阅读说明：本技术 一种最大化生产化学品的集成工艺方法 (Integrated process method for maximally producing chemicals ) 是由 范景新 郭春垒 臧甲忠 刘航 辛利 李滨 吴青 马明超 董子超 姜雪丹 于 2021-09-20 设计创作，主要内容包括：本发明提供了一种最大化生产化学品的集成工艺方法。本发明集成工艺方法包括：先将原料油进行定向改质,改质汽柴油产物中富含烯烃,通过吸附分离进行非芳烃(烷烃+烯烃)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。改质重油中富含多环芳烃,可生产优质的针状焦。本发明具有原料适应性强、化学品收率高、氢耗低、操作条件缓和等优势,可用于工业化生产。(The invention provides an integrated process for maximizing the production of chemicals. The integrated process method comprises the following steps: raw oil is directionally modified, the modified gasoline and diesel oil product is rich in olefin, non-aromatic hydrocarbon (alkane and olefin) and aromatic hydrocarbon components are separated through adsorption separation, and the olefin and aromatic hydrocarbon yield increasing processing technology is matched according to component characteristics so as to maximally produce low-carbon olefin and aromatic hydrocarbon. The modified heavy oil is rich in polycyclic aromatic hydrocarbon and can produce high-quality needle coke. The method has the advantages of strong raw material adaptability, high chemical yield, low hydrogen consumption, mild operation conditions and the like, and can be used for industrial production.)

1. An integrated process for maximizing the production of chemicals comprising the steps of:

1) raw oil is firstly fed into a raw material directional modification unit, and under the action of a directional modification catalyst, under the conditions of reaction temperature of 350-650 ℃, pressure of 0.1-1.0 MPa and steam/oil mass ratio of 0.1: 1-10: 1, directional decarburization, demetalization and cracking modification reaction of heavy components are carried out, so as to obtain hydrogen, a fulvene gas, modified fulvene distillate oil and coke;

2) feeding the modified fulvene distillate oil obtained in the step 1) into a selective hydrofining unit, and reacting at the reaction temperature of 60-180 ℃, the pressure of 2.0-4.0 MPa and the mass space velocity of 0.5-3.0 h under the action of a selective hydrofining catalyst^-1Removing colloid, alkadiene and alkaline nitrogen impurities under the condition that the volume ratio of hydrogen to oil is 400: 1-800: 1 to obtain fuel gas and refined distillate oil;

3) the refined distillate oil obtained in the step 2) enters a refined distillate oil cutting unit to obtain gasoline and diesel oil fractions which are rich in olefin at the temperature of less than or equal to 350 ℃ and heavy distillate oil which is rich in polycyclic aromatic hydrocarbon at the temperature of more than 350 ℃;

4) the gasoline and diesel oil fraction obtained in the step 3) enters a gasoline and diesel oil adsorption separation unit, and is subjected to adsorption at the temperature of 60-120 ℃, the pressure of 0.2-0.6 MPa and the mass space velocity of 1.0-2.0 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 alkene-rich non-aromatic hydrocarbon adsorption components;

5) the heavy distillate oil obtained in the step 3) enters a needle coke yield increasing unit, and needle coke, coking gasoline and diesel oil and alkene-rich gas are obtained through delayed coking and high-temperature calcination procedures;

6) the adsorbed alkene-rich non-aromatic hydrocarbon component obtained in the step 4) and the coking gasoline and diesel oil obtained in the step 5) enter an alkene yield increasing unit together, and under the action of an alkene yield increasing catalyst, a directional catalytic cracking reaction is carried out under the conditions of 500-650 ℃ of reaction temperature, 0.1-0.5 MPa of pressure, 5: 1-20: 1 of agent-oil ratio and 0.1: 1-1.5: 1 of steam-oil mass ratio to obtain alkene-rich gas, cracked aromatic-rich gasoline and diesel oil and coke;

7) the aromatic hydrocarbon adsorbing component obtained in the step 4) and the cracked aromatic-rich gasoline and diesel oil obtained in the step 6) enter an aromatic hydrocarbon yield increasing unit together, and under the action of an aromatic hydrocarbon yield increasing catalyst, the reaction temperature is 360-500 ℃, the pressure is 3.0-6.0 MPa, and the volume airspeed is 0.5-2.0 h^-1And performing selective cracking reaction on the hydrogen-oil volume ratio of 800: 1-1500: 1 to obtain fuel gas, saturated liquefied gas, light aromatic hydrocarbon and C₉/C₁₀Aromatic hydrocarbons;

in the raw material directional modification unit in the step 1), heavy oil macromolecules in the raw material oil undergo a directional modification reaction, the conversion rate of the 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 heavy oil is 60-85 wt%.

2. The integrated process of claim 1, wherein the feedstock oil in step 1) is at least one of a paraffinic base crude oil, a meso-base crude oil, a naphthenic base crude oil, a waxy oil, an atmospheric residue, a vacuum residue, an oil sand bitumen, and a deasphalted oil.

3. The integrated process of claim 1 wherein the feedstock directional upgrading unit of step 1) is in the form of one of a moving bed, a dense fluid bed, and a riser reactor.

4. The integrated process method according to claim 1, wherein the directional modification catalyst in step 1) is a supported catalyst containing a heavy metal scavenger and a basic auxiliary agent, wherein the carrier is 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 scavenger is one or more of Bi, Ce, Sn, Cr and La, and the active component of the basic auxiliary agent is at least one of Li, Na, Ca, Mg, K and Ba.

5. The integrated process of claim 1, wherein the selective hydrorefining catalyst in step 2) is a supported catalyst, wherein the carrier is one or more of macroporous alumina, amorphous silica-alumina and a molecular sieve, and the supported metal component is one or more of Ni, Mo, Co and W.

6. The integrated process method according to claim 1, wherein the gasoline and diesel oil adsorption separation unit in the step 4) adopts a fixed bed or a simulated moving bed, and the adsorbent is one or more of white carbon black, a mesoporous high-silicon molecular sieve, activated carbon and clay.

7. The integrated process of claim 1, wherein the olefin production increasing unit in step 6) is in the form of one of riser, reducing riser, downer and downer reducing reactor, and the olefin production increasing catalyst is at least one of fully crystalline high silicon beta, mercerized, ZSM-5, APO-5, TS-1, MCM-22 and Y, IM-5 molecular sieves.

8. The integrated process of claim 1, wherein the aromatics production catalyst in step 7) is a metal-modified composite molecular sieve catalyst, the molecular sieve is at least two of Y, mordenite, beta, ZSM-5, MCM-22, and MCM-48, and the metal-modified component is at least one of Ni, Mo, Zn, Pt, Pd, Re, Sn, W, and Co.

Technical Field

The invention relates to the technical field of production of low-carbon olefins, aromatic hydrocarbons and needle coke, in particular to an integrated process method for maximally producing chemicals.

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 and heavy 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 or heavy oil processing technologies mainly include several technical routes of steam cracking, catalytic cracking and hydrocracking, have strong raw material dependence, and are 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 and relatively single chemical variety in the existing technology for preparing chemicals from crude oil or heavy oil, integrates the processes of directional modification of raw oil, adsorption and separation of gasoline and diesel hydrocarbons, aromatic hydrocarbon yield increase, olefin yield increase, needle coke yield increase and the like, and converts oil products into low-carbon olefin, aromatic hydrocarbon and high-quality needle coke to the maximum extent.

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

the invention provides an integrated process method for maximally producing chemicals, wherein raw oil is directionally modified, a processing unit is selected according to the characteristics of a modified product, chemicals are maximally produced, the yield of the chemicals can reach 70-80%, and the integrated process method comprises the following steps:

1) raw oil is firstly fed into a raw material directional modification unit, and under the action of a directional modification catalyst, under the conditions of reaction temperature of 350-650 ℃, pressure of 0.1-1.0 MPa and steam/oil mass ratio of 0.1: 1-10: 1, directional decarburization, demetalization and cracking modification reaction of heavy components are carried out to obtain hydrogen, a fulvene gas, modified fulvene distillate oil and coke;

2) feeding the modified fulvene distillate oil obtained in the step 1) into a selective hydrofining unit, and reacting at the reaction temperature of 60-180 ℃, the pressure of 2.0-4.0 MPa and the mass space velocity of 0.5-3.0 h under the action of a selective hydrofining catalyst^-1Removing colloid, alkadiene and alkaline nitrogen impurities under the condition that the volume ratio of hydrogen to oil is 400: 1-800: 1 to obtain fuel gas and refined distillate oil;

3) the refined distillate oil obtained in the step 2) enters a refined distillate oil cutting unit to obtain gasoline and diesel oil fractions (less than or equal to 350 ℃) rich in olefin and heavy distillate oil (more than 350 ℃) rich in polycyclic aromatic hydrocarbon;

4) the gasoline and diesel oil fraction obtained in the step 3) enters a gasoline and diesel oil adsorption separation unit, and is subjected to adsorption at the temperature of 60-120 ℃, the pressure of 0.2-0.6 MPa and the mass space velocity of 1.0-2.0 h under the action of an adsorbent^-1Under the conditions of (1), carrying out gasoline-diesel oil aromatic hydrocarbon groupSeparating the components from the non-aromatic hydrocarbon components to obtain aromatic hydrocarbon components and alkene-rich non-aromatic hydrocarbon components;

5) the heavy distillate oil obtained in the step 3) enters a needle coke yield increasing unit, and needle coke, coking gasoline and diesel oil and alkene-rich gas are obtained through delayed coking and high-temperature calcination procedures;

6) the adsorbed alkene-rich non-aromatic hydrocarbon component obtained in the step 4) and the coking gasoline and diesel oil obtained in the step 5) enter an alkene yield increasing unit together, and under the action of an alkene yield increasing catalyst, a directional catalytic cracking reaction is carried out under the conditions of 500-650 ℃ of reaction temperature, 0.1-0.5 MPa of pressure, 5: 1-20: 1 of agent-oil ratio and 0.1: 1-1.5: 1 of steam-oil mass ratio to obtain alkene-rich gas, cracked aromatic-rich gasoline and diesel oil and coke;

7) the aromatic hydrocarbon adsorbing component obtained in the step 4) and the cracked aromatic-rich gasoline and diesel oil obtained in the step 6) enter an aromatic hydrocarbon yield increasing unit together, and under the action of an aromatic hydrocarbon yield increasing catalyst, the reaction temperature is 360-500 ℃, the pressure is 3.0-6.0 MPa, and the volume airspeed is 0.5-2.0 h^-1And performing selective cracking reaction on the hydrogen-oil volume ratio of 800: 1-1500: 1 to obtain fuel gas, saturated liquefied gas, light aromatic hydrocarbons (benzene, toluene and xylene) and C₉/C₁₀Aromatic hydrocarbons;

in the step 1), the raw material is subjected to directional modification, heavy oil macromolecules in the raw material oil undergo directional modification reaction, the conversion rate of the 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 heavy oil is 60-85 wt%.

The raw oil in the step 1) is at least one of paraffin-base crude oil, intermediate-base crude oil, naphthenic base crude oil, wax oil, atmospheric residue oil, vacuum residue oil, oil sand asphalt and deasphalted oil. The reactor is in the form of one of moving bed, dense-phase fluidized bed and riser reactor. The directional 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-silicon 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.

The selective hydrofining catalyst in the step 2) is a supported catalyst, wherein the carrier is one or more of macroporous alumina, amorphous silica-alumina and a molecular sieve, and the supported metal component is one or more of Ni, Mo, Co and W.

In the step 4), the gasoline and diesel oil adsorption separation unit adopts a fixed bed or a simulated moving bed, and the adsorbent is one or more of white carbon black, a mesoporous high-silicon molecular sieve, activated carbon and white clay.

In the olefin yield increasing unit in the step 6), the adopted reactor form is one of a riser, a reducing riser, a downer and a downer reducing reactor, and the olefin yield increasing catalyst is at least one of fully crystalline high-silicon beta, mercerized, ZSM-5, APO-5, TS-1, MCM-22 and Y, IM-5 molecular sieves.

In the step 7), 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, MCM-22 and MCM-48, and the metal modified component is at least one of Ni, Mo, Zn, Pt, Pd, Re, Sn, W and Co.

Compared with the prior art, the integrated process method for maximally producing chemicals provided by the invention has the following beneficial effects:

1) the raw material adaptability is strong, and the processing process is simple: the crude oil directional modification unit is adopted to modify crude oil or heavy oil into high-quality chemical production raw materials (rich in olefin and aromatic hydrocarbon), so that 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 modified gasoline and diesel oil is separated from non-aromatic hydrocarbon (alkane and olefin) and aromatic hydrocarbon components through adsorption separation, and is converted into low-carbon olefin and aromatic hydrocarbon by matching a subsequent processing unit according to the characteristics of the components, and the total chemical yield reaches 70-80%.

Drawings

FIG. 1 is a schematic flow diagram of an integrated process for maximizing the production of chemicals according to the present invention.

Detailed Description

The following will further describe the implementation and effects of the method according to the present invention with reference to specific examples, but the present invention is not limited thereto.

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.

Raw material directional modification unit: the reactor adopts a descending bed reactor, the directional modification catalyst adopts Ba-Ca/attapulgite (based on the catalyst, the Ba content is 5.0 wt%, the Ca content is 3.0 wt%, and the balance is attapulgite and other binders), and the reaction conditions are as follows: the temperature is 480 ℃, the pressure is 0.1MPa, and the steam/oil mass ratio is 3: 1.

A selective hydrorefining unit: the catalyst adopts Ni-Mo/macroporous alumina (based on the catalyst, 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 120 ℃, the pressure is 3.0MPa, and the mass space velocity is 2.0h^-1And the volume ratio of hydrogen to oil is 600: 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 carbon material yield increasing unit: the reaction temperature of the coking device is 510 ℃, and the reaction pressure is 0.15 MPa.

An olefin stimulation 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.

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^-1And the volume ratio of hydrogen to oil is 900: 1.

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.

Raw material 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.

A selective hydrorefining unit: the catalyst adopts Ni-Co/amorphous silicon aluminum + alumina (based on the catalyst, the Ni content is 10 wt%, the Co content is 4.0 wt%, and the balance is amorphous silicon aluminum + alumina), and the reaction conditions are as follows: the temperature is 140 ℃, the pressure is 3.0MPa, and the mass space velocity is 1.5h^-1And the volume ratio of hydrogen to oil is 500: 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 1.5h^-1。

A carbon material yield increasing unit: the reaction temperature of the coking device is 510 ℃, and the reaction pressure is 0.15 MPa.

An olefin stimulation 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.

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.

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.

Raw material 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.

A selective hydrorefining unit: the catalyst adopts Ni-Mo-Co/alumina (based on the catalyst, the Ni content is 10 wt%, the Mo content is 5.0 wt%, the Co content is 4.0 wt%, and the balance is alumina), and the reaction conditions are as follows: the temperature is 150 ℃, the pressure is 4.0MPa, and the mass space velocity is 1.5h^-1And the volume ratio of hydrogen to oil is 600: 1.

Gasoline and diesel oil adsorption separation unit: adopting a simulated moving bed process, wherein the adsorbent is activated carbon, and the separation conditions are as follows: the adsorption temperature is 100 ℃, the pressure is 0.8MPa, and the mass space velocity is 2.0h^-1。

A carbon material yield increasing unit: the reaction temperature of the coking device is 510 ℃, and the reaction pressure is 0.15 MPa.

An olefin stimulation 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.

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.

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

Example 4

The vacuum residue of a certain refinery is used as a raw material, and the properties of the raw material are shown in table 1.

Raw material directional modification unit: adopting a descending bed reactor, adopting a Bi-Ba-Mg/high-silicon MCM-48 molecular sieve (taking the catalyst as a reference, the Bi content is 2.0 wt%, the Ba content is 8.0 wt%, the Mg content is 6.0 wt%, and the balance is the molecular sieve and a binder), and reacting under the following conditions: the temperature is 480 ℃, the pressure is 0.5MPa, and the steam/oil mass ratio is 4.0: 1.

A selective hydrorefining unit: the catalyst adopts Ni-Co/amorphous silicon aluminum + alumina (based on the catalyst, the Ni content is 14 wt%, the Co content is 6.0 wt%, and the balance is amorphous silicon aluminum + alumina), and the reaction conditions are as follows: the temperature is 120 ℃, the pressure is 4.0MPa, and the mass space velocity is 1.0h^-1And the volume ratio of hydrogen to oil is 600: 1.

Gasoline and diesel oil adsorption separation unit: adopting a simulated moving bed process, wherein the adsorbent is activated 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 carbon material yield increasing unit: the reaction temperature of the coking device is 510 ℃, and the reaction pressure is 0.15 MPa.

An olefin stimulation unit: adopting a descending bed reducing reactor, wherein the catalyst is a high-silicon ZSM-5+ beta molecular sieve catalyst, and the reaction conditions are as follows: the reaction temperature is 580 ℃, the pressure is 0.3MPa, the agent-oil ratio is 15:1, and the steam-oil mass ratio is 0.8: 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 10 wt%, the Pd content is 0.2 wt%, the beta molecular sieve content is 40 wt%, the Y molecular sieve content is 20 wt%, and the balance is alumina), and the reaction conditions are as follows: the temperature is 430 ℃, the pressure is 8.0MPa, and the volume space velocity is 1.0h^-1And the volume ratio of hydrogen to oil is 1000: 1.

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

TABLE 1 examples 1-4 Properties of the raw materials

Raw materials	Example 1	Example 2	Example 3	Example 4
					Density, g/cm3	0.862	0.90	0.935	0.949
API°	32.8	24.6	15.2	14.3
					Wax content, wt.%	28.6	10.8	5.8	4.6
Freezing point, deg.C	30	-2	-12	-15
					Carbon residue in wt%	3.28	6.0	11.4	14.0
Colloid + asphaltene, wt.%	7.45	11.4	22.6	25.2
					Sulfur content, ug/g	1800	2600	28000	30000
Nitrogen content, ug/g	2100	3200	5100	4800
					Metal content, ug/g	16	35	140	220

TABLE 2 examples 1-4 Material balances

Examples	Example 1	Example 2	Example 3	Example 4
					Raw materials in wt%
Raw oil	100	100	100	100
					Hydrogen gas	1.29	1.52	1.64	1.82
Product, wt%
					Hydrogen gas	0.4	0.36	0.38	0.36
Fuel gas	4.69	4.94	4.87	4.46
					Alkene-rich gas	58.96	56.27	55.69	54.21
Ethylene	7.21	6.01	6.35	6.84
					Propylene (PA)	28.58	25.62	24.65	25.38
Butene (butylene)	13.25	12.35	11.88	11.92
					Trienes as inhibitors of HIV infection	49.04	43.98	42.88	44.14
Saturated liquefied gas	4.93	5.68	4.89	5.62
					Benzene, toluene and xylene	10.89	10.67	12.81	12.77
C9/C10 aromatic hydrocarbons	7.28	8.42	7.68	8.22
					Needle coke	8.99	8.85	9.01	8.34
Burning coke	5.15	6.33	6.31	7.84
					Total yield of chemicals	76.2	71.92	72.38	73.47

As shown in Table 2, the total yield of chemicals (olefin, aromatic hydrocarbon and carbon material production raw materials) can reach 71-76% and the total hydrogen consumption is only 1.3-1.8 wt% after the paraffin-based crude oil, the intermediate-based crude oil, the naphthenic base crude oil and the slag reduction are processed by the method of the invention.