阅读说明：本技术 一种由原油最大化生产基础化学品的组合工艺方法 (Combined process for maximizing production of basic chemicals from crude oil ) 是由 郭春垒 于海斌 李犇 王银斌 臧甲忠 刘航 董子超 范景新 刘晗 周微 刘洋 于 2021-09-20 设计创作，主要内容包括：本发明提供了一种由原油最大化生产基础化学品的组合工艺方法,该方法先将原油进行精制,精制原油经轻重切割,轻馏分经吸附分离进行非芳烃与芳烃组分的分离,针对组分特性配套烯烃、芳烃增产加工工艺,以最大化生产低碳烯烃和芳烃；重馏分经定向改质单元,转化为富含烯烃和芳烃的改质产物,改质汽柴油经催化裂解增产烯烃、芳烃,改质重产物中富含多环芳烃。本发明组合工艺方法具有原料适应性强、化学品收率高(75～85wt％)、氢耗低、操作条件缓和等优势,可用于工业化生产。(The invention provides a combined process method for producing basic chemicals from crude oil to the maximum extent, which comprises the steps of refining the crude oil, cutting the refined crude oil by light and heavy, separating non-aromatic hydrocarbon and aromatic hydrocarbon components by light fraction through adsorption separation, and matching olefin and aromatic hydrocarbon yield-increasing processing technology aiming at component characteristics to produce low-carbon olefin and aromatic hydrocarbon to the maximum extent; the heavy fraction is converted into a modified product rich in olefin and aromatic hydrocarbon through a directional modification unit, the modified gasoline and diesel oil is subjected to catalytic cracking to increase the yield of olefin and aromatic hydrocarbon, and the modified heavy product is rich in polycyclic aromatic hydrocarbon. The combined process method has the advantages of strong raw material adaptability, high chemical yield (75-85 wt%), low hydrogen consumption, mild operation conditions and the like, and can be used for industrial production.)

1. A combined process for maximizing the production of base chemicals from crude oil comprising the steps of:

1) crude oil firstly enters a crude oil hydrofining unit, and under the action of a crude oil hydrofining catalyst, the reaction temperature is 280-420 ℃, the pressure is 3.0-8.0 MPa, and the mass space velocity is 1.0-2.5 h^-1Removing colloid, olefin and sulfur and nitrogen impurities under the condition that the volume ratio of hydrogen to oil is 300: 1-800: 1 to obtain fuel gas and refined crude oil;

2) the refined crude oil obtained in the step 1) enters a refined crude oil cutting unit, and is rectified and separated to obtain gasoline and diesel oil fractions with the temperature of less than or equal to 375 ℃ and heavy oil fractions with the temperature of more than 375 ℃;

3) the gasoline and diesel oil fraction obtained in the step 2) enters a gasoline and diesel oil adsorption separation unit, and is subjected to adsorption temperature of 40-150 ℃, pressure of 0.2-1.0 MPa and mass space velocity of 0.5-1.5 h under the action of an adsorbent^-1Under the condition of (1), separating aromatic hydrocarbon components and non-aromatic hydrocarbon components of the gasoline and diesel oil to obtain aromatic hydrocarbon adsorption components and non-aromatic hydrocarbon adsorption components;

4) the heavy oil fraction obtained in the step 2) enters a heavy oil directional modification unit, and under the action of a directional modification catalyst, directional decarburization, demetalization and cracking modification reactions are carried out under the conditions that the reaction temperature is 350-520 ℃, the pressure is 0.1-1.0 MPa and the steam/oil mass ratio is 0.1: 1-10: 1, so as to obtain hydrogen, a fulvene gas, modified fulvene distillate oil and coke;

5) the non-aromatic hydrocarbon adsorbing component obtained in the step 3) enters an ethylene steam cracking unit, and cracking reaction is carried out under the conditions that the reaction temperature is 750-850 ℃, the pressure is 0.1-0.5 MPa, the steam/oil mass ratio is 0.3: 1-1.2: 1, and the residence time is 0.05-0.5 s, so that the alkene-rich gas, the cracked gasoline and diesel oil and the ethylene tar are obtained;

6) the adsorbed aromatic hydrocarbon component obtained in the step 3) enters an aromatic hydrocarbon yield increasing unit, and is subjected to reaction at the temperature of 360-460 ℃, the pressure of 4.0-8.0 MPa and the volume airspeed of 1.0-2.0 h under the action of an aromatic hydrocarbon yield increasing catalyst^-1And performing selective cracking reaction under the condition that the volume ratio of hydrogen to oil is 600: 1-1200: 1 to obtain fuel gas, saturated liquefied gas, light aromatic hydrocarbon and C₉/C₁₀Aromatic hydrocarbons;

7) the modified rich-alkene distillate oil obtained in the step 4) enters a rich-alkene distillate oil cutting unit, and is rectified and separated to obtain rich-alkene light distillate oil with the temperature of less than or equal to 375 ℃ and rich-aromatic heavy distillate oil with the temperature of more than 375 ℃;

8) allowing the light olefin-rich distillate oil obtained in the step 7) to enter a catalytic cracking unit, and performing directional catalytic cracking reaction under the action of a catalytic cracking catalyst at the conditions of reaction temperature of 480-600 ℃, pressure of 0.1-0.3 MPa, agent-oil ratio of 8: 1-15: 1 and steam-oil mass ratio of 0.2: 1-1.0: 1 to obtain olefin-rich gas, catalytic gasoline and diesel oil, oil slurry and coke;

9) returning the cracked gasoline and diesel oil obtained in the step 5) and the catalytic gasoline and diesel oil obtained in the step 8) to the aromatic hydrocarbon yield increasing unit in the step 6) together;

10) step 6), the obtained fuel gas and the saturated liquefied gas are returned to the ethylene steam cracking unit in the step 5);

11) the ethylene tar obtained in the step 5), the aromatic-rich heavy distillate oil obtained in the step 7) and the slurry oil obtained in the step 8) enter a needle coke yield increasing unit together, and needle coke, coking gasoline and diesel oil and alkene-rich gas are obtained through delayed coking and high-temperature calcination procedures;

in the heavy oil directional modification unit in the step 4), heavy oil macromolecules undergo a directional modification reaction, the conversion rate of heavy oil is more than or equal to 70 wt%, the olefin content in the converted gasoline and diesel oil product is 40-60 wt%, the aromatic hydrocarbon content is 20-40 wt%, and the polycyclic aromatic hydrocarbon content in the converted heavy oil is 60-85 wt%.

2. The method of claim 1 wherein the crude oil in step 1) is at least one of a paraffinic, a mesogenic, and a naphthenic crude oil.

3. The method of claim 1, wherein the crude oil hydrorefining catalyst in step 1) is a metal supported catalyst, wherein the carrier is at least one of macroporous alumina, silica and amorphous silica-alumina, and the supported metal component is at least one of Ni, Mo, Co and W.

4. The method as claimed in claim 1, wherein the gasoline-diesel adsorption separation unit in step 3) adopts a fixed bed or a simulated moving bed, and the adsorbent is at least one of mesoporous high-silica molecular sieve, activated carbon, clay, white carbon black, activated carbon and silica gel.

5. The method according to claim 1, wherein the heavy oil directional upgrading unit in step 4) is in the form of one of a moving bed, a dense fluidized bed and a riser reactor; the directional modified catalyst is a supported catalyst containing a heavy metal trapping agent and an alkaline auxiliary agent, wherein the carrier is at least one of white carbon black, a mesoporous high-silicon molecular sieve, attapulgite, silica gel, alumina, kaolin, montmorillonite, carclazyte and diatomite, the active component of the heavy metal trapping agent is one or more of Bi, Ce, Sn, Cr and La, and the active component of the alkaline auxiliary agent is at least one of Li, Na, Ca, Mg, K and Ba.

6. The method according to claim 1, wherein the aromatic hydrocarbon yield increasing catalyst in the step 6) is a metal modified composite molecular sieve catalyst, the molecular sieve is at least two of Y, mercerized zeolite, beta, ZSM-5 and MCM-22, and the metal modified component is at least one of Ni, Mo, Zn, Pt, Pd, Re and Sn.

7. The method of claim 1, wherein the catalytic cracking unit in step 8) is in the form of one of a downer and a downer reducer, and the olefin yield increasing catalyst is at least one of a fully crystalline high silica beta, a mercerized form, a ZSM-5 form, an APO-5 form, a TS-1 form, an MCM-22 form, and an Y, IM-5 form.

Technical Field

The invention relates to the technical field of production of low-carbon olefins, aromatic hydrocarbons and needle coke, in particular to a combined process method for maximally producing basic chemicals from crude oil.

Background

With the vigorous development of new energy technologies, the fossil energy status is greatly challenged. The traditional refining industrial structure mainly produces high-quality gasoline and diesel oil, the transformation difficulty to the chemical industry is large, the chemical industry product rate can only reach about 45%, a large amount of gasoline and diesel oil still need to be produced, the product sale faces great difficulty, and the seeking of a revolutionary industry transformation upgrading technology is imperative. The technology of directly preparing chemicals from crude oil is an important means for industrial transformation, and has become a hot spot of current research.

The method for directly preparing chemicals from crude oil overturns the traditional processing concept, has the remarkable advantages of short flow, low energy consumption, low investment, high chemical yield and the like, and breaks through the existing pattern of the global petrochemical industry, thereby having revolutionary influence on the refining industry. At present, the most representative foreign technologies for directly producing chemicals from crude oil are the exxonmobil technology and the saudi amat technology, and the domestic representative technologies mainly include the crude oil catalytic cracking technology developed by the institute of petrochemical and chemical engineering science and the Chinese petroleum university.

The exxon meifu company applies serial patents at home and abroad, such as US20050261538A1, US007488459B2, CN200580016314.X, CN200780047937.2 and the like, at first, the technical innovation point is that crude oil is directly supplied to a steam cracking furnace, and a flash tank is added between a convection section and a radiation section of the cracking furnace, compared with the traditional naphtha cracking process, 100-200 dollars can be earned for each 1 ton of ethylene produced, and the process has great competitive advantage. However, the raw materials of the technology are limited to paraffin-based crude oil, and a large amount of heavy oil by-produced still needs to be sent to a traditional refinery for treatment.

Saudi America technology includes both thermal crude oil chemical (TC2CTM) technology and catalytic crude oil chemical (CC2CTM) technology. Related patents of a TC2CTM technical route include US20130248416A1, US20130228495A1, US20160312132A1, CN201380006638.X, CN201780078205.3 and CN201880020904.7, crude oil is directly processed by adopting an integrated hydrotreating, steam cracking and coking process to produce olefin, aromatic hydrocarbon petrochemical products and petroleum coke, the route aims at that the raw material is paraffin-based crude oil, the yield of the steam cracking raw material is improved by a hydrogenation method, so that the yield of ethylene is increased, and the petroleum coke is produced from heavy oil which is not converted by a coking process. Related patents of the CC2CTM technical route include US2013033165, CN201380015214.X and the like, crude oil hydrocracking, steam cracking and high-severity catalytic cracking are adopted to increase the yield of low-carbon olefin and aromatic hydrocarbon, and the traditional processing technology with high cost such as grafting hydrocracking and the like is still needed.

Patents published by the institute of petrochemical and chemical science, such as CN201810523356.1, CN110540869A, CN110540866A, etc., firstly cut crude oil into light and heavy fractions, and then perform catalytic cracking to produce low-carbon olefins, which is implemented by using a double-riser reactor of a set of catalytic cracking apparatus, and the two risers are respectively fed with different distillate oil. The technology requires the raw material to be paraffin base crude oil, and if the raw material is intermediate base or naphthenic base, the cut heavy fraction needs to be hydrogenated firstly.

The university of petroleum in china promulgated two technological routes: one is that crude oil or heavy oil fraction enters two reactors to be catalytically cracked after being cut (CN109575982A), the technical route is basically consistent with the stone hospital route, and the raw material is mainly limited to paraffin base crude oil; the other is a crude oil integrated pretreatment, acid catalytic cracking and hydrotreatment process (CN201810341186.5, CN201810341227.0 and US16386872), the route mainly aims at poor crude oil, a large amount of heavy oil circulates in a system, the energy consumption of the system is high, and the externally thrown heavy oil cannot be utilized.

In summary, the existing crude oil processing technologies mainly include several technical routes of steam cracking, catalytic cracking and hydrocracking, and are high in raw material dependence and mainly suitable for paraffin-based crude oil or heavy oil raw materials. In addition, the product mainly comprises olefin and aromatic hydrocarbon, the yield of chemicals is 40-70%, the yield is further improved, and the variety of the chemicals needs to be further expanded.

Disclosure of Invention

The invention mainly solves the problems of poor raw material adaptability, low chemical yield, few chemical varieties and the like in the existing technology for preparing chemicals from crude oil, integrates the processes of heavy oil directional modification, gasoline and diesel adsorption separation, aromatic hydrocarbon yield increase, olefin yield increase, needle coke yield increase and the like, and converts the crude oil into low-carbon olefin, aromatic hydrocarbon and needle coke to the maximum extent.

In order to solve the technical problems, the invention adopts the following technical scheme:

the invention provides a combined process method for maximally producing basic chemicals from crude oil, which comprises the following steps:

1) crude oil firstly enters a crude oil hydrofining unit, and under the action of a crude oil hydrofining catalyst, the reaction temperature is 280-420 ℃, the pressure is 3.0-8.0 MPa, and the mass space velocity is 1.0-2.5 h^-1Removing impurities such as colloid, olefin, sulfur and nitrogen under the condition that the volume ratio of hydrogen to oil is 300: 1-800: 1 to obtain fuel gas and refined crude oil;

2) the refined crude oil obtained in the step 1) enters a refined crude oil cutting unit, and is rectified and separated to obtain gasoline and diesel fractions (less than or equal to 375 ℃) and heavy oil fractions (more than 375 ℃);

3) the gasoline and diesel oil fraction obtained in the step 2) enters a gasoline and diesel oil adsorption separation unit, and is subjected to adsorption temperature of 40-150 ℃, pressure of 0.2-1.0 MPa and mass space velocity of 0.5-1.5 h under the action of an adsorbent^-1Under the condition of (1), separating aromatic hydrocarbon components and non-aromatic hydrocarbon components of the gasoline and diesel oil to obtain aromatic hydrocarbon adsorption components and non-aromatic hydrocarbon adsorption components;

4) the heavy oil fraction obtained in the step 2) enters a heavy oil directional modification unit, and under the action of a directional modification catalyst, directional decarburization, demetalization and cracking modification reactions are carried out under the conditions that the reaction temperature is 350-520 ℃, the pressure is 0.1-1.0 MPa and the steam/oil mass ratio is 0.1: 1-10: 1, so as to obtain hydrogen, a fulvene gas, modified fulvene distillate oil and coke;

5) the non-aromatic hydrocarbon adsorbing component obtained in the step 3) enters an ethylene steam cracking unit, and cracking reaction is carried out under the conditions that the reaction temperature is 750-850 ℃, the pressure is 0.1-0.5 MPa, the steam/oil mass ratio is 0.3: 1-1.2: 1, and the residence time is 0.05-0.5 s, so that the alkene-rich gas, the cracked gasoline and diesel oil and the ethylene tar are obtained;

6) the adsorbed aromatic hydrocarbon component obtained in the step 3) enters an aromatic hydrocarbon yield increasing unit, and is subjected to reaction at the temperature of 360-460 ℃, the pressure of 4.0-8.0 MPa and the volume airspeed of 1.0-2.0 h under the action of an aromatic hydrocarbon yield increasing catalyst^-1And performing selective cracking reaction under the condition that the volume ratio of hydrogen to oil is 600: 1-1200: 1 to obtain fuel gas, saturated liquefied gas, light aromatic hydrocarbons (benzene, toluene and xylene) and C₉/C₁₀Aromatic hydrocarbons;

7) the modified rich-alkene distillate oil obtained in the step 4) enters a rich-alkene distillate oil cutting unit, and is rectified and separated to obtain rich-alkene light distillate oil (less than or equal to 375 ℃) and rich-aromatic heavy distillate oil (more than 375 ℃);

8) allowing the light olefin-rich distillate oil obtained in the step 7) to enter a catalytic cracking unit, and performing directional catalytic cracking reaction under the action of a catalytic cracking catalyst at the conditions of reaction temperature of 480-600 ℃, pressure of 0.1-0.3 MPa, agent-oil ratio of 8: 1-15: 1 and steam-oil mass ratio of 0.2: 1-1.0: 1 to obtain olefin-rich gas, catalytic gasoline and diesel oil, oil slurry and coke;

9) returning the cracked gasoline and diesel oil obtained in the step 5) and the catalytic gasoline and diesel oil obtained in the step 8) to the aromatic hydrocarbon yield increasing unit in the step 6) together;

10) step 6), the obtained fuel gas and the saturated liquefied gas are returned to the ethylene steam cracking unit in the step 5);

11) the tar obtained in the step 5), the aromatic-rich heavy distillate oil obtained in the step 7) and the slurry oil obtained in the step 8) enter a needle coke yield increasing unit together, and needle coke, coking gasoline and diesel oil and alkene-rich gas are obtained through delayed coking and high-temperature calcination procedures;

in the heavy oil directional modification unit in the step 4), heavy oil macromolecules undergo a directional modification reaction, the conversion rate of heavy oil is more than or equal to 70 wt%, the olefin content in the converted gasoline and diesel oil product is 40-60 wt%, the aromatic hydrocarbon content is 20-40 wt%, and the polycyclic aromatic hydrocarbon content in the converted heavy oil is 60-85 wt%.

The crude oil in the step 1) is at least one of paraffin base crude oil, intermediate base crude oil and naphthenic base crude oil. The crude oil hydrorefining catalyst is metal supported catalyst, and the carrier is at least one of macroporous alumina, silica and amorphous silica-alumina, and the supported metal component is at least one of Ni, Mo, Co and W.

In the step 3), the gasoline and diesel oil adsorption separation unit adopts a fixed bed or a simulated moving bed, and the adsorbent is at least one of a mesoporous high-silicon molecular sieve, activated carbon, argil, white carbon black, activated carbon and silica gel.

In the step 4), the heavy oil directional modification unit adopts one of a moving bed, a dense-phase fluidized bed and a riser reactor. The oriented modification catalyst is a supported catalyst containing a heavy metal trapping agent and an alkaline auxiliary agent, wherein the carrier comprises but is not limited to at least one of white carbon black, a mesoporous high-silica molecular sieve, attapulgite, silica gel, alumina, kaolin, montmorillonite, clay and diatomite, the active component of the heavy metal trapping agent comprises but is not limited to one or more of Bi, Ce, Sn, Cr and La, and the active component of the alkaline auxiliary agent comprises but is not limited to at least one of Li, Na, Ca, Mg, K and Ba.

In the step 6), the aromatic hydrocarbon yield-increasing catalyst is a metal modified composite molecular sieve catalyst, the molecular sieve is at least two of Y, mercerization, beta, ZSM-5 and MCM-22, and the metal modified component is at least one of Ni, Mo, Zn, Pt, Pd, Re and Sn.

In the step 8), the catalytic cracking unit adopts one of a descending bed and a descending bed reducing reactor, and the olefin yield increasing catalyst is at least one of a full-crystalline high-silicon beta, mercerized, ZSM-5, APO-5, TS-1, MCM-22 and Y, IM-5 molecular sieve.

Compared with the prior art, the combined process method for producing the basic chemicals to the maximum extent by using the crude oil has the following beneficial effects:

1) the raw material adaptability is strong, and the processing process is simple: the heavy oil is modified into high-quality chemical production raw materials (rich in olefin and aromatic hydrocarbon) by adopting the heavy oil directional modification unit, and the dependence of high chemical yield on paraffin-based raw materials is broken.

2) The chemical species are various, and the chemical yield is high: the directional upgrading unit enriches polycyclic aromatic hydrocarbon into upgraded heavy oil, and is a high-quality needle coke production raw material. The gasoline and diesel oil is subjected to adsorption separation to realize separation of non-aromatic hydrocarbon (alkane and olefin) and aromatic hydrocarbon components, and is converted into low-carbon olefin, aromatic hydrocarbon and needle coke by matching a subsequent processing unit according to component characteristics, wherein the total chemical yield reaches 75-85%.

Drawings

FIG. 1 is a schematic flow diagram of a combined process for maximizing the production of base chemicals from crude oil according to the present invention.

In the figure: the device comprises a crude oil hydrofining unit 1, a refined crude oil cutting unit 2, a gasoline and diesel oil adsorption and separation unit 3, a heavy oil directional modification unit 4, an ethylene steam cracking unit 5, an aromatic hydrocarbon yield increasing unit 6, a fulvene distillate oil cutting unit 7, a catalytic cracking unit 8 and a needle coke yield increasing unit 9.

Detailed Description

The following further describes the implementation and effects of the method according to the present invention by means of specific embodiments, but the present invention is not limited thereby.

As shown in fig. 1, the present invention provides a combined process for maximizing the production of base chemicals from crude oil, comprising the steps of:

1) crude oil enters a crude oil hydrofining unit 1 firstly, and under the action of a crude oil hydrofining catalyst and under reaction conditions, impurities such as colloid, olefin, sulfur and nitrogen are removed to obtain fuel gas and refined crude oil;

2) the refined crude oil obtained in the step 1) enters a refined crude oil cutting unit 2, and is rectified and separated to obtain gasoline and diesel fractions (less than or equal to 375 ℃) and heavy oil fractions (more than 375 ℃);

3) the gasoline and diesel oil fraction obtained in the step 2) enters a gasoline and diesel oil adsorption separation unit 3, and the gasoline and diesel oil aromatic hydrocarbon component and the non-aromatic hydrocarbon component are separated under the action of an adsorbent to obtain an adsorbed aromatic hydrocarbon component and an adsorbed non-aromatic hydrocarbon component;

4) the heavy oil fraction obtained in the step 2) enters a heavy oil directional modification unit 4, and is subjected to directional decarburization, demetalization and cracking modification reaction under the action of a directional modification catalyst to obtain hydrogen, a fulvene gas, modified fulvene distillate oil and coke;

5) the absorbed non-aromatic hydrocarbon components obtained in the step 3) enter an ethylene steam cracking unit 5 for cracking reaction to obtain alkene-rich gas, cracked gasoline and diesel oil and ethylene tar;

6) the adsorbed aromatic hydrocarbon component obtained in the step 3) enters an aromatic hydrocarbon yield increasing unit 6, and is subjected to selective cracking reaction under the action of an aromatic hydrocarbon yield increasing catalyst to obtain fuel gas, saturated liquefied gas, light aromatic hydrocarbons (benzene, toluene and xylene) and C₉/C₁₀Aromatic hydrocarbons;

7) the modified rich-alkene distillate oil obtained in the step 4) enters a rich-alkene distillate oil cutting unit 7, and is rectified and separated to obtain rich-alkene light distillate oil (less than or equal to 375 ℃) and rich-aromatic heavy distillate oil (more than 375 ℃);

8) the light distillate oil rich in alkene obtained in the step 7) enters a catalytic cracking unit 8, and is subjected to directional catalytic cracking reaction under the action of a catalytic cracking catalyst to obtain a gas rich in alkene, catalytic gasoline and diesel oil, oil slurry and coke;

9) returning the cracked gasoline and diesel oil obtained in the step 5) and the catalytic gasoline and diesel oil obtained in the step 8) to the aromatic hydrocarbon yield increasing unit 6 in the step 6) together;

10) step 6), the obtained fuel gas and the saturated liquefied gas are returned to the ethylene steam cracking unit 5 in the step 5);

11) the tar obtained in the step 5), the aromatic-rich heavy distillate oil obtained in the step 7) and the slurry oil obtained in the step 8) enter a needle coke yield increasing unit 9 together, and needle coke, coking gasoline and diesel oil and alkene-rich gas are obtained through delayed coking and high-temperature calcination processes.

Example 1

Paraffin-based crude oil from a refinery is used as a raw material, and the properties of the raw material are shown in Table 1.

A crude oil hydrofining unit: the catalyst adopts Ni-Mo/macroporous alumina (taking the catalyst as a base)Accurately, the Ni content is 8 wt%, the Mo content is 4.0 wt%, and the balance is macroporous alumina), and the reaction conditions are as follows: the temperature is 320 ℃, the pressure is 5.0MPa, and the mass space velocity is 1.0h^-1And the volume ratio of hydrogen to oil is 800: 1.

Gasoline and diesel oil adsorption separation unit: adopting a simulated moving bed process, wherein the adsorbent is white carbon black, and the separation conditions are as follows: the adsorption temperature is 90 ℃, the pressure is 0.5MPa, and the mass space velocity is 1.0h^-1。

A heavy oil directional modification unit: the reactor adopts a riser reactor, the directional modification catalyst adopts Bi-Ca-K/coarse silica gel (based on the catalyst, the Bi content is 2.5 wt%, the Ca content is 5.0 wt%, the K content is 8.0 wt%, and the balance is coarse silica gel), and the reaction conditions are as follows: the temperature is 500 ℃, the pressure is 0.1MPa, and the steam/oil mass ratio is 1.0: 1.

Ethylene steam cracking unit: the reaction temperature is 780 ℃, the pressure is 0.1MPa, the steam/oil mass ratio is 0.4:1, and the retention time is 0.1 s.

An aromatic hydrocarbon yield increasing unit: the catalyst is a bimetal modified composite molecular sieve catalyst (based on the catalyst, the Ni content is 12 wt%, the Mo content is 4 wt%, the Y molecular sieve content is 40 wt%, the beta molecular sieve content is 20 wt%, the ZSM-5 molecular sieve content is 10 wt%, and the balance is alumina), and the reaction conditions are as follows: the temperature is 400 ℃, the pressure is 5.0MPa, and the volume space velocity is 1.0h^-1Hydrogen-oil volume ratio of 900:1

A catalytic cracking unit: adopting a descending bed reactor, wherein the catalyst is a high-silicon ZSM-5+ beta + MCM-22 molecular sieve catalyst, and the reaction conditions are as follows: the reaction temperature is 580 ℃, the pressure is 0.2MPa, the agent-oil ratio is 10:1, and the steam-oil mass ratio is 1: 1.

Needle coke yield increase unit: the reaction temperature of the coking device is 510 ℃, and the reaction pressure is 0.15 MPa.

The material balance of the above process is shown in Table 2.

Example 2

The properties of the intermediate base crude oil from a refinery are shown in Table 1.

A crude oil hydrofining unit: the catalyst adopts Ni-Mo/macroporous alumina (based on the catalyst, the Ni content is 12 wt%, the Mo content is 4.0 wt%, and the balance is macroporous alumina), and the reaction conditions are as follows: the temperature is 360 ℃ and the pressure is 6.0MPa, mass airspeed of 1.5h^-1And the volume ratio of hydrogen to oil is 800: 1.

Gasoline and diesel oil adsorption separation unit: a fixed bed process is adopted, the adsorbent is a mesoporous high-silicon SBA-15 molecular sieve, and the separation conditions are as follows: the adsorption temperature is 120 ℃, the pressure is 0.5MPa, and the mass space velocity is 0.5h^-1。

A heavy oil directional modification unit: the reactor adopts a dense-phase fluidized bed, the directional modification catalyst adopts Bi-Ca-K/white carbon black (taking the catalyst as a reference, the Bi content is 4.0 wt%, the Ca content is 10.0 wt%, the K content is 5.0 wt%, and the balance is white carbon black), and the reaction conditions are as follows: the temperature is 480 ℃, the pressure is 0.2MPa, and the steam/oil mass ratio is 2.0: 1.

An aromatic hydrocarbon yield increasing unit: the catalyst is a bimetal modified composite molecular sieve catalyst (based on the catalyst, the Ni content is 12 wt%, the Pt content is 0.2 wt%, the beta molecular sieve content is 55 wt%, the ZSM-5 molecular sieve is 15 wt%, and the balance is alumina), and the reaction conditions are as follows: the temperature is 420 ℃, the pressure is 6.0MPa, and the volume space velocity is 1.5h^-1And the volume ratio of hydrogen to oil is 1200: 1.

Ethylene steam cracking unit: the reaction temperature is 800 ℃, the pressure is 0.2MPa, the steam/oil mass ratio is 0.3, and the retention time is 0.05S.

A catalytic cracking unit: adopting a descending bed reducing reactor, wherein the catalyst is a high-silicon ZSM-5+ Y molecular sieve catalyst, and the reaction conditions are as follows: the reaction temperature is 600 ℃, the pressure is 0.1MPa, the agent-oil ratio is 15:1, and the steam-oil mass ratio is 0.8: 1.

Needle coke yield increase unit: the reaction temperature of the coking device is 510 ℃, and the reaction pressure is 0.15 MPa.

The material balance of the above process is shown in Table 2.

Example 3

Naphthenic base crude oil of a certain refinery is used as a raw material, and the properties of the raw material are shown in table 1.

A crude oil hydrofining unit: the catalyst adopts Ni-Mo/macroporous alumina (based on the catalyst, the Ni content is 12 wt%, the Mo content is 4.0 wt%, and the balance is macroporous alumina), and the reaction conditions are as follows: the temperature is 360 ℃, the pressure is 6.0MPa, and the mass space velocity is 1.5h^-1And the volume ratio of hydrogen to oil is 800: 1.

Gasoline and diesel oil adsorption separation unit: miningThe simulated moving bed process is adopted, the adsorbent is active carbon, and the separation conditions are as follows: the adsorption temperature is 100 ℃, the pressure is 0.8MPa, and the mass space velocity is 1.0h^-1。

A heavy oil directional modification unit: the reactor adopts a moving bed, the directional modification catalyst adopts a Ce-Ca-Mg/high-silicon MCM-48 molecular sieve (the catalyst is used as a reference, the Ce content is 3.0 wt%, the Ca content is 15.0 wt%, the Mg content is 3.0 wt%, and the balance is molecular sieve + binder), and the reaction conditions are as follows: the temperature is 500 ℃, the pressure is 0.5MPa, and the steam/oil mass ratio is 2.0: 1.

An aromatic hydrocarbon yield increasing unit: the catalyst is a bimetal modified composite molecular sieve catalyst (based on the catalyst, the Ni content is 12 wt%, the Pt content is 0.3 wt%, the beta molecular sieve content is 40 wt%, the ZSM-5 molecular sieve is 20 wt%, and the balance is alumina), and the reaction conditions are as follows: the temperature is 420 ℃, the pressure is 5.0MPa, and the volume space velocity is 1.5h^-1And the volume ratio of hydrogen to oil is 1000: 1.

Ethylene steam cracking unit: the reaction temperature is 820 ℃, the pressure is 0.1MPa, the steam/oil mass ratio is 0.6:1, and the retention time is 0.05 s.

A catalytic cracking unit: adopting a descending bed reducing reactor, wherein the catalyst is a high-silicon ZSM-5+ Y molecular sieve catalyst, and the reaction conditions are as follows: the reaction temperature is 560 ℃, the pressure is 0.2MPa, the agent-oil ratio is 12:1, and the steam-oil mass ratio is 0.6: 1.

Needle coke yield increase unit: the reaction temperature of the coking device is 510 ℃, and the reaction pressure is 0.15 MPa.

The material balance of the above process is shown in Table 2.

TABLE 1 EXAMPLES 1 TO 3 Properties of raw materials

TABLE 2 examples 1-3 Material balances

Examples	Example 1	Example 2	Example 3
				Raw materials in wt%
Crude oil	100	100	100
				Hydrogen gas	1.53	1.62	1.57
Product, wt%
				Hydrogen gas	0.48	0.44	0.4
Alkene-rich gas	61.21	54.54	52.04
				Ethylene	12.85	9.28	8.85
Propylene (PA)	30.24	22.92	21.22
				Butene (butylene)	13.36	10.64	9.55
Trienes as inhibitors of HIV infection	56.45	42.84	39.62
				Coking gasoline and diesel oil	3.32	4.05	4.26
Benzene, toluene and xylene	13.54	16.53	16.96
				C9/C10 aromatic hydrocarbons	6.21	8.76	9.26
Needle coke	9.85	9.78	10.2
				Coke	6.92	7.52	8.45
Total yield of chemicals	86.05	77.91	76.04

As can be seen from Table 2, the total yield of chemicals (olefin + aromatic hydrocarbon + needle coke) in the paraffin-based crude oil, the intermediate-based crude oil and the naphthenic base crude oil can reach 76-86% by the method of the invention, and the total hydrogen consumption is only 1.5-1.62 wt%.