaction and the thermal cracking reaction well, and have important significance for realizing the limit control of the reaction; the expected reaction process is that the specific gravity of catalytic reaction is increased as much as possible in the large molecule cracking stage of heavy oil and the like, thermal cracking is limited, the temperature is gradually increased in the small molecule cracking stage, and the proportion of thermal cracking reaction is increased; however, in the prior art, heat is provided in the inlet area of the reactor in the reaction process, the reaction is a gradual cooling process, particularly for the reaction for preparing ethylene, the reaction temperature is higher in the initial stage, namely the heavy oil cracking stage at the lower part of the reactor, and heavy components are directly subjected to thermal cracking reaction, so that the effect of catalytic cracking reaction is reduced.

CN101323798A (application No. 200810140866.7) discloses a catalytic conversion method, which is sequentially performed in a first reaction system and a second reaction system, wherein all or part of fractions generated after raw oil enters the first reaction system for catalytic reaction enter the second reaction system in a gaseous and/or liquid form for further catalytic reaction, and the first reaction system and the second reaction system respectively use corresponding catalysts according to the difference between the reaction raw material and the target product. The method overcomes the defects of poor selectivity, low auxiliary agent content, dilution effect on the catalyst and the like when a single catalyst is adopted by using two reaction systems and using a specific catalyst to carry out selective catalytic conversion on different fractions. However, the following problems still remain in this method:

no matter the raw oil of the first reaction system is cracked, or the gas-phase intermediate component of the second reaction system is further catalytically cracked, the heat in the reaction process is still provided in the inlet area of the reactor, the reaction is a gradual temperature rise process, the molecules are gradually reduced in the continuous reaction process of the intermediate component, and the heat condition for re-cracking the small molecules is insufficient in the rear section of the reactor, so that the production of high-value product ethylene is greatly reduced.

Disclosure of Invention

The invention aims to provide a method for preparing ethylene and propylene by catalytic conversion of crude oil on the basis of the prior art, which adopts a double-reaction regeneration system to carry out gradual temperature rise, two-stage or three-stage temperature gradient double catalysis and gas phase relay catalytic conversion on the crude oil which is desalted, dehydrated and separated into light and heavy components, can realize the high-yield preparation of ethylene and propylene low-carbon olefin products, has low equipment investment and low energy consumption, and can be used for treating the crude oil or heavy petroleum hydrocarbon raw materials to produce chemical raw materials. The invention also provides a device for preparing ethylene and propylene by catalytic conversion of crude oil.

The technical scheme of the invention is as follows:

a method for preparing ethylene and propylene by crude oil catalytic conversion, the crude oil after desalinization and dehydration is heated in a heating furnace or a heat exchange device after being pressurized by a pump, and separated into two components according to boiling points by a crude oil separation tower or a flash tower (or a flash tower or a primary distillation tower) after being preheated, namely a crude oil heavy component (or a high boiling point component separated from the crude oil, or a high boiling point component separated from the primary distillation tower or the flash tower) and a crude oil light component (or a low boiling point component separated from the crude oil, or a light hydrocarbon component separated from the crude oil); the heavy component of the crude oil is subjected to catalytic cracking in an ethylene preparation device by catalytic conversion to prepare ethylene and propylene, and the light component of the crude oil is sent out of the device or subjected to catalytic cracking in the ethylene preparation device by catalytic conversion to prepare ethylene and propylene;

the device for preparing ethylene by catalytic conversion is provided with a first reaction regeneration system and a second reaction regeneration system which are arranged in parallel, wherein the first reaction regeneration system uses a first catalyst, and the second reaction regeneration system uses a second catalyst; in specific implementation, each reaction regeneration system is provided with a reactor and a regenerator; a catalyst with strong heavy oil catalytic cracking capability is used in the first reaction regeneration system for carrying out catalytic cracking conversion on high boiling point components separated from the crude oil; a catalyst or a heat carrier with strong cracking capability of intermediate components or micromolecules and high selectivity of low-carbon olefin is used in the second reaction regeneration system; the first reaction regeneration system is provided with one or more reactors, and when the properties of reaction raw materials entering the first reaction regeneration system are different, the raw materials with different properties can be subjected to catalytic cracking reaction in different reactors; the material flow generated by the first reaction regeneration system is further subjected to catalytic cracking and thermal cracking combined reaction in a second reaction regeneration system to obtain ethylene and propylene products; the second reaction regeneration system is provided with one or more reactors; after the catalyst is separated from the reaction product of the first reaction regeneration system, the reaction product is in a whole or partial gas phase state, or after heavy components with high boiling point are separated, the gas phase state of lighter components enters a second system for further conversion; the light components of the crude oil separated by the crude oil separation tower or the flash tower can be directly subjected to catalytic conversion and thermal cracking in the second reaction regeneration system;

the method comprises the following steps:

(1) the desalted and dehydrated crude oil is pressurized and pumped into a heat exchange device or a heating furnace for heating, and then enters a crude oil separation tower or a flash tower after being preheated to be separated into crude oil light components (non-condensable gas, light naphtha or naphtha and light diesel oil which are low boiling point components) and crude oil heavy components (other components of the crude oil light components are separated, namely the components of the crude oil light components with boiling points higher than the low boiling point in the crude oil, including diesel oil, wax oil and heavy oil components in the crude oil); the components and the proportion of the light components and the heavy components of the crude oil can be adjusted by controlling the temperature of the preheated crude oil and the temperature and the pressure of a crude oil separation tower or a flash tower;

(2) the heavy components of the crude oil are directly or after being heated, firstly subjected to catalytic conversion in a first reaction regeneration system, enter a first reactor, and subjected to catalytic cracking reaction in the environment of a first catalyst introduced from the first regenerator through a first regeneration vertical pipe, the catalytic cracking conversion, decarburization and demetalization of the heavy components and macromolecules are primarily completed, the reaction that the heavy components and the macromolecules are primarily subjected to catalytic cracking is realized, the heavy components and the macromolecules are converted into components mainly comprising high-olefin gasoline and diesel oil, namely intermediate components mainly comprising C5-C18, and the intermediate components become intermediate raw materials which are further cracked into ethylene and propylene, and after the intermediate products flow out of the first reactor and are separated out of the catalyst, gas phases can be kept to directly enter a second reaction regeneration system for continuous reaction; after a material flow formed by the reaction of the first reactor enters a first settler and a first catalyst is separated out, a first reaction system product is formed; the first catalyst separated by the first settler enters a first regenerator for regeneration after being stripped in a first stripping section, and is recycled;

(3) the product gas phase state of the first reaction system enters a second reactor of a second reaction regeneration system, or the product of the first reaction system is separated into heavy components (namely the liquid heavy components of the product of the first reaction system) through a separation tower or a fractionating tower to form light components of the product of the first reaction system, and the light components of the product of the first reaction system enter the second reactor in the gas phase state to continue catalytic conversion; in order to improve the efficiency of the second reaction regeneration system, the gas stream generated by the first reaction system, namely the product of the first reaction system, can firstly enter a separation tower or a fractionating tower to separate heavy components with high boiling point; the other fractions enter a second reaction regeneration system in a gaseous/gas phase mode to further perform catalytic reaction; returning all or part of the separated heavy components to the first reaction regeneration system for continuous catalytic conversion; a heavy component delivery device which does not return to the first reaction regeneration system; during specific implementation, part or all of the heavy components separated from the product of the first reaction system are returned to the first reactor for continuous catalytic conversion, or the heavy components are returned to the first reactor for continuous catalytic conversion after hydrogenation; the second catalyst from the second regenerator and introduced by the second regeneration vertical pipe enters the second reactor, further provides heat and increases the temperature, and continues catalytic cracking and thermal cracking reactions to generate ethylene and propylene products; after the material flow formed by the reaction in the second reactor enters a second settler and the catalyst is separated out, a second reaction system product is obtained; the catalyst separated by the second settler enters a second regenerator for regeneration after being stripped in a second stripping section, and is recycled;

(4) when the crude oil light component is processed by the ethylene preparation device through catalytic conversion, the crude oil light component directly enters the second reaction regeneration system, catalytic cracking is carried out in the second reactor, namely, the crude oil light component and the material flow generated by the reaction of the first reaction regeneration system are subjected to the ethylene preparation reaction through catalytic cracking in the same reactor, or catalytic cracking is carried out in a third reactor additionally arranged in the second reaction regeneration system, and the material flow formed by the reaction of the third reactor enters a second settler.

The method for preparing ethylene and propylene by catalytic conversion of crude oil is further characterized in that crude oil is recombined into a mixture containing a diesel oil component, a wax oil component and a heavy oil component in the crude oil, and the boiling point of the mixture is higher than 145 ℃; the light component of the crude oil is the mixture of non-condensable gas, naphtha or light naphtha component in the crude oil, or the mixture of the non-condensable gas, the naphtha or light naphtha component and light diesel oil component in the crude oil, and the boiling point is lower than 360 ℃. In the invention, as is known in practice, the composition of the light components of the crude oil depends on the pressure and temperature of a crude oil separation tower or a flash tower, and the composition of the light components of the crude oil can be adjusted according to the temperature of the separation tower or a primary distillation tower, for example, the light components of the crude oil can be noncondensable gas and light naphtha below 150 ℃, can be noncondensable gas and naphtha below 180 ℃, can be noncondensable gas and gasoline below 200 ℃, and can be light diesel oil components below 300 ℃, because the petroleum hydrocarbon components are complex, the separated light components can contain part of heavy components and part of light components in the separation process, wherein at least saturated and dissolved parts can not be separated, and the components below the separated light diesel oil can be the light components of the crude oil; in the method for preparing ethylene and propylene by catalytic conversion of crude oil, further, the reaction of the first reactor is carried out under the condition favorable for catalytic conversion, the outlet reaction temperature is 490-550 ℃, the reaction time is 0.5-5.0 s, and the absolute pressure of the reaction pressure is 0.23-0.40 Mpa; the outlet reaction temperature of the second reactor is 600-750 ℃, the reaction time is 0.5-5.0 s, the gauge pressure of the reaction pressure is 0.10-0.30 MPa, and the actual reaction temperature is controlled by the catalyst amount entering the second reactor (the relative high-temperature reaction zone); in the method for preparing ethylene and propylene by catalytic conversion of crude oil, the active component of the first catalyst is selected from one or a mixture of HY, USY, REY, REHY, REUSY and H-ZSM-5; the active component of the second catalyst is selected from Y-type zeolite, L-type zeolite, ZSM-5 zeolite, beta zeolite, aluminum phosphate zeolite, mordenite, or one or a mixture of modified zeolites.

In the method for preparing ethylene and propylene by catalytic conversion of crude oil, the second reactor is provided with an upper stage heat supply and a lower stage heat supply and catalyst circulation and is provided with two reaction zones with different upper and lower temperatures and catalyst-to-oil ratios, the second reactor is divided into the upper and lower reaction zones by the upper catalyst and the heat supply position, the upper and lower reaction zones comprise a lower sub-high temperature reaction zone and an upper high temperature reaction zone, a second regenerant (or called as a second catalyst or a second regenerated catalyst) of the second regenerator respectively enters the sub-high temperature reaction zone and the upper high temperature reaction zone in two paths, the upper catalyst supplies heat and the catalyst further improves the reaction temperature and the catalyst-to-oil ratio, selective reaction is carried out in the upper and lower reactors of graded heat supply (two-stage heat supply) and graded catalyst supply (two-stage catalyst supply), and gradual temperature rise in the reaction process of the second reaction regeneration, the reaction severity is gradually increased, the reaction mode of gradually increasing the reaction temperature is adapted to the molecular structure of reactants with gradually reduced molecular weight and the change of the requirements on reaction conditions, and the efficiency of preparing ethylene and the selectivity of products at different orders are improved;

the first reaction system product or the light component of the first reaction system product after heavy component separation firstly enters a secondary high temperature reaction zone, secondary high temperature reaction is carried out under the environment of a second catalyst (at this time, the second catalyst is also called a lower regenerant) introduced from a second regenerator through a second regeneration vertical pipe, catalytic cracking conversion is continuously carried out, further, cracking reaction which is mainly catalytic cracking reaction is carried out on the residual heavy component or larger molecules and intermediate components, C3-C8 components are added, more C3-C8 components are generated, the reaction temperature is 530-600 ℃, the reaction time is 0.1-5.0 s, the reaction pressure gauge pressure is 0.12-0.40 MPa, and the actual reaction temperature is controlled by the catalyst entering the secondary high temperature reaction zone;

the product and the catalyst in the secondary high-temperature reaction zone flow upwards to enter the high-temperature reaction zone, the second catalyst or the upper regenerant introduced from the second regenerator through the upper regeneration vertical pipe enters the second reactor, and the material flow in the secondary high-temperature reaction zone is conveyed to the high-temperature reaction zone, and after heat is provided and the temperature of the material flow is increased, the material flow continues to carry out the combined reaction of catalytic cracking and thermal cracking to generate ethylene and propylene products; the high-temperature reaction zone has the reaction temperature of 600-750 ℃, the reaction time of 0.1-5.0 s, the reaction pressure gauge pressure of 0.10-0.40 MPa, and the actual reaction temperature is controlled by the catalyst entering the high-temperature reaction zone.

Preferably, the temperature of the second catalyst or lower regenerant entering the secondary high temperature reaction zone is 660-760 ℃, and the carbon content of the catalyst is lower than 0.15%; the temperature of the second catalyst or the weighting regenerant introduced into the high-temperature reaction zone is 700-800 ℃, and the carbon content of the catalyst is lower than 0.5%.

Preferably, when the crude oil light component is subjected to catalytic cracking conversion in the second reactor, the crude oil light component is directly reacted in the high-temperature reaction zone.

The method for preparing ethylene and propylene by crude oil catalytic conversion further comprises the step of carrying out catalytic cracking conversion on light components of crude oil in an independent third reactor, wherein the reaction temperature is 640-750 ℃, the reaction time is 0.3-4.0 seconds, and the reaction pressure gauge pressure is 0.10-0.40 MPa.

Further, in practice, the fuel oil can be supplemented in the second regenerator of the second reaction regeneration system; and preferably, the heavy cycle oil is supplemented in front of the outlet of the second reactor to serve as fuel oil, so that quenching and coke formation supplement are realized.

In the method for preparing ethylene and propylene by catalytic conversion of crude oil, further, when the light component of the product of the first reaction system enters the second reaction regeneration system, the light component of the product of the first reaction system exchanges heat with the product of the second reaction system, and the heated light component of the product of the first reaction system enters the second reaction regeneration system to react so as to make up for the heat of the second reaction regeneration system.

The method for preparing ethylene and propylene by crude oil catalytic conversion further comprises the steps of firstly carrying out hydrogenation treatment on the crude oil heavy component separated in the crude oil separation tower or the flash tower to remove heavy metal, sulfur and alkaline nitrogen elements, improving the hydrogen content and improving the property, and then feeding the obtained crude oil heavy component hydrogenation component into the first reaction regeneration system for catalytic conversion.

The invention also provides a device for preparing ethylene and propylene by catalytic conversion of crude oil, wherein the device for preparing olefin by catalytic conversion of crude oil is provided with two reaction regeneration systems in parallel, namely a first reaction regeneration system and a second reaction regeneration system connected with the first reaction regeneration system on the process; the first reaction regeneration system and the second reaction regeneration system are both provided with a reactor and a catalyst regenerator; the first reaction regeneration system can be provided with one or more reactors, and the second reaction regeneration system is provided with one or two reactors; the specific scheme is as follows: a first reaction regeneration system and a second reaction regeneration system are arranged at the downstream of a crude oil heating furnace or a heat exchanger (crude oil preheating heat exchange part) and a crude oil separation tower or a flash tower (flash evaporation or primary distillation part);

the first reaction regeneration system is provided with a first reactor, a first settler, a first stripping section and a first regenerator, a first reactor reaction raw material inlet is arranged at the lower part of the first reactor, and a material flow pipeline is arranged between the first reactor reaction raw material inlet and the bottom of the crude oil separation tower or the flash tower so as to introduce crude oil heavy components separated by the crude oil separation tower or the flash tower into the first reactor; a first reactor regenerant inlet at the lower portion of the first reactor is communicated with a first regenerant outlet of the first regenerator through a first regeneration riser;

the second reaction regeneration system is provided with a second reactor, a second settler, a second stripping section and a second regenerator; a second regenerant inlet at the lower part of the second reactor is communicated with a second regenerant outlet of the second regenerator through a second regeneration vertical pipe; a material flow pipeline is arranged between the first reaction gas product outlet of the first settler and the bottom of the second reactor to introduce a first reaction system product into the second reactor, or a material flow pipeline is arranged between the first reaction gas product outlet and the bottom of the second reactor, and a separation tower or a fractionating tower is arranged on the material flow pipeline at the same time; the first reactor and the second reactor are selected from a riser, a fluidized bed single or composite reactor.

In the above apparatus for producing ethylene and propylene by catalytic conversion of crude oil, further, a heavy oil light component inlet is provided at the lower part of the second reactor of the second reaction regeneration system, and a material flow line is provided between the heavy oil light component inlet and the top of the crude oil separation tower or the flash tower, so as to introduce the crude oil light component separated by the crude oil separation tower or the flash tower into the first reactor;

or the second reaction regeneration system is provided with a third reactor, the third reactor and the second reactor share a second settler, a second stripping section and a second regenerator, the lower part of the third reactor is provided with a heavy oil light component inlet, a material flow pipeline is arranged between the heavy oil light component inlet and the top of the crude oil separation tower or the flash tower so as to introduce the crude oil light component separated by the crude oil separation tower or the flash tower into the third reactor, and a second regenerant III inlet at the lower part of the third reactor is communicated with a second regenerant III outlet of the second regenerator through a third regeneration vertical pipe.

In the above method for producing ethylene and propylene by catalytic conversion of crude oil, further, the second reactor (configured as an upper and lower partitioned reactor with upper and lower catalyst circulation and twice heat supply) comprises a lower sub-high temperature reaction zone and an upper high temperature reaction zone; and a second regenerant inlet at the lower part of the secondary high-temperature reaction zone is communicated with a second regenerant outlet of the second regenerator through a second regeneration vertical pipe, and an upper regenerated catalyst inlet at the lower part of the high-temperature reaction zone is communicated with an upper regenerant outlet of the second regenerator through an upper regeneration vertical pipe.

The technical scheme of the invention is as follows:

1. in the specific implementation, the crude oil after the desalting and dehydrating treatment is subjected to heat exchange at the pressure of 0.8-1.8 MPa and preheated to 200-fold-plus-minus-plus-minus-plus-minus-; the high boiling point component comprises a conventional diesel oil component, a wax oil component and a heavy oil component; the specific operation of the flash or preliminary distillation column, as well as the split boiling points and specific components of each component, are well known to those skilled in the art; the high boiling point component separated from the crude oil directly or after being heated enters a catalytic cracking ethylene preparation device to prepare ethylene and propylene by fluidized catalysis, and the low boiling point component is processed by other devices such as steam cracking and the like or is subjected to fluidized catalytic conversion together with the high boiling point component to prepare ethylene and propylene;

in the invention, the heavy components of the crude oil, namely the diesel oil component in the high boiling point component, can enter a first reaction regeneration system and a second reaction regeneration system together with the wax oil component and the heavy oil component in sequence for catalytic conversion; or the high boiling point component is firstly separated, the separated diesel oil component directly enters the second reaction regeneration system, and the wax oil component and the heavy oil component outside the diesel oil component are separated and enter the ethylene preparation device through catalytic conversion from the first reaction regeneration system.

2. The reaction regeneration system is known and provided with a reactor, a settler, a steam stripping section and a regenerator, wherein the outlet of the reactor is communicated with a gas-solid separation device in the settler, the steam stripping section is arranged below the settler, the lower part of the steam stripping section is communicated with the regenerator through a spent riser (spent catalyst conveying pipe), and the regenerator is communicated with a regenerant inlet of the reactor through a regenerated riser (regenerated catalyst conveying pipe); in the specific implementation and arrangement: the reactor and the regenerator are preferably arranged in parallel, and the reactor and the settler can be coaxially arranged or arranged in parallel; the top of the settler is provided with a product outlet of the reaction system; one or more reactors can be arranged in one set of reaction regeneration system to meet the requirements of different raw materials, and the outlets of the reactors can be communicated with the same settler to carry out gas-solid separation operation on the reacted material flow; the lower part of the reactor is provided with a raw material feeding port (a feeding nozzle when liquid phase feeding is carried out), the feeding port is arranged above or below a regenerant inlet of the reactor, and a lifting or fluidizing medium gas inlet is arranged at the bottom of the reactor. The conventional specific arrangement and connection positions of the reactor, the settler, the stripping section and the regenerator in the reaction regeneration system, and the inlet and outlet positions and specification requirements of various material flows can be grasped by engineering technicians, and are not described in detail below. As is known, the reaction process of the reactor using a reaction regeneration system in the form of a riser is as follows: the regenerated catalyst or called regenerating agent enters the lower part of the reactor through the regeneration vertical pipe, goes upward along the reactor, the reaction raw material enters the reactor through the feed inlet, contacts with the catalyst and flows upward together to realize reaction, the material flow after the reaction enters the settler to separate the catalyst, the product flows out through the product outlet, the catalyst enters the stripping section for stripping, and the spent catalyst or called spent agent enters the regenerator through the spent vertical pipe to realize regeneration and recycle.

3. In the implementation of the invention, the product of the first reaction system, although containing heavy components similar to oil slurry recycle oil, can directly enter the second reaction regeneration system in a gas phase state. The reaction for preparing the ethylene needs high temperature of more than 600 ℃, and the core problem to be solved is that the reaction coke formation can not provide enough reaction heat; the first reaction regeneration system can conveniently provide heat by heating the raw materials, and the second reaction regeneration system can increase coke formation and realize heat supply because light components generate less coke, heat required by high-temperature cracking is more, and heat lacking in the second reaction regeneration system is more, and heavy components in the product of the first reaction system are properly introduced; part of heavy components enter the second reaction regeneration system, so that the heat is transferred from the first reaction regeneration system to the second reaction regeneration system skillfully, and other supplementary heat needed by the second reaction regeneration system is reduced; meanwhile, as all the gas phase enters the second reaction regeneration system without being cooled, more heat can be transferred to the second reaction regeneration system. In addition, from the view of reaction catalytic chemistry, the heavy component is well separated, but the separated heavy component can be liquefied only by taking heat and reducing the temperature, and meanwhile, the temperature of the light component is also reduced, so that the heat brought into a second reaction regeneration system is reduced, and as a result, the heat of the system is insufficient, and particularly, the second system needs to supplement more heat;

the heavy component can be separated from the product of the first reaction system, and the light component enters the second reaction regeneration system in a gas phase state, so that the reaction efficiency of the second reaction regeneration system is improved; all or part of the separated heavy components return to the first reaction regeneration system for continuous catalytic conversion, and the heavy components which do not return to the first reaction regeneration system are sent out of the device; heavy components separated from a product of the first reaction system are subjected to hydrogenation treatment, appropriate aromatic hydrocarbon ring opening and side chain scission are carried out, the hydrogen content is increased, the properties of the heavy components are improved, and then the heavy components are returned to the first reaction regeneration system for reaction, so that the catalytic conversion efficiency of the first reaction regeneration system is improved;

the separated light components can exchange heat with a product stream of the second reaction regeneration system, and enter the second reaction regeneration system for continuous reaction after being heated;

heavy components are separated, and the heavy components can be separated through cooling of a heat exchange device; or the heavy components are separated by a fractionating tower (namely a fractionating system) or a separating tower, the fractionating tower or the separating tower is arranged in a material flow link between the product outlet of the first settler and the bottom of the second reactor, the fractionating tower or the separating tower is provided with a tower bottom reflux device or a device combining the tower bottom reflux and the middle heat exchange, and the fractionating tower or the separating tower separates the heavy components by the way of combining the tower bottom heat exchange or the tower bottom heat exchange and the middle heat exchange; separation of heavy components is a common process and is well known to engineering designers. It is known that a fractionating column and a separating column both work on the basis of the principle of fractionation to separate components, both according to different boiling points, the fractionating column has a side product in addition to separating the components into gas and liquid components, and the separating column only separates the gas and liquid components without a side product.

4. When the heavy component separated from the product of the first reaction system returns to the first reaction system for continuous reaction, the heavy component enters the first reactor again for reaction, or enters an additional independent reactor for reaction, the cutting temperature of the heavy component is controlled according to the boiling point of 350-360 ℃, and part or all of the components with high boiling point returns to the first reaction regeneration system, namely, when the heavy component separated from the product of the first reaction system returns to the first reaction regeneration system for continuous reaction, the cutting temperature of the heavy component is controlled according to the boiling point of 350 ℃, part or all of the components with boiling point higher than 350 ℃ return to the first reaction regeneration system, or after hydrogenation, the heavy component returns to the first reaction regeneration system, and the rest is sent out; or the heavy component cutting temperature is controlled according to the boiling point of 480-500 ℃, and the components with the boiling point higher than 480-500 ℃ are separated and then sent out of the device or returned to the first reaction regeneration system after being subjected to hydrogenation treatment.

5. In the invention, crude oil heavy combination obtained by crude oil preliminary separation is reacted under the condition of two-stage or even three-stage temperature gradient to prepare ethylene and propylene in turn, firstly, crude oil heavy components enter a first reaction zone, namely a low-temperature reaction zone in a first reaction regeneration system to carry out cracking reaction, and all or part of the generated components enter a second reaction regeneration system in turn in a gaseous form to carry out cracking reaction with increased temperature; when at least one reactor, namely the second reactor, in the second reaction regeneration system is provided with an upper stage and a lower stage of heat supply and catalyst circulation, the gaseous components generated by the first reaction regeneration system continuously carry out cracking reaction in the secondary high-temperature reaction zone and the high-temperature reaction zone in sequence.

6. In the invention, when the second reaction regeneration system is provided with a reactor with upper and lower subareas, the temperatures of the second regenerants introduced into different reaction zones of the reactor through the second regenerator can be the same or different; the second regenerator can adopt single-stage regeneration or multi-stage regeneration when being implemented, preferably adopt the two-stage regeneration form of upper and lower series connection used in the embodiment, the second spent catalyst from the second stripping section firstly enters a first-stage regeneration zone from the lower part of the second regenerator, contacts and reacts with the coke-burning air, flows upwards and enters a second-stage regeneration zone to be regenerated continuously, and supplements fuel in the first-stage regeneration zone or the second-stage regeneration zone to realize regenerator heat supplement; in the practice of the present invention, the upper regenerant is from the second regeneration zone and the lower regenerant is either from the second regeneration zone or from the first regeneration zone.

7. In the first reaction regeneration system, the mass ratio of the steam used by the first reactor to the heavy components of the crude oil is 5-20%, in the second reaction regeneration system, the mass ratio of the steam supplemented to the second reactor to the heavy components of the crude oil is 5-30%, and the mass ratio of the steam to the heavy components of the crude oil in the reaction process of the second reaction regeneration system is 15-50%; when the second reaction regeneration system is provided with a reactor with an upper subarea and a lower subarea, the steam supplemented to the second reaction regeneration system is supplemented in the secondary high-temperature reaction zone or is supplemented in the secondary high-temperature reaction zone and the high-temperature reaction zone respectively.

8. And (3) supplementing the heavy cycle oil or the heavy oil to the reactor before the outlet of the second reactor and/or the third reactor, so as to realize the quenching of the reaction product and supplement heat through the heavy cycle oil or the heavy oil green coke.

9. The treatment of the product of the second reaction system after flowing out of the second settler is a conventional engineering process, which relates to product quenching, heat exchange, fractionation and the like, if a steam generator can be arranged at the outlet of the second settler of the second reaction regeneration system, steam is generated by utilizing the heat of high-temperature product material flow, and the engineering design unit of the steam generator is mastered; or the low-temperature medium can be directly mixed with the product material flow to realize the quenching and cooling of the product; as is known to the engineer.

Effects of the invention

The invention provides a method for preparing ethylene and propylene by gradual temperature rise, two-stage or three-stage temperature gradient dual catalysis and gas phase relay conversion based on a catalytic cracking mechanism. As is well known to those skilled in the art, the heavy oil catalytic cracking process can be regarded as a parallel sequential reaction, heavy oil macromolecules (C18 or more) are firstly cracked to generate middle molecular (C5-C12) products such as gasoline, diesel oil and the like, and the lower cracking temperature can highlight the catalytic cracking reaction, generally 490-530 ℃; part of gasoline and diesel oil is cracked into C3-C8 at 530-600 deg.c; at higher temperature, 600-750 ℃, C3-C8 will further crack into C1, C2, C3 small molecule products. The invention follows the reaction rule and is provided with a plurality of stages of temperature gradients which are gradually heated in series: a low temperature zone, a high temperature zone or a low temperature zone, a sub-high temperature zone and a high temperature zone; simultaneously, proper special catalysts are respectively prepared for low-temperature cracking and high-temperature cracking, a double reaction system is arranged, and double catalysts circulate to strive for exerting the maximum effectiveness of the catalysts; the raw material gas phase relay also provides heat for the second reaction regeneration system to make up for the heat deficiency. The invention reduces the low-value target product on the premise of lower energy consumption, in the method, the crude oil is firstly divided into two parts of light component with low boiling point and heavy component with high boiling point, the heavy component of the crude oil is subjected to multiple catalytic conversion reactions in two reaction regeneration systems, different catalysts can be used according to specific feeding properties and product requirements, thus increasing the selectivity and improving the efficiency, for example, the heavy component of the crude oil can be subjected to decarburization, demetalization and heavy component macromolecule catalytic conversion in a first reaction regeneration system, and the catalyst suitable for micromolecule reaction is used in a second reaction regeneration system for further catalytic conversion to produce chemical raw materials such as low-carbon olefin and the like. In addition, all or part of fractions discharged from the first reaction regeneration system can directly enter the second reaction regeneration system in a gaseous state to provide more heat for the second reaction regeneration system, so that the requirement on heat supply capacity is reduced, the problem of insufficient heat caused by insufficient coke generation of the second reaction regeneration system is solved, the method of cooling and separating firstly and then preheating again and returning to the reactor is changed, the equipment investment of the device can be saved, and the energy consumption is reduced.

Description of the drawings:

FIG. 1 is a schematic process diagram according to one embodiment of the present invention;

FIG. 2 is a schematic process diagram according to a second embodiment of the present invention;

FIG. 3 is a schematic diagram of a third process according to an embodiment of the present invention;

FIG. 4 is a schematic diagram of a fourth process of the present invention;

FIG. 5 is a schematic diagram of a fifth process according to an embodiment of the present invention;

FIG. 6 is a schematic diagram of a sixth process of an embodiment of the present invention;

FIG. 7 is a schematic diagram of a seventh process according to an embodiment of the present invention;

FIG. 8 is a schematic view of an eighth process of an embodiment of the present invention;

the numbering marks in the figure are as follows:

r10 first reactor; r11 first catalyst pre-lift gas; a first catalyst pre-lift gas inlet of R11A, a heavy component of R12 crude oil (or a high boiling component separated from crude oil or a high boiling component separated from a primary distillation tower or a flash distillation tower), a reaction raw material inlet of a first reactor of R12A, and a component after hydrogenation of the heavy component of the R12H crude oil (or a high boiling component in the hydrotreated crude oil); the system comprises R13 crude oil heavy component atomized steam, R14 first reaction system product, R14A first reaction gas product outlet, R14G first reaction system product light component, R14L first reaction system product liquid heavy component, R14L2 recycle oil, R14LH first reaction system product liquid heavy component hydrogenated component, R15 first regeneration slide valve, R15A first reactor regenerant inlet, R16 first standby slide valve, R16A first standby riser and R17 first reaction zone;

s10 first stripping section, S11 first stripping member;

a D10 first settler, a D11 first cyclone;

g10 first regenerator, G11 catalyst regeneration gas, G11A first regeneration gas inlet, G12A first regenerant inlet, G14 first regeneration standpipe (first regenerated catalyst transfer line), G14A first regenerant outlet; g15 first regenerator dilute phase zone, G16 first regenerator cyclone, G17 first regenerator burnt flue gas, G17A first flue gas outlet;

r20 second reactor, R20A second reaction zone, R21 second reactor make-up steam, R22 upper regenerant slide valve, R22A upper regenerated catalyst inlet, R23 high temperature reaction zone make-up steam, R24 second reaction system product, R24A second regenerant inlet or lower regenerant inlet, R25 second regenerated slide valve or lower regenerated slide valve, R25A second regenerant inlet or lower regenerant inlet, R26 second regenerant valve, R26A second spent riser or second spent catalyst transfer pipe, R27 second high temperature reaction zone, R28 high temperature reaction zone;

r30 third reactor (crude oil light component reactor, crude oil separated low boiling point component reactor or naphtha cracking reactor); r31 third reactor steam, R35 third regenerant slide valve, R35A second regenerant iii inlet; a hydrogenation reactor for heavy components of R50 crude oil; r60 hydrogenation reactor;

g20 second regenerator, G21 charring air (second regenerator charring air), G21A charring gas inlet, G22 upper regeneration standpipe, G22A upper regenerant outlet, G24 second regeneration standpipe (second regeneration catalyst delivery pipe or lower regeneration standpipe), G24A second regenerant outlet or lower regenerant outlet, G25 second regenerator dilute phase zone, G27 charred flue gas, G27A second flue gas outlet, G28 fuel oil; g34 third regenerating riser (second regenerant III catalyst conveying pipe or naphtha cracking reactor regenerant riser), G34A second regenerant III outlet (naphtha cracking reactor regenerant outlet);

s20 second stripping section, S21 second stripping section components;

d20 second settler;

a T00 crude oil separation tower or flash tower, a T10 first reaction system product heavy component separation tower, a T20 fractionating tower and a T30 second fractionating tower; a0 crude oil heating furnace or heat exchanger, A1 stream heat exchanger, A2 crude oil heavy component heating heat exchanger (or crude oil separation tower bottom product heat exchanger), B steam generator;

f0 crude oil, F0G crude oil light components (or low boiling point components separated from the crude oil or non-condensable gas and naphtha components separated from the crude oil), F3 water, F4 steam, F21 liquefied gas and dry gas products, F22 gasoline components, F23 Light Cycle Oil (LCO) components and F24 heavy components; h₂Hydrogen gas; LS low-pressure steam;

TIC temperature display control.

The specific implementation mode is as follows:

the technical solutions of the present invention are described below with specific examples, but the scope of the present invention is not limited thereto.