CN217351264U

CN217351264U - Device for preparing olefin and aromatic hydrocarbon by crude oil classification processing

Info

Publication number: CN217351264U
Application number: CN202220937551.0U
Authority: CN
Inventors: 王庆元; 任鹏; 陈树群; 黄云; 孙涛
Original assignee: Spang Technology Co ltd
Current assignee: Spang Technology Co ltd
Priority date: 2022-04-21
Filing date: 2022-04-21
Publication date: 2022-09-02
Anticipated expiration: 2032-04-21

Abstract

The utility model provides a device for preparing olefin and aromatic hydrocarbon by crude oil classification processing, which comprises a crude oil cutting unit, a fluidization cracking unit and a hydropyrolysis unit, wherein the crude oil cutting unit sequentially comprises a flash tower and aromatic hydrocarbon-alkane separation equipment; the light component outlet of the flash tower is connected with the fluidized cracking unit, the middle component outlet and the heavy component outlet of the flash tower are connected with the aromatic hydrocarbon-alkane separation device, the alkane-rich outlet of the aromatic hydrocarbon-alkane separation device is connected with the fluidized cracking unit, the aromatic hydrocarbon-rich outlet is connected with the hydropyrolysis unit, and one outlet of the hydropyrolysis unit is connected with the fluidized cracking unit. The utility model divides the crude oil into light components, rich alkane and rich arene according to the characteristics of the crude oil, and then selects a proper processing device to produce alkene and arene according to the characteristics of each component, thereby fully improving the yield of the crude oil for producing alkene and arene chemicals and improving the utilization value; the device has the advantages of simple structure, short flow, strong adaptability to raw materials and strong application value.

Description

Device for preparing olefin and aromatic hydrocarbon by crude oil classification processing

Technical Field

The utility model belongs to the technical field of petroleum processing, a device of alkene and arene is prepared in categorised processing of crude oil is related to.

Background

The traditional petrochemical industry is mostly of an oil refining type, a processing route is mainly based on a large-scale normal pressure reduction device, a main line is used for producing clean fuel oil and improving the quality of product oil, chemical products such as olefin and aromatic hydrocarbon are byproducts, the production proportion is low and is only 5-10%, along with the development and change of fuel and petrochemical markets, the demand on chemical raw materials is continuously increased and becomes a main driving force for the increase of the demand on crude oil, and the chemical products produced from the crude oil become one of main means for transformation upgrading, quality improvement and efficiency improvement of petroleum refining enterprises, so that the technology for producing the chemical products by the crude oil in a maximized mode is necessarily researched.

At present, a crude oil refining type enterprise generally adds an additional process device on an oil refining plate device, such as hydrocracking, converts a heavy product into a light product, and then passes through olefin cracking, reforming extraction and other devices to realize an integrated production mode of refining oil, ethylene, propylene and aromatic hydrocarbon, wherein the yield of chemicals accounts for about 50% at this time, and still needs to be further improved; if an atmospheric and vacuum distillation device is omitted and the steam cracking is adopted to directly realize the conversion of crude oil to produce ethylene and propylene, although the yield of chemicals can be improved, the technology has the defects of high reaction temperature, high energy consumption, low comprehensive efficiency and the like, the requirement on raw materials is higher, heavy components need to be converted into light components, and the device cannot be effectively simplified.

CN 113025378A discloses a crude oil processing method and system for a system for producing more olefins, the method comprises: the crude oil and steam enter a flash separator for first separation, and light phase components and heavy phase components are separated; carrying out second separation on the light phase component to separate a non-aromatic hydrocarbon component and an aromatic hydrocarbon component; subjecting the non-aromatic components to steam cracking to obtain ethylene, propylene, steam cracked heavy oil and a first C4-C5 component; carrying out catalytic cracking on the heavy phase component to obtain propylene, ethylene-rich gas, catalytic cracking slurry oil and a second C4-C5 component; carrying out hydrocracking treatment on the steam cracking heavy oil and/or the catalytic cracking slurry oil to obtain hydrogenated wax oil, and then carrying out catalytic cracking on the hydrogenated wax oil; the method aims at the problems that the separation temperature of the crude oil is high, so that the light and heavy components in the crude oil are distributed unevenly, the subsequent treatment difficulty is high, the separated non-aromatic components still adopt the traditional steam cracking mode, the reaction temperature is high, and the comprehensive efficiency is low.

CN 113817503a discloses a combined process method for preparing chemicals from crude oil, which comprises the following steps: firstly, carrying out hydrofining on the crude oil to remove S, N, metal and other impurities to obtain refined crude oil; the refined crude oil enters a crude oil adsorption separation unit, and a crude oil non-aromatic hydrocarbon component and a crude oil aromatic hydrocarbon component are obtained under the action of an adsorbent; aiming at the differences of the composition and properties of crude oil non-aromatic hydrocarbon components and crude oil aromatic hydrocarbon components, different processing modes are respectively adopted, the crude oil non-aromatic hydrocarbon components are subjected to olefin yield increase unit and gasoline and diesel oil hydrofining unit to produce low-carbon olefin to the maximum extent, the crude oil aromatic hydrocarbon components are subjected to aromatic hydrocarbon component cutting unit, aromatic hydrocarbon yield increase unit and needle coke yield increase unit to produce low-carbon aromatic hydrocarbon to the maximum extent, and products such as needle coke are produced as a byproduct; the method adopts a crude oil adsorption separation unit to separate aromatic hydrocarbon components and non-aromatic hydrocarbon components, but has the disadvantages of large crude oil treatment capacity, slow adsorption operation, large equipment volume and adsorbent consumption, high cost, low treatment efficiency and numerous subsequent steps for producing chemicals.

In summary, for the devices and processes for preparing chemicals by classifying and processing crude oil, especially for preparing olefin and aromatic hydrocarbon products, appropriate separation devices and processes are selected according to the component characteristics of crude oil, so that the separation efficiency is improved, the subsequent production of chemicals is facilitated, the production devices are simplified, and the yield of chemicals prepared from crude oil is improved.

SUMMERY OF THE UTILITY MODEL

Problem to prior art exists, the utility model aims to provide a device of alkene and arene is prepared in categorised processing of crude oil, the device is cut apart into light component, rich alkane and rich arene component with it according to the characteristic of crude oil, selects suitable processing equipment and technology to produce alkene, arene according to the characteristics of each component again, fully improves the yield of chemicals such as crude oil production alkene, arene, realizes the refining type production of crude oil, improves its using value.

To achieve the purpose, the utility model adopts the following technical proposal:

the utility model provides a device for preparing olefin and aromatic hydrocarbon by crude oil classification processing, which comprises a crude oil cutting unit, a fluidization cracking unit and a hydropyrolysis unit, wherein the crude oil cutting unit sequentially comprises a flash tower and an aromatic hydrocarbon-alkane separation device, and the fluidization cracking unit comprises a cascade riser reactor; the light component outlet of the flash tower is connected with the inlet of the fluidized cracking unit, the middle component outlet and the heavy component outlet of the flash tower are connected with the inlet of the aromatic hydrocarbon-alkane separation device, the alkane-rich outlet of the aromatic hydrocarbon-alkane separation device is connected with the inlet of the fluidized cracking unit, the aromatic hydrocarbon-rich outlet of the aromatic hydrocarbon-alkane separation device is connected with the inlet of the hydropyrolysis unit, and one outlet of the hydropyrolysis unit is connected with the inlet of the fluidized cracking unit.

The utility model discloses in, the process route of producing chemicals by crude oil is the development direction that crude oil utilized at present, the device passes through the setting of crude oil segmentation unit, especially flash separation and arene-alkane separation two-stage splitter's setting, fully cuts apart the component that is fit for different technology in the crude oil and handles, according to the principle that suitable fragrant then fragrant, suitable alkene then alkene, adopt the fluidization schizolysis unit with light component and rich alkane mainly to produce alkene, adopt the hydropyrolysis unit mainly to produce arene with rich arene, some other products can also utilize equipment in the device to handle once more, help realizing turning into alkene and arene products with crude oil is whole, improve its value of utilization; the device has the advantages of simple structure, shorter flow, lower cost, strong adaptability to raw materials and stronger industrial popularization and application value.

Following conduct the utility model discloses preferred technical scheme, nevertheless do not conduct the utility model provides a technical scheme's restriction, through following technical scheme, can reach and realize better the utility model discloses a technical purpose and beneficial effect.

As the utility model discloses preferred technical scheme, the flash column includes first flash column and second flash column, the top export of first flash column links to each other with the entry of fluidization cracking unit, the bottom export of first flash column links to each other with the entry of second flash column, the top export and the bottom export of second flash column all link to each other with arene-alkane splitter's entry.

Preferably, the arene-alkane separating device comprises a first arene-alkane separating device and a second arene-alkane separating device, the intermediate component outlet of the flash tower is connected with the inlet of the first arene-alkane separating device, and the heavy component outlet of the flash tower is connected with the inlet of the second arene-alkane separating device.

Preferably, the first alkane-rich outlet of the first aromatic hydrocarbon-alkane separation device and the second alkane-rich outlet of the second aromatic hydrocarbon-alkane separation device are both connected with the inlet of the fluidized cracking unit, and the first aromatic hydrocarbon-rich outlet of the first aromatic hydrocarbon-alkane separation device and the second aromatic hydrocarbon-rich outlet of the second aromatic hydrocarbon-alkane separation device are both connected with the inlet of the hydropyrolysis unit.

Preferably, the aromatics-paraffins separation apparatus independently comprises an extractive separation column.

The utility model discloses in, the crude oil cut apart is the prerequisite that realizes the chemical production, its separation degree can greatly influence alkene, the yield of aromatic hydrocarbon product, therefore adopt two-stage splitter, adopt flash distillation splitter earlier, specifically select two-stage flash column, according to the selection of process conditions, obtain the light component at first flash column top of the tower, the second flash column obtains intermediate component and heavy ends, adopt the extraction separator again, utilize equipment and treat the characteristic of separation component, with alkane and aromatic hydrocarbon separation in intermediate component and the heavy ends, be convenient for follow-up classification processing.

As the utility model discloses preferred technical scheme, the device still includes the pre-heater, the export of pre-heater links to each other with flash column's entry.

Preferably, the preheater comprises a heat exchanger and/or a heating furnace, and when the heat exchanger is selected, the crude oil is used as a cold flow, and the outlet of the cold flow is connected with the inlet of the flash tower.

Preferably, the device also comprises a gasification heating furnace, wherein the inlet of the gasification heating furnace is connected with the alkane-rich outlet of the aromatic hydrocarbon-alkane separation device, and the outlet of the gasification heating furnace is connected with the inlet of the fluidized cracking unit.

Preferably, the gasification heating furnace is provided with a fuel inlet and a flue gas outlet, and the flue gas outlet of the gasification heating furnace is connected with the heat flow inlet of the heat exchanger.

In the utility model, the crude oil flash separation needs to reach a certain temperature, in order to avoid the influence of the temperature rise in the flash tower due to the over-low crude oil temperature, the crude oil is preheated to reach the separation temperature, the heat source can select the hot flue gas of the heating furnace or the reaction heat in the device, and the heat utilization rate in the system is improved; the paraffin-rich component separated by the aromatic hydrocarbon-paraffin separation device needs to be heated and converted into gas phase before fluidized cracking, so a gasification heating furnace is arranged, and the paraffin-rich component is heated by utilizing the combustion heat of fuel gas to realize preheating of the fluidized cracking raw material.

As a preferred embodiment of the present invention, the riser reactor in the fluidized cracking unit comprises at least two stages, such as two stages, three stages or four stages.

Preferably, the riser reactor comprises a primary riser reactor and a secondary riser reactor.

Preferably, the hydrogen-rich product of the fluidized cracking unit is passed into the inlet of the hydropyrolysis unit.

The utility model discloses in, among the cascade fluidization cleavage reaction, rich alkane and light component heat up gradually under the catalyst effect, generate alkene products and hydrogen such as ethylene, propylene, and hydrogen can be used to the raw materials of the hydropyrolysis reaction, also can generate the pyrolysis oil simultaneously, including the aromatic hydrocarbon component, carry out subsequent aromatic hydrocarbon separation.

As the preferred technical scheme of the utility model, the hydropyrolysis unit includes at least one stage of hydropyrolysis reactor, such as one stage, two stages or tertiary etc., preferably two stages.

Preferably, the hydropyrolysis unit comprises a primary hydropyrolysis reactor and a secondary hydropyrolysis reactor.

Preferably, the outlet for non-aromatic products of the hydropyrolysis unit is connected to the inlet of the fluidized cracking unit.

The utility model discloses in, the hydropyrolysis unit is with being rich in the aromatic hydrocarbon component under hydrogen and catalyst existence, takes place polycyclic aromatic hydrocarbon cracking reaction, and the reaction product obtains the aromatic hydrocarbon product and the non-aromatic hydrocarbon product that contain benzene, toluene, xylol through the separation, and the aromatic hydrocarbon product can send out the device and further separate, and the non-aromatic hydrocarbon product then returns fluidization cracking unit, mixes through gasification heating furnace heating with being rich in the alkane to the form of gasification steam gets into the riser reactor of establishing ties.

The utility model also provides a method for adopt above-mentioned device to prepare alkene and arene, the method includes following step:

(1) carrying out flash separation on the crude oil to obtain a light component, an intermediate component and a heavy component, and separating the intermediate component and the heavy component into an alkane-rich component and an aromatic hydrocarbon-rich component respectively;

(2) carrying out cascade fluidization cracking reaction on the light component and the alkane-rich component obtained in the step (1) to obtain cracked gas and cracked oil, wherein the cracked gas comprises olefin and hydrogen;

(3) and (3) carrying out hydropyrolysis reaction on the aromatic hydrocarbon-rich component obtained in the step (1) to obtain an aromatic hydrocarbon product and a non-aromatic hydrocarbon product, and returning the non-aromatic hydrocarbon product to the step (2) to carry out cascade fluidization cracking reaction.

As the preferable technical proposal of the utility model, the crude oil is preheated before the flash separation in the step (1).

Preferably, the crude oil is preheated with hot flue gas of a gasification furnace.

Preferably, the flash separation in step (1) comprises two-stage flash separation, namely first-stage flash separation and second-stage flash separation.

Preferably, the feed temperature of the primary flash separation is 300-350 ℃, such as 300 ℃, 310 ℃, 320 ℃, 330 ℃, 340 ℃ or 350 ℃ and the like; the pressure is 0 to 50kPaG, for example, 0kPaG, 10kPaG, 20kPaG, 30kPaG, 40kPaG or 50kPaG, etc., but the pressure is not limited to the values listed, and other values not listed in the respective numerical ranges are also applicable.

Preferably, light components are obtained at the top of the tower during the first-stage flash separation, and the components at the bottom of the tower are continuously subjected to second-stage flash separation.

Preferably, the feed temperature of the secondary flash separation is 320-400 ℃, such as 320 ℃, 340 ℃, 350 ℃, 360 ℃, 380 ℃ or 400 ℃ and the like; the pressure is 2 to 20kPaA, for example, 2kPaA, 5kPaA, 8kPaA, 10kPaA, 15kPaA or 20kPaA, but the pressure is not limited to the above-mentioned values, and other values not shown in the respective ranges are also applicable.

Preferably, the intermediate component is obtained at the top of the tower during the secondary flash separation, and the heavy component is obtained at the bottom of the tower.

The utility model discloses in, the selection of flash distillation temperature and pressure is mainly in order to realize the initial gross separation of crude oil component, separates out light component earlier when one-level flash separation, then separates into intermediate constituent and heavy ends when second grade flash separation, and both further separation be for richening alkane component and richening arene component after again, wherein light component mainly includes alkane, alkene and the cycloalkane of C1 ~ C6.

As the preferable technical proposal of the utility model, the separation mode of the intermediate component and the heavy component in the step (1) independently comprises solvent extraction.

Preferably, the intermediate component is separated into a first alkane-rich and a first aromatic-rich, and the heavy component is separated into a second alkane-rich and a second aromatic-rich.

Preferably, the extractant used for solvent extraction of the intermediate component comprises any one of furfural, N-methylpyrrolidone, 2-pyrrolidone, morpholine, sulfolane, dimethyl sulfoxide, a di-or tri-glycol ether, or a combination of at least two of these, typical but non-limiting examples being: combinations of furfural and N-methylpyrrolidone, sulfolane and dimethyl sulfoxide, diethylene glycol ether and triethylene glycol ether, 2-pyrrolidone, morpholine and sulfolane, and the like.

Preferably, the extractant used for the heavy ends solvent extraction comprises any one of propane, butane, pentane, hexane, cyclohexane or heptane, or a combination of at least two of these, typical but non-limiting examples being: a combination of propane and butane, a combination of hexane and cyclohexane, a combination of propane, butane and pentane, a combination of pentane, hexane, cyclohexane and heptane, and the like.

The utility model discloses in, alkane component and the aromatic hydrocarbon component in intermediate component and the heavy ends are because molecular weight differs little, cause the boiling point to be close, are difficult to direct flash separation, therefore select suitable separation mode according to the characteristic of component.

As the preferable technical proposal of the utility model, the alkane-rich component in the step (2) is firstly heated to form alkane-rich gas and then mixed with the light component.

Preferably, the alkane-rich component comprises predominantly alkanes of C6 and above C6.

Preferably, the first alkane-rich component comprises alkanes from C6 to C18, and the second alkane-rich component comprises alkanes above C18.

Preferably, the heating of the alkane rich gas is conducted by radiation heat transfer from the combustion of the fuel, and the flue gas after radiation heat transfer is used for preheating the crude oil in the step (1).

Preferably, the cascade fluidized cracking reaction of step (2) includes a first-stage fluidized cracking reaction and a second-stage fluidized cracking reaction.

Preferably, the temperature of the first fluidized cracking reaction in step (2) is 500 to 650 ℃, for example, 500 ℃, 520 ℃, 550 ℃, 580 ℃, 600 ℃, 620 ℃ or 650 ℃, but is not limited to the values listed, and other values not listed in the range of the values are also applicable.

Preferably, the time of the first-stage fluidized cracking reaction in step (2) is 0.5 to 2s, such as 0.5s, 0.8s, 1s, 1.2s, 1.5s, 1.8s, or 2s, but is not limited to the recited values, and other values not recited in the range of the values are also applicable.

Preferably, the temperature of the secondary fluidized cracking reaction in step (2) is 650 to 850 ℃, for example 650 ℃, 700 ℃, 750 ℃, 800 ℃ or 850 ℃, but not limited to the recited values, and other values not recited in the range of the values are also applicable.

Preferably, the time of the secondary fluidized cracking reaction in step (2) is 0.5 to 2s, such as 0.5s, 0.8s, 1s, 1.2s, 1.5s, 1.8s or 2s, but not limited to the recited values, and other values not recited in the range of the values are also applicable.

Preferably, the pressure of the fluidized cracking reaction in step (2) is 0.1 to 0.51MPaG, such as 0.1MPaG, 0.15MPaG, 0.2MPaG, 0.25MPaG, 0.3MPaG, 0.35MPaG, 0.4MPaG, 0.45MPaG, or 0.51MPaG, but not limited to the enumerated values, and other values not enumerated within the range of values are also applicable.

Preferably, the olefins of step (2) comprise mainly ethylene and propylene.

Preferably, the product of the fluidized cracking reaction in the step (2) further comprises a C4 fraction and a C5 fraction, and the C4 fraction and the C5 fraction are a mixture of alkane and alkene.

In the utility model discloses in, the C4 fraction is mainly with butane, 1-butene, isobutene, 2-butene and butadiene, and C5 fraction includes the catenation of 5 carbon's alkane, monoolefin and polyene, cyclic compound.

Preferably, one of the components of the cracked gas separated in the step (2) is hydrogen-rich gas, and the hydrogen-rich gas is used as a raw material for the hydropyrolysis reaction in the step (3).

Preferably, the volume fraction of hydrogen in the hydrogen-rich gas is not less than 90%, such as 90%, 92%, 94%, 95%, 96%, or 98%, but is not limited to the recited values, and other unrecited values within the range are equally applicable.

Preferably, the fluidized cracking reaction in the step (2) adopts catalytic cracking with a catalyst or thermal cracking with an inert heat carrier, and includes a ZSM-5 molecular sieve catalyst, a ZSM-11 molecular sieve catalyst, a REY type molecular sieve catalyst, a USY type molecular sieve catalyst, a REHY type molecular sieve catalyst, alumina, silicate, and the like.

The utility model discloses in, adopt the cascade riser reactor, can effectively improve the yield of alkene result, and compare steam cracking technology, adopt the utility model provides a fluidization schizolysis can reduce device investment and running cost, reduces the energy consumption, improves alkene result yield.

As the preferable technical proposal of the utility model, the step (3) of the hydropyrolysis reaction comprises a first-stage hydropyrolysis reaction and a second-stage hydropyrolysis reaction.

Preferably, the temperature of the primary hydropyrolysis reaction is 380 to 465 ℃, such as 380 ℃, 400 ℃, 420 ℃, 440 ℃, 450 ℃ or 465 ℃ and the like, but is not limited to the recited values, and other values not recited in the range of values are equally applicable.

Preferably, the temperature of the secondary hydropyrolysis reaction is 450 to 550 ℃, for example 450 ℃, 460 ℃, 480 ℃, 500 ℃, 520 ℃, 540 ℃ or 550 ℃, but is not limited to the recited values, and other values not recited in the range of the values are also applicable.

Preferably, the pressure of the primary hydropyrolysis reaction and the secondary hydropyrolysis reaction is independently 10 to 30MPaG, such as 10MPaG, 15MPaG, 20MPaG, 25MPaG or 30MPaG, but not limited to the recited values, and other values not recited in the range of values are also applicable.

Preferably, the primary hydropyrolysis and the secondary hydropyrolysis have a hydrogen to oil ratio of independently 500 to 2000, such as 500, 800, 1000, 1200, 1500, 1800 or 2000, but not limited to the recited values, and other values not recited in this range are equally applicable.

Preferably, the volume space velocity of the primary hydropyrolysis reaction and the secondary hydropyrolysis reaction is 0.5-2.0 h independently ^-1 E.g. 0.5h ^-1 、1.0h ^-1 、1.2h ^-1 、1.5h ^-1 、1.8h ^-1 Or 2.0h ^-1 And the like, but are not limited to the recited values, and other values not recited within the numerical range are also applicable.

Preferably, the reaction product of the primary hydropyrolysis is subjected to a secondary hydropyrolysis reaction.

Preferably, the aromatic hydrocarbon product in the step (3) comprises benzene, toluene and xylene, and the aromatic hydrocarbon product is mixed with the pyrolysis oil obtained in the step (2) to be used as an aromatic hydrocarbon raw material.

Preferably, the product of the hydropyrolysis reaction of step (3) further comprises a gas phase component comprising H ₂ S、NH ₃ 、H ₂ And CH ₄ Besides, the hydrocarbon additive also comprises a plurality of gas-phase hydrocarbons in C1-C4.

In the utility model, the hydropyrolysis process is based on the principle of directional conversion of the material structure, adopts the molecular segmentation technology to carry out the fractional hydropyrolysis, firstly carries out the hydropyrolysis of macromolecular aromatic hydrocarbon into 2-4 ring aromatic hydrocarbon through the primary hydropyrolysis reaction, and then carries out the cracking of the secondary hydropyrolysis reaction into mixed aromatic hydrocarbon rich in BTX; the process can directly convert the rich aromatic hydrocarbon into the light aromatic hydrocarbon without catalytic reforming, and has the advantages of high aromatic hydrocarbon yield and low energy consumption of a device.

Compared with the prior art, the utility model discloses following beneficial effect has:

(1) the device adopts two-stage separation equipment to divide the crude oil into light components, rich alkane and rich aromatic hydrocarbon components according to the characteristics of the crude oil, then selects a proper processing device according to the characteristics of each component, adopts the fluidized cracking unit to mainly produce olefin with the light components and the rich alkane, adopts the hydropyrolysis unit to mainly produce aromatic hydrocarbon with the rich aromatic hydrocarbon, fully improves the yield of chemicals such as the crude oil production olefin and the aromatic hydrocarbon, the yield of olefin products can reach more than 53 percent, the yield of aromatic hydrocarbon products can reach more than 30 percent, and the utilization value of the device is improved;

(2) device simple structure, the flow is shorter, and the cost is lower, to the strong adaptability of raw materials, has stronger industrial popularization using value.

Drawings

FIG. 1 is a schematic diagram of the structural connection of an apparatus for producing olefins and aromatics by classification processing of crude oil provided in example 1 of the present invention;

the system comprises a preheater 1, a flash tower 2, a first flash tower 21, a second flash tower 22, a first aromatic hydrocarbon-alkane separation device 3, a second aromatic hydrocarbon-alkane separation device 4, a gasification heating furnace 5, a fluidized cracking unit 6 and a hydropyrolysis unit 7.

Detailed Description

To better explain the utility model, the technical proposal of the utility model is convenient to understand, and the utility model is further explained in detail below. However, the following embodiments are only simple examples of the present invention, and do not represent or limit the scope of the present invention, which is defined by the appended claims.

The utility model provides a device for preparing olefin and aromatic hydrocarbon by crude oil classification processing, which comprises a crude oil cutting unit, a fluidization cracking unit 6 and a hydropyrolysis unit 7, wherein the crude oil cutting unit comprises a flash tower 2 and an aromatic hydrocarbon-alkane separation device in sequence, and the fluidization cracking unit 6 comprises a cascade riser reactor; the light component outlet of the flash tower 2 is connected with the inlet of the fluidized cracking unit 6, the middle component outlet and the heavy component outlet of the flash tower 2 are connected with the inlet of the aromatic hydrocarbon-alkane separation device, the alkane-rich outlet of the aromatic hydrocarbon-alkane separation device is connected with the inlet of the fluidized cracking unit 6, the aromatic hydrocarbon-rich outlet of the aromatic hydrocarbon-alkane separation device is connected with the inlet of the hydropyrolysis unit 7, and one outlet of the hydropyrolysis unit 7 is connected with the inlet of the fluidized cracking unit 6.

The following are typical but non-limiting examples of the present invention:

example 1:

the embodiment provides a device for preparing olefin and aromatic hydrocarbon by classifying and processing crude oil, the structural connection schematic diagram of the device is shown in fig. 1, and the device comprises a crude oil dividing unit, a fluidized cracking unit 6 and a hydropyrolysis unit 7, wherein the crude oil dividing unit sequentially comprises a flash tower 2 and an aromatic hydrocarbon-alkane separation device, and the fluidized cracking unit 6 comprises a cascade riser reactor; the light component outlet of the flash tower 2 is connected with the inlet of the fluidized cracking unit 6, the middle component outlet and the heavy component outlet of the flash tower 2 are connected with the inlet of the aromatic hydrocarbon-alkane separation device, the upper outlet of the aromatic hydrocarbon-alkane separation device is connected with the inlet of the fluidized cracking unit 6, the lower outlet of the aromatic hydrocarbon-alkane separation device is connected with the inlet of the hydropyrolysis unit 7, and one outlet of the hydropyrolysis unit 7 is connected with the inlet of the fluidized cracking unit 6.

The flash tower 2 comprises a first flash tower 21 and a second flash tower 22, wherein the top outlet of the first flash tower 21 is connected with the inlet of the fluidized cracking unit 6, the bottom outlet of the first flash tower 21 is connected with the inlet of the second flash tower 22, and the top outlet and the bottom outlet of the second flash tower 22 are both connected with the inlet of the aromatic hydrocarbon-alkane separation equipment.

The arene-alkane separating device comprises a first arene-alkane separating device 3 and a second arene-alkane separating device 4, an intermediate component outlet of the flash tower 2 is connected with an inlet of the first arene-alkane separating device 3, and a heavy component outlet of the flash tower 2 is connected with an inlet of the second arene-alkane separating device 4.

The first alkane-rich outlet of the first aromatic hydrocarbon-alkane separation device 3 and the second alkane-rich outlet of the second aromatic hydrocarbon-alkane separation device 4 are both connected with the inlet of the fluidized cracking unit 6, and the first aromatic hydrocarbon-rich outlet of the first aromatic hydrocarbon-alkane separation device 3 and the second aromatic hydrocarbon-rich outlet of the second aromatic hydrocarbon-alkane separation device 4 are both connected with the inlet of the hydropyrolysis unit 7.

The aromatic hydrocarbon-alkane separation equipment is an extraction separation tower.

The device also comprises a preheater 1, wherein the outlet of the preheater 1 is connected with the inlet of the flash tower 2.

The preheater 1 is a heat exchanger, and a cold flow outlet of the heat exchanger is connected with an inlet of the flash tower 2.

The device also comprises a gasification heating furnace 5, wherein an inlet of the gasification heating furnace 5 is connected with an alkane-rich outlet of the aromatic hydrocarbon-alkane separation equipment, and an outlet of the gasification heating furnace 5 is connected with an inlet of the fluidized cracking unit 6.

The gasification heating furnace 5 is provided with a fuel inlet and a flue gas outlet, and the flue gas outlet of the gasification heating furnace 5 is connected with the heat flow inlet of the heat exchanger.

The riser reactor in the fluidized cracking unit 6 comprises two stages, namely a first-stage riser reactor and a second-stage riser reactor; the hydrogen-rich product of the fluidized cracking unit 6 is passed into the inlet of the hydropyrolysis unit 7.

The hydropyrolysis unit 7 comprises two-stage hydropyrolysis reactors, namely a first-stage hydropyrolysis reactor and a second-stage hydropyrolysis reactor.

The outlet of the non-aromatic products of the hydropyrolysis unit 7 is connected to the inlet of the fluidized cracking unit 6.

Example 2:

the embodiment provides a device for preparing olefins and aromatic hydrocarbons by classifying and processing crude oil, which comprises a crude oil partitioning unit, a fluidized cracking unit 6 and a hydropyrolysis unit 7, wherein the crude oil partitioning unit sequentially comprises a flash tower 2 and an aromatic hydrocarbon-alkane separation device, and the fluidized cracking unit 6 comprises a cascade riser reactor; the light component outlet of the flash tower 2 is connected with the inlet of the fluidized cracking unit 6, the middle component outlet and the heavy component outlet of the flash tower 2 are connected with the inlet of the aromatic hydrocarbon-alkane separation device, the upper outlet of the aromatic hydrocarbon-alkane separation device is connected with the inlet of the fluidized cracking unit 6, the lower outlet of the aromatic hydrocarbon-alkane separation device is connected with the inlet of the hydropyrolysis unit 7, and one outlet of the hydropyrolysis unit 7 is connected with the inlet of the fluidized cracking unit 6.

The preheater 1 is a heating furnace.

The device also comprises a gasification heating furnace 5, wherein the inlet of the gasification heating furnace 5 is connected with the alkane-rich outlet of the aromatic hydrocarbon-alkane separation equipment, and the outlet of the gasification heating furnace 5 is connected with the inlet of the fluidized cracking unit 6.

The gasification heating furnace 5 is provided with a fuel inlet and a flue gas outlet.

The hydropyrolysis unit 7 includes two-stage hydropyrolysis reactors, which are a primary hydropyrolysis reactor and a secondary hydropyrolysis reactor, respectively.

Example 3:

the embodiment provides a device for preparing olefin and aromatic hydrocarbon by classifying and processing crude oil, which comprises a crude oil segmentation unit, a fluidized cracking unit 6 and a hydropyrolysis unit 7, wherein the crude oil segmentation unit sequentially comprises a flash tower 2 and an aromatic hydrocarbon-alkane separation device, and the fluidized cracking unit 6 comprises a cascade riser reactor; the light component outlet of the flash tower 2 is connected with the inlet of the fluidized cracking unit 6, the middle component outlet and the heavy component outlet of the flash tower 2 are connected with the inlet of the aromatic hydrocarbon-alkane separation device, the upper outlet of the aromatic hydrocarbon-alkane separation device is connected with the inlet of the fluidized cracking unit 6, the lower outlet of the aromatic hydrocarbon-alkane separation device is connected with the inlet of the hydropyrolysis unit 7, and one outlet of the hydropyrolysis unit 7 is connected with the inlet of the fluidized cracking unit 6.

The riser reactor in the fluidized cracking unit 6 comprises three stages, namely a first-stage riser reactor, a second-stage riser reactor and a third-stage riser reactor; the hydrogen-rich product of the fluidized cracking unit 6 is passed into the inlet of the hydropyrolysis unit 7.

An outlet of a non-aromatic hydrocarbon product of the hydro-pyrolysis unit 7 is connected with an inlet of the fluidized cracking unit 6, and an outlet pipeline of the aromatic hydrocarbon product of the hydro-pyrolysis unit 7 is converged with an outlet pipeline of a cracked oil product of the fluidized cracking unit 6 and then connected with an aromatic hydrocarbon production device.

Example 4:

this example provides a process for the preparation of olefins and aromatics by means of a crude oil fractionation process, carried out with reference to the apparatus of example 1, comprising the steps of:

(1) preheating the saute medium crude oil by hot flue gas, and then sequentially carrying out two-stage flash separation in a flash tower 2, wherein the feeding temperature of the first-stage flash separation is 320 ℃, the pressure is 25kPaG, the light component is obtained at the top of the tower, the components at the bottom of the tower are continuously subjected to the second-stage flash separation, the feeding temperature of the second-stage flash separation is 360 ℃, the pressure is 10kPaA, the intermediate component is obtained at the top of the tower, and the heavy component is obtained at the bottom of the tower;

the intermediate component and the heavy component are separated by an extraction separator respectively, an extracting agent used for extracting the intermediate component is N-methyl pyrrolidone, the volume ratio of the extracting agent to the intermediate component is 3:1, an extracting agent used for extracting the heavy component is N-hexane, the volume ratio of the extracting agent to the heavy component is 5:1, the intermediate component is separated to obtain first paraffin-rich hydrocarbon and first aromatic hydrocarbon-rich hydrocarbon, and the heavy component is separated to obtain second paraffin-rich hydrocarbon and second aromatic hydrocarbon-rich hydrocarbon;

(2) forming alkane-rich gas by burning fuel gas for supplying heat for the alkane-rich component obtained in the step (1), mixing the alkane-rich gas with the light component for a cascade fluidized cracking reaction, wherein the fluidized cracking reaction is carried out by adopting a two-stage riser reactor, the used catalyst is a ZSM-5 zeolite catalyst, the temperature of the first-stage fluidized cracking reaction is 600 ℃, the time is 1s, the temperature of the second-stage fluidized cracking reaction is 800 ℃, the time is 1.5s, the pressure of the two-stage reaction is 0.25MPa, and cracking gas, a C4 component, a C5 component and cracking oil are obtained, wherein the cracking gas comprises ethylene, propylene and hydrogen-rich gas which is used as a raw material for the hydropyrolysis reaction in the step (3);

(3) carrying out two-stage hydropyrolysis reaction on the aromatic hydrocarbon-rich component obtained in the step (1) by using a hydropyrolysis reactor, wherein the catalyst is a Mo-Ni hydrogenation catalyst, the temperature of the first-stage hydropyrolysis reaction is 440 ℃, the reaction pressure is 22MPaG, the hydrogen-oil ratio is 700, and the volume space velocity is 0.65h ^-1 (ii) a The first stage isThe reaction product of the hydropyrolysis is continuously subjected to secondary hydropyrolysis reaction, the temperature of the secondary hydropyrolysis reaction is 500 ℃, the reaction pressure is 22MPaG, the hydrogen-oil ratio is 1700, and the volume space velocity is 1.0h ^-1 And (3) performing a two-stage hydropyrolysis reaction to obtain an aromatic hydrocarbon product, a non-aromatic hydrocarbon product and fuel gas, wherein the aromatic hydrocarbon product comprises benzene, toluene and xylene, the aromatic hydrocarbon product is mixed with the pyrolysis oil obtained in the step (2) to be used as an aromatic hydrocarbon raw material, and the fuel gas comprises H ₂ S、NH ₃ 、H ₂ And CH ₄ And (3) returning the non-aromatic hydrocarbon products to the step (2) for cascade fluidized cracking reaction.

In this example, the crude oil is subjected to component division, and then to cascade fluidization cracking and hydropyrolysis, so that the crude oil is fully converted into chemicals, the yield of olefin products reaches 56.9%, and the yield of aromatic hydrocarbon products reaches 31.7%.

Example 5:

(1) preheating the Saudi medium crude oil by using hot flue gas, then entering a flash tower 2 to sequentially carry out two-stage flash separation, wherein the feeding temperature of the first-stage flash separation is 300 ℃, the pressure is 0kPaG, the light component is obtained at the top of the tower, the second-stage flash separation is continuously carried out on the components at the bottom of the tower, the feeding temperature of the second-stage flash separation is 340 ℃, the pressure is 2kPaA, the intermediate component is obtained at the top of the tower, and the heavy component is obtained at the bottom of the tower;

the intermediate component and the heavy component are separated by an extraction separator respectively, an extracting agent used for extracting the intermediate component is sulfolane, the volume ratio of the extracting agent to the intermediate component is 3:1, an extracting agent used for extracting the heavy component is n-hexane, the volume ratio of the extracting agent to the heavy component is 3:1, the intermediate component is separated to obtain first paraffin-rich hydrocarbon and first aromatic hydrocarbon-rich hydrocarbon, and the heavy component is separated to obtain second paraffin-rich hydrocarbon and second aromatic hydrocarbon-rich hydrocarbon;

(2) forming alkane-rich gas by burning fuel gas for supplying heat for the alkane-rich component obtained in the step (1), mixing the alkane-rich gas with the light component for a cascade fluidized cracking reaction, wherein the fluidized cracking reaction is carried out by adopting a two-stage riser reactor, the used catalyst is a ZSM-11 zeolite catalyst, the temperature of the first-stage fluidized cracking reaction is 650 ℃, the time is 0.5s, the temperature of the second-stage fluidized cracking reaction is 850 ℃, the time is 0.8s, and the pressure of the two-stage reaction is 0.4MPa, so as to obtain cracking gas, a C4 component, a C5 component and cracking oil, the cracking gas comprises ethylene, propylene and hydrogen-rich gas, and the hydrogen-rich gas is used as a raw material for the hydropyrolysis reaction in the step (3);

(3) carrying out two-stage hydropyrolysis on the aromatic hydrocarbon-rich component obtained in the step (1) by adopting a hydropyrolysis reactor, wherein the catalyst is a Mo-Ni hydrogenation catalyst, the temperature of the first-stage hydropyrolysis is 465 ℃, the reaction pressure is 30MPaG, the hydrogen-oil ratio is 600, and the volume space velocity is 0.6h ^-1 (ii) a The reaction product of the primary hydropyrolysis is continuously subjected to secondary hydropyrolysis reaction, the temperature of the secondary hydropyrolysis reaction is 550 ℃, the reaction pressure is 30MPaG, the hydrogen-oil ratio is 1500, and the volume space velocity is 1.0h ^-1 And (3) obtaining aromatic hydrocarbon products, non-aromatic hydrocarbon products and fuel gas through two-stage hydropyrolysis reaction, wherein the aromatic hydrocarbon products comprise benzene, toluene and xylene, the aromatic hydrocarbon products are mixed with the pyrolysis oil obtained in the step (2) to be used as aromatic hydrocarbon raw materials, and the fuel gas comprises H ₂ S、NH ₃ 、H ₂ And CH ₄ And (3) returning the non-aromatic hydrocarbon product to the step (2) for carrying out the cascade fluidized cracking reaction.

In this embodiment, the crude oil is subjected to component division, and is subjected to cascade fluidized cracking and hydropyrolysis, so that the crude oil is fully converted into chemicals, the yield of olefin products reaches 58.1%, and the yield of aromatic hydrocarbon products reaches 30.9%.

Example 6:

this example provides a process for the preparation of olefins and aromatics by classification processing of crude oil, which is carried out with reference to the apparatus of example 2, and which comprises the following steps:

(1) preheating the Saudi medium crude oil by using a heating furnace, then entering a flash tower 2 to sequentially carry out two-stage flash separation, wherein the feeding temperature of the first-stage flash separation is 350 ℃, the pressure is 50kPaG, the light component is obtained at the top of the tower, the component at the bottom of the tower is continuously subjected to the second-stage flash separation, the feeding temperature of the second-stage flash separation is 400 ℃, the pressure is 20kPaA, the intermediate component is obtained at the top of the tower, and the heavy component is obtained at the bottom of the tower;

the intermediate component and the heavy component are separated by an extraction separator respectively, an extractant used for extracting the intermediate component is diethylene glycol ether, the volume ratio of the extractant to the intermediate component is 4:1, an extractant used for extracting the heavy component is propane, the volume ratio of the extractant to the heavy component is 5:1, the intermediate component is separated to obtain first paraffin-rich hydrocarbon and first aromatic hydrocarbon-rich hydrocarbon, and the heavy component is separated to obtain second paraffin-rich hydrocarbon and second aromatic hydrocarbon-rich hydrocarbon;

(2) forming alkane-rich gas from the alkane-rich component obtained in the step (1) by adopting a fuel gas combustion heat supply mode, mixing the alkane-rich gas with a light component to perform a cascade fluidization cracking reaction, wherein the fluidization cracking reaction is performed by adopting a two-stage riser reactor, the used catalyst is a USY molecular sieve catalyst, the temperature of the first-stage fluidization cracking reaction is 500 ℃, the time is 1.5s, the temperature of the second-stage fluidization cracking reaction is 650 ℃, the time is 2s, and the pressure of the two-stage reaction is 0.5MPa, so that cracking gas, a C4 component, a C5 component and cracking oil are obtained, the cracking gas comprises ethylene, propylene and hydrogen-rich gas, and the hydrogen-rich gas is used as a raw material for the hydropyrolysis reaction in the step (3);

(3) carrying out two-stage hydropyrolysis reaction on the aromatic hydrocarbon-rich component obtained in the step (1) by using a hydropyrolysis reactor, wherein the catalyst is a W-Mo-Ni hydrogenation catalyst, the temperature of the first-stage hydropyrolysis reaction is 380 ℃, the reaction pressure is 10MPaG, the hydrogen-oil ratio is 1000, and the volume space velocity is 0.8h ^-1 (ii) a The primary hydropyrolysis reaction product continues to carry out secondary hydropyrolysis reaction, the temperature of the secondary hydropyrolysis reaction is 450 ℃, the reaction pressure is 15MPaG, the hydrogen-oil ratio is 1800, and the volume space velocity is 1.5h ^-1 And (3) performing a two-stage hydropyrolysis reaction to obtain an aromatic hydrocarbon product, a non-aromatic hydrocarbon product and fuel gas, wherein the aromatic hydrocarbon product comprises benzene, toluene and xylene, the aromatic hydrocarbon product is mixed with the pyrolysis oil obtained in the step (2) to be used as an aromatic hydrocarbon raw material, and the fuel gas comprises H ₂ S、NH ₃ 、H ₂ And CH ₄ And (3) returning the non-aromatic hydrocarbon products to the step (2) for cascade fluidized cracking reaction.

In this embodiment, the crude oil is subjected to component division, and is subjected to cascade fluidized cracking and hydropyrolysis, so that the crude oil is fully converted into chemicals, the yield of olefin products reaches 53.6%, and the yield of aromatic hydrocarbon products reaches 34.5%.

Example 7:

this example provides a process for the preparation of olefins and aromatics by means of a crude oil fractionation process, carried out in accordance with the apparatus of example 2, comprising the steps of:

(1) preheating the Saudi medium crude oil by using a heating furnace, then entering a flash tower 2 to sequentially carry out two-stage flash separation, wherein the feeding temperature of the first-stage flash separation is 335 ℃, the pressure is 15kPaG, the light component is obtained at the top of the tower, the component at the bottom of the tower is continuously subjected to the second-stage flash separation, the feeding temperature of the second-stage flash separation is 375 ℃, the pressure is 8kPaA, the intermediate component is obtained at the top of the tower, and the heavy component is obtained at the bottom of the tower;

the intermediate component and the heavy component are separated by an extraction separator respectively, an extracting agent for extracting the intermediate component is furfural, the volume ratio of the extracting agent to the intermediate component is 3:1, an extracting agent for extracting the heavy component is butane and pentane in the volume ratio of 1:1, the volume ratio of the extracting agent to the heavy component is 5:1, the intermediate component is separated to obtain first alkane-rich and first aromatic-rich, and the heavy component is separated to obtain second alkane-rich and second aromatic-rich;

(2) forming alkane-rich gas from the alkane-rich component obtained in the step (1) by adopting a fuel gas combustion heat supply mode, mixing the alkane-rich gas with the light component to perform a cascade fluidization cracking reaction, wherein the fluidization cracking reaction is performed by adopting a two-stage riser reactor, the used catalyst is a ZSM-5 molecular sieve catalyst, the temperature of the first-stage fluidization cracking reaction is 550 ℃, the time is 1.2s, the temperature of the second-stage fluidization cracking reaction is 750 ℃, the time is 1.5s, the pressure of the two-stage reaction is 0.2MPa, so that cracking gas, a C4 component, a C5 component and cracking oil are obtained, the cracking gas comprises ethylene, propylene and hydrogen-rich gas, and the hydrogen-rich gas is used as a raw material for the hydropyrolysis reaction in the step (3);

(3) carrying out two-stage hydropyrolysis reaction on the aromatic hydrocarbon-rich component obtained in the step (1) by using a hydropyrolysis reactor, wherein the catalyst is a W-Ni hydrogenation catalyst, the temperature of the first-stage hydropyrolysis reaction is 420 ℃, the reaction pressure is 20MPaG, the hydrogen-oil ratio is 800, and the volume space velocity is 1.0h ^-1 (ii) a The first stageThe hydropyrolysis reaction product continues to carry out secondary hydropyrolysis reaction, the temperature of the secondary hydropyrolysis reaction is 475 ℃, the reaction pressure is 20MPaG, the hydrogen-oil ratio is 1700, and the volume space velocity is 1.2h ^-1 And (3) performing a two-stage hydropyrolysis reaction to obtain an aromatic hydrocarbon product, a non-aromatic hydrocarbon product and fuel gas, wherein the aromatic hydrocarbon product comprises benzene, toluene and xylene, the aromatic hydrocarbon product is mixed with the pyrolysis oil obtained in the step (2) to be used as an aromatic hydrocarbon raw material, and the fuel gas comprises H ₂ S、NH ₃ 、H ₂ And CH ₄ And (3) returning the non-aromatic hydrocarbon product to the step (2) for carrying out the cascade fluidized cracking reaction.

In this embodiment, the crude oil is subjected to component division, and is subjected to cascade fluidized cracking and hydropyrolysis, so that the crude oil is fully converted into chemicals, the yield of olefin products reaches 57.1%, and the yield of aromatic hydrocarbon products reaches 30.2%.

Comparative example 1:

this comparative example provides an apparatus and process for the preparation of olefins and aromatics by means of a crude oil fractionation process, with reference to the apparatus of example 1, except that: the crude oil separation unit comprises only a flash column 2.

The process is referred to the process in example 4 with the difference that: in the step (1), only flash separation is carried out, and extraction separation operation is not carried out.

In the comparative example, because the crude oil is only subjected to flash separation, alkane components with the molecular weights close to those of aromatic hydrocarbon components in the intermediate component and the heavy component are difficult to separate fully, and when the two components are used for producing olefin and aromatic hydrocarbon respectively, the conversion rate is low, the yield of olefin products is only 46.1%, and the yield of aromatic hydrocarbon products is only 28.7%.

Comparative example 2:

this comparative example provides an apparatus and process for the preparation of olefins and aromatics by means of a crude oil fractionation process, with reference to the apparatus of example 1, except that: the fluidized cracking unit 6 employs a conventional steam cracking furnace.

The process is referred to the process in example 4 with the difference that: preparing olefin from the alkane-rich component and the light component in the step (2) by adopting a steam cracking mode, wherein the cracking temperature is 900 ℃, and the reaction time is 0.2 s.

In the comparative example, as the paraffin-rich component and the light component after the crude oil is cut adopt the steam cracking process, the required equipment is more complex, the operation cost is higher, and the yield of the olefin product is limited and is only 42 percent.

It can be seen from the above examples and comparative examples that synthesize, the device of the utility model adopts two-stage splitter according to the characteristic of crude oil to cut it into light component, rich alkane and rich arene component, and then selects suitable processing apparatus according to the characteristic of each component, and light component and rich alkane adopt the fluidization cracking unit mainly to produce alkene, and rich arene adopts the hydropyrolysis unit mainly to produce arene, fully improves the yield of chemicals such as alkene, arene and the like produced from crude oil, the yield of alkene products can reach more than 53%, the yield of arene products can reach more than 30%, improves the value of its utilization; the device has the advantages of simple structure, shorter flow, lower cost, strong adaptability to raw materials and stronger industrial popularization and application value.

The present invention is described in the above embodiments, but the present invention is not limited to the above detailed device, i.e. the present invention must rely on the above detailed device to implement. It should be clear to those skilled in the art that any improvement of the present invention, to the addition of the equivalent replacement and auxiliary devices of the present invention, the selection of the specific mode, etc., all fall within the scope of protection and disclosure of the present invention.

Claims

1. The device for preparing the olefin and the aromatic hydrocarbon by classifying and processing the crude oil is characterized by comprising a crude oil segmentation unit, a fluidized cracking unit and a hydropyrolysis unit, wherein the crude oil segmentation unit sequentially comprises a flash tower and an aromatic hydrocarbon-alkane separation device, and the fluidized cracking unit comprises a cascade riser reactor; the light component outlet of the flash tower is connected with the inlet of the fluidized cracking unit, the middle component outlet and the heavy component outlet of the flash tower are connected with the inlet of the aromatic hydrocarbon-alkane separation device, the alkane-rich outlet of the aromatic hydrocarbon-alkane separation device is connected with the inlet of the fluidized cracking unit, the aromatic hydrocarbon-rich outlet of the aromatic hydrocarbon-alkane separation device is connected with the inlet of the hydropyrolysis unit, and one outlet of the hydropyrolysis unit is connected with the inlet of the fluidized cracking unit.

2. The apparatus for the separation and processing of crude oil to make olefins and aromatics according to claim 1, wherein the flash column comprises a first flash column and a second flash column, wherein the top outlet of the first flash column is connected to the inlet of the fluidized cracking unit, the bottom outlet of the first flash column is connected to the inlet of the second flash column, and the top outlet and the bottom outlet of the second flash column are both connected to the inlet of the aromatics-paraffins separation device.

3. The apparatus for processing crude oil to produce olefins and aromatics according to claim 1, wherein the aromatics-paraffins separating means comprises a first aromatics-paraffins separating means and a second aromatics-paraffins separating means, the intermediate component outlet of the flash column is connected to the inlet of the first aromatics-paraffins separating means, and the heavy component outlet of the flash column is connected to the inlet of the second aromatics-paraffins separating means.

4. The apparatus for processing and producing olefins and aromatics according to claim 3, wherein the first paraffin-rich outlet of the first aromatics-paraffins separation device and the second paraffin-rich outlet of the second aromatics-paraffins separation device are both connected to the inlet of the fluidized cracking unit, and the first aromatics-rich outlet of the first aromatics-paraffins separation device and the second aromatics-rich outlet of the second aromatics-paraffins separation device are both connected to the inlet of the hydropyrolysis unit;

the aromatics-paraffins separation apparatus independently includes an extractive separation column.

5. The apparatus for the classified processing of crude oil to produce olefins and aromatics according to claim 1, further comprising a preheater, an outlet of which is connected to an inlet of the flash column.

6. The apparatus for processing crude oil to produce olefins and aromatics according to claim 1, further comprising a gasification furnace, wherein an inlet of the gasification furnace is connected to the alkane-rich outlet of the aromatics-alkane separation device, and an outlet of the gasification furnace is connected to an inlet of the fluidized cracking unit;

the gasification heating furnace is provided with a fuel inlet and a flue gas outlet.

7. The apparatus for the classified processing of crude oil to produce olefins and aromatics according to claim 1, wherein the riser reactor in the fluidized cracking unit comprises at least two stages.

8. The apparatus for the fractionation of crude oil into olefins and aromatics according to claim 7, wherein the riser reactor comprises a primary riser reactor and a secondary riser reactor;

and introducing the hydrogen-rich product of the fluidized cracking unit into an inlet of the hydropyrolysis unit.

9. The apparatus for the separation and processing of crude oil into olefins and aromatics according to claim 1, wherein the hydropyrolysis unit comprises at least one hydropyrolysis reactor.

10. The apparatus for the separation and processing of crude oil into olefins and aromatics according to claim 9, wherein the hydropyrolysis unit comprises a primary hydropyrolysis reactor and a secondary hydropyrolysis reactor;

and the outlet of the non-aromatic hydrocarbon product of the hydropyrolysis unit is connected with the inlet of the fluidized cracking unit.